CN110066685A - The stabilized hydrogenation object reuse method of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product - Google Patents

The stabilized hydrogenation object reuse method of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Download PDF

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CN110066685A
CN110066685A CN201810109800.5A CN201810109800A CN110066685A CN 110066685 A CN110066685 A CN 110066685A CN 201810109800 A CN201810109800 A CN 201810109800A CN 110066685 A CN110066685 A CN 110066685A
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hydrocarbon
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hydrogenation
hydrogen
reaction
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何巨堂
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The stabilized hydrogenation object reuse method of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product, suitable for using the direct hydrogenation liquefaction of coal reaction process of hydrogen supply dissolvent, heavy-oil hydrogenation reaction process, the stabilized hydrogenation conversion product that kerosene refines the middle matter hydrocarbon in the gas phase RUA-HS-V of the reaction product RUA-P of the preceding conversion zone RUA of hydrogenation process altogether is recycled to RUA reuse, form two stage process i.e. " hydrogen supply hydrocarbon obtained by the stabilized hydrogenation product of catalysis reaction intermediate gas phase product is recycled and/or is recycled with defeated target feedstock hydrocarbon ", the stripping step containing liquid product of settable RUA increases half way hydrogen supply dissolvent internal circulating load, the hydrogen supply capacity of half way hydrogen supply dissolvent can be given full play in gas phase RUA-HS-V or reduce second heat soaking time or reduce long circulating circuit hydrogen supply dissolvent dosage or The heavy hydrogen supply dissolvent reaction time is reduced, hydrogen supply dissolvent cycle cost is greatly lowered, improves process economy.

Description

The stabilized hydrogenation object reuse of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Method
Technical field
The present invention relates to the stabilized hydrogenation object reuse methods of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product, fit For using the direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation reaction process, kerosene of hydrogen supply dissolvent to refine hydrogenation reaction mistake altogether The stabilized hydrogenation conversion product of middle matter hydrocarbon in the gas phase RUA-HS-V of the reaction product RUA-P of the preceding conversion zone RUA of journey is recycled to RUA reuse, foring two stage process, i.e. " hydrogen supply hydrocarbon circulation obtained by the stabilized hydrogenation product of catalysis reaction intermediate gas phase product makes It is recycled with and/or with defeated target feedstock hydrocarbon ", it is molten that the stripping step containing liquid product of settable RUA increases half way hydrogen supply Agent internal circulating load, when can give full play to the hydrogen supply capacity of half way hydrogen supply dissolvent in gas phase RUA-HS-V or reduce secondary heat cracking reaction Between or reduce long circulating circuit hydrogen supply dissolvent dosage or reduce the heavy hydrogen supply dissolvent reaction time, hydrogen supply dissolvent is greatly lowered and follows Ring cost improves process economy.
Background technique
Application of the invention is described first.
Hydrogen supply hydrocarbon described herein refers to that direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation reaction process, kerosene refine altogether In hydrogenation process with hydrogen supply function the hydrocarbon component, hydrogen supply hydrocarbon include the double ring arene of fractional saturation, fractional saturation it is more Cycloaromatics.In hydrogen supply hydrocarbon, the hydrogen supply speed of dihydro body is all larger than tetrahydro body, the dihydro body of thrcylic aromatic hydrocarbon and the dihydro of double ring arene Body is compared, and it is low that hydrogen supply speed has height to have；Although test is it has been proved that polycyclic aromatic hydrocarbon has the energy of transmitting hydrogen without hydrogen supply capacity Power.At 400 DEG C, the opposite hydrogen supply speed of following component is as follows:
Hydrocarbon material of the present invention refers to carbon containing, protium liquid and/or solid, such as oil and/or coal.
Hydrocarbon material hydrogenation process RU of the present invention refers to wrapping using hydrocarbon material as the hydrogenation process of raw material Include the hydrofining reaction and/or catalytic hydrocracking reaction and/or heat from hydrogenation cracking reaction and/or thermal cracking free radical of hydrocarbon material The reaction process such as the stabilized hydrogenation reaction of fragment.
Hydrocarbon powder of the present invention adds hydrogen direct liquefaction process, generally refers to direct hydrogenation liquefaction of coal process, still It may include combining the liquefied other hydrocarbon powders being mainly made of carbon, protium with coal dust, such as waste plastics, useless rubber It can be used for liquefied powder made of the solids such as glue.In general, in order to accelerate hydrogen supply speed, inhibit thermal condensation reaction, reduction reaction Heat improves reaction operability, and efficient hydrocarbon powder adds hydrogen direct liquefaction process to use hydrogen supply dissolvent oil.
Heavy oil of the present invention refers to mainly being higher than by normal boiling point 350 DEG C of hydro carbons, preferably mainly by routine The weight that the heavy hydrocarbon oil that hydro carbons of the boiling point higher than 450 DEG C forms, the preferably mainly hydro carbons by normal boiling point higher than 530 DEG C form Matter hydrocarbon ils is particularly preferably the heavy rich in aromatic structure unit mainly low higher than 530 DEG C of hydrogen content by normal boiling point The inferior heavy oil of hydro carbons composition；For the hydrogenation process especially heat from hydrogenation cracking reaction process of inferior heavy oil, in order to add Fast hydrogen supply speed inhibits thermal condensation reaction, reduces heat of reaction, improves reaction operability, and efficient inferior heavy oil adds hydrogen anti- Process is answered to need using hydrogen supply dissolvent oil.
The hydrofining reaction of the hydrocarbon material, can be plus hydrogen removing impurities qualitative response such as hydrodemetallization reaction plus hydrogen is de- Organic oxygen is reacted plus hydrogen removal of organic sulfur reacts, adding hydrogen to take off, organic oxygen is reacted plus the de- organochlorine of hydrogen reacts plus the de- Organic fluoride of hydrogen is anti- It answers, can be unsaturated carbon-carbon bond adds hydrogen saturated reaction such as olefins hydrogenation reaction, alkynes that hydrogen saturated reaction, aromatic hydrocarbons is added to add Hydrogen saturated reaction can be one or more of above-mentioned reaction.The heat from hydrogenation cracking reaction and thermal cracking of the hydrocarbon material are certainly It is reacted, is usually always occurred together, it is generally present in the high-temperature hydrogenation of coal and/or heavy oil by the stabilized hydrogenation of base fragment During heat cracking reaction, the hydrogenation process that is refined altogether such as direct hydrogenation liquefaction of coal reaction process, kerosene, heavy-oil hydrogenation hot tearing In change reaction process, heavy-oil hydrogenation reaction process.
Therefore, hydrocarbon material hydrogenation process of the present invention, the high-temperature hydrogenation that can be coal and/or inferior heavy oil are anti- It answers process, even, can be extra heavy oil hydrodemetallization reaction process, hydrodesulfurization reaction process, hydrodenitrogeneration were reacted Journey, front hydrofining reaction section such as hydrodemetallization conversion zone plus the hydrogen that can be extra heavy oil hydrocracking reaction process are de- Reaction of Salmon-Saxl section and/or hydrodenitrogeneration conversion zone.
2 of liquid material (including slurries) serial operation or the hydrocarbon material hydrogenation reaction system of multiple conversion zones composition is described below System.
A conversion zone of the present invention, refers to the gas comprising hydrocarbon material hydrogenation reaction step and the step gas-liquid product The technical process of liquid separating step.
By taking direct hydrogenation liquefaction of coal reaction process as an example, it belongs to the high hydrocarbon material deep hydrogenation of hydrogen consumption and reacted Journey, since always main body reaction is rapidly completed in the reaction zone in front to easy reactive component, also because common process middle front part reaction zone is total It is that hydrogen purity is high, objectionable impurities gas concentration is minimum, the easy highest reaction zone of reactant concentration, therefore, from hydrogenation reaction speed It is said on degree, reaction hydrogen-consuming volume, wait the reaction compartment of liquid reaction volumes, the amounts of hydrogen of front reaction zone consumption is anti-much larger than rear portion The amounts of hydrogen for answering area to consume, and usually discharge a large amount of reaction heat；Bond strength simultaneously between impurity element and carbon is lower Chemical bond is prone to cleavage reaction, and therefore, the foreign gas amount that front reaction zone generates generally also is much larger than rear portion reaction zone The foreign gas amount of generation is the main generation area of foreign gas；With the extension of the reaction mechanism mechanism of reaction, solid and/or high boiling hydrocarbon component Gradually it is converted into the hydro carbons of low boiling point, mid-boiling point, the average molecular weight of such liquid (including slurries) is smaller and smaller, mean boiling point It is lower and lower.Based on above-mentioned analysis, the whole hydrogenation process can be usually divided on a macro scale: the first hydrogenation reaction mistake Journey, that is, hydrogen consumption is high, foreign gas yield is high, the front reaction process more than liquid material high boiling component, the second hydrogenation process The rear portion reaction process that i.e. hydrogen consumption is low, foreign gas low output, liquid material high boiling component are few.
Middle matter hydrocarbon described herein refers to that conventional boiling range is 230~400 DEG C of hydro carbons, and the hydrogen supply hydrocarbon of the boiling point range is logical It is often ideal hydrogen supply dissolvent component.
The either heat from hydrogenation cracking reaction of the inferior heavy oil of direct hydrogenation liquefaction of coal reaction process or macromolecular Journey, macromolecular fracture therein are converted into the process of the middle matter hydrocarbon of suitable molecular weight, are the tandem reactor process of a multi-step, Therefore, the initial stage lighting of heavy target material has been made lower than 400 DEG C of hydrocarbon products, still in not yet formation wide variety of conventional boiling point The reaction process position (this transition point certainly exists) that task is basically completed, it is anti-can to be divided into front for W-response process Area, rear portion reaction zone are answered, at this time the middle matter hydrocarbon in front reaction zone product, will mainly be converted by hydrogen supply dissolvent or hydrogen supply dissolvent Object composition.In this way, said from the angle that evaporation or air lift vaporize, hydrogen supply dissolvent and solid particle, high boiling asphalitine and heavy oil, Normal boiling point is higher than 400 DEG C especially greater than 530 DEG C of hydro carbons, there is obvious or huge boiling-point difference.Due to strongly exothermic Hydrogenation process usually using a large amount of hydrogen, therefore, under hydrogen and the gas stripping of other gas components, the confession The middle matter hydrocarbon of hydrogen solvent naphtha, will be balanced distribution between the gas phase and liquid phase of reaction mass, in operating pressure, operation temperature Under conditions of degree, material composition, reaction depth are certain, certain distribution ratio will be formed, this is coal and/or heavy oil plus hydrogen lighting A kind of specific vapor liquid equilibrium property existing for reaction process.And for being mainly higher than 530 DEG C of hydro carbons group by normal boiling point At heavy oil unifining process, the performance of this characteristic becomes apparent: hydrogen supply dissolvent and heavy hydrocarbon feeds, heavy products it Between, at least there is 100~150 DEG C of boiling-point difference.
The normal boiling point of either middle coalite tar is higher than 350 DEG C or the double distilled grouping higher than 450 DEG C or higher than 530 DEG C At raw material hydrocarbon RU-F1 heat from hydrogenation cracking process or direct hydrogenation liquefaction of coal reaction process, the operation scheme of optimization is usual Using at least 2 up flow type expanded bed reactors, substantially front hydrogenator carries out either shallow hydrogenation process RUA, rear portion at this time Hydrogenator carries out deep hydrogenation process RUB；Since easy reactive component completes most of reaction in front reaction zone, because This, rear portion reaction process usually carries out the cleavage reaction of the higher carbon-carbon bond of chemical bond bond strength, such rear portion reaction process Operation temperature is usually some higher；Either shallow hydrogenation process RUA, operation temperature is usually relatively low, usually 350~470 DEG C, one As be 380~460 DEG C, but reaction temperature value of the reaction temperature value generally compared with deep hydrogenation process RUB is lower such as logical Often low 5~50 DEG C out；Deep hydrogenation process RUB, operation temperature is usually higher, typically up to 410~480 DEG C, generally up to 425 ~475 DEG C, the reaction temperature generally it is higher compared with the reaction temperature of either shallow hydrogenation process RUA be such as usually higher by 5~50 DEG C or It is higher.In this way, after hydrogen supply dissolvent oil enters rear portion reaction zone, if cannot with hydrogen-abstracting agent match reaction, it will occur with Heat cracking reaction is leading heat from hydrogenation cracking reaction；Since the hydrogen-abstracting agent quantity of rear portion reaction zone is far fewer than front reaction zone, And part reaction product has been converted into middle matter hydrocarbon or hydrogen supply agent, therefore, in the charging of usual rear portion reaction zone, does not need front Hydrogen supply agent more than reaction zone equivalent, that is to say, that need excessive hydrogen supply agent or hydrogen supply agent conversion product reaction system is discharged.
The heat from hydrogenation cracking of the either inferior heavy oil of direct hydrogenation liquefaction of coal suspension bed reaction process or macromolecular is outstanding Floating bed reaction process, hydrogen supply dissolvent oil is in the aromatization that the leading reaction of front reaction zone is hydrogen supply, therefore, molecular weight It is varied less with mean boiling point, it is contemplated that the front reaction zone of hydrocarbon material hydrogenation process is generally inherently a generation The reaction zone of a large amount of removing impurities qualitative responses and aromatic hydrocarbons saturated reaction, therefore, the hydro carbons in the gas-phase product of front reaction zone, usual one Surely be mainly made of hydrogen supply dissolvent or hydrogen supply dissolvent conversion product, that is to say, that there are a kind of hydrogen supply dissolvent and heavy charge, The relative separation effect of heavy product, usual 20~50% hydrogen supply dissolvent or hydrogen supply dissolvent conversion product are present in reaction medium In gas phase, such huge distribution ratio forms surprising separating effect, and the task of the present invention is make full use of this opposite Separating effect proposes improved process.
It is opposite to belong to " liquid reactive efficient hydrogen supply dissolvent " word with the hydrogen supply dissolvent in conventional reaction medium liquid phase It answers, the hydrogen supply dissolvent in conventional reaction medium gas phase is known as " half way hydrogen supply dissolvent or efficiently keeping hydrogen solvent " by the present invention.
In the different processes of hydrocarbon material hydrogenation process described in detail below, the composition of reaction product.
Hydrocarbon material hydrogenation reaction of the present invention, refer to hydrogen exist and pressurized conditions under, carbon containing, protium liquid The hydrogenation reaction that body and/or solid such as oil and/or coal occur, occurs hydrofinishing for its feedstock oil of hydrocarbon oil hydrogenation process and/or adds Hydrogen heat cracking reaction generates the hydrocarbon products of at least part more low molecular weight or normal boiling point lower than 450 DEG C, straight for coal hydrogenation Connect its feed coal of liquefaction reaction process occur swollen thermosol, primary pyrolysis, the secondary thermal cracking of intermediate product, free radical stabilized hydrogenation, The reactions such as thermal condensation generate the hydrocarbon products that at least part normal boiling point is lower than 450 DEG C.
Hydrocarbon material hydrogenation process of the present invention, typical example are that high temperature coal-tar floating bed hydrogenation deep refining is anti- It answers process, middle coalite tar floating bed hydrogenation heat cracking reaction process, direct hydrogenation liquefaction of coal reaction process, kerosene to refine altogether to add Hydrogen reaction process, petroleum based heavy fuel oils suspension bed or boiling bed hydrogenation cracking reaction process, usually using hydrogen supply dissolvent oil or dilution Oil.
Hydrocarbon material hydrogenation reaction of the present invention, reaction product BASE-RU-P, at least gas-liquid two-phase logistics are most Situation belongs to gas, liquid, solid three-phase logistics.Hydrogenation reaction effluent RU-P-X of the present invention is for being discharged hydrogenation reaction product BASE-RU-P occurs in the form of 1 tunnel or 2 tunnels or multichannel material, is gas phase or liquid phase or gas-liquid mixed phase or gas-liquid-solid three-phase object Stream.
Hydrocarbon material heat from hydrogenation cracking reaction process of the present invention, including hydrocarbon material heat cracking reaction and thermal cracking free radical The stabilized hydrogenation of fragment reacts, and it is total to be present in direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation heat cracking reaction process, kerosene It processes in the reaction process such as heat from hydrogenation cracking reaction process.
Hydrocarbon material heat from hydrogenation cracking reaction process of the present invention, usually using up flow type expanded bed hydrogenator
Expanded bed reactor of the present invention is vertical up-flow reactor, and expanded bed reaction is belonged to when using catalyst Device；The vertical central axis upright for referring to working condition reactor after installing is in ground；Up flow type refers to reaction process object Material main body flow direction travels through reaction compartment or catalyst bed or the catalyst co-flow with uplink from bottom to top；Expanded bed Refer to that working condition catalyst bed is in swelling state, catalyst bed expansion ratio, which is defined as catalyst bed, has reaction former The ratio of the height CUH of the empty bed static condition of the maximum height CWH and catalyst bed of working condition when material passes through KBED, in general, referred to as slight expanded-bed when KBED is lower than 1.10, referred to as ebullated bed when KBED is between 1.25~1.55, and suspension bed It is considered as the expanded bed of most extreme form.
Back-mixing stream expanded bed reaction zone of the present invention, refers to the mode of operation of the reaction zone using expanded bed reactor There are liquid stream back-mixings there is circulation fluid in other words；Back-mixing stream or circulation fluid refer to the intermediate product XK or final at flow points K At least part liquid phase XK-L in product X K is as the upstream reaction zone circulating fluid XK-LR return logistics XK, circulating fluid XK- The reaction product of LR flows through K point and is present among XK.The mode for forming back-mixing stream can be any appropriate mode, such as react Built-in inner ring flow cartridge, built-in outer ring flow cartridge, built-in liquid collecting cup+diversion pipe+circulating pump, external circulation pipe is arranged in device Deng.Under above-mentioned working condition, due to the multiple circulate operation of liquid product or intermediate liquid product, so that in gas-phase product It experienced less thermal response for hydrogen supply dissolvent oil is oily with respect to the hydrogen supply dissolvent in liquid phase, therefore remaining more for Hydrogen Energy Power is more suitable for using the present invention.
The liquid collecting cup or liquid trap being arranged in reactor of the present invention, refer to being arranged in reactor for collecting The container of liquid, usual top or upper side opening, bottom or lower side installation diversion pipe are for conveying or being discharged collection Liquid；The top liquid trap of expanded bed reactor is typically mounted on the de- liquid zone of gas-liquid material, obtains the liquid containing a small amount of bubble With gas-liquid mixed phase logistics or obtain liquids and gases.Typical example is the heavy oil boiling bed hydrogenation reaction that H-OIL technique uses Device.
Hot high score device of the present invention, refers to the gas-liquid separation equipment for separating high-temp gas-liquid material.
Two sections of the present invention or multi-stek hydrogenation method refer to comprising two conversion zones or multiple conversion zones plus hydrogen side Method.
A hydrogenation reaction section of the present invention, to it referring to entering a hydrogenation process since feedstock hydrocarbon Hydrogenation products gas-liquid separation obtains at least one process section until generating the liquid product that oil forms by least part, includes The gas-liquid separation process of the hydrogenation reaction product of the hydrogenation process and this section of the hydrogenation reaction section.Therefore, one-stage hydrogenation side Method, the process for being commonly referred to as initial hydrocarbon feedstock only includes a hydrogenation reaction section and a hydrogenation products gas-liquid separation Adding for 1 or 2 or more serial operation can be used in the flow model of journey, a hydrogenation reaction section as needed Hydrogen reactor, therefore number of reactors and form are not the foundations for determining conversion zone, what one or some tandem reactors formed Reaction step and its product separator common combination could form the hydrogenation reaction section in a complete meaning.
Secondary hydrogenation method of the present invention refers to that the process of initial feedstock hydrocarbon includes liquid material processing stream Journey is the flow model of serial operation formed " by two different hydrogenation processes and hydrogenation products gas-liquid separation process ", The logistics that wherein at least a part of one-stage hydrogenation generates oil composition enters secondary hydrogenation reaction process.
Three sections of method of hydrotreating of the present invention refer to that the process of initial hydrocarbon feedstock includes liquid material processing flow For the flow model of serial operation formed " by three different hydrogenation processes and hydrogenation products gas-liquid separation process ", The logistics that middle at least part one-stage hydrogenation generates oil composition enters secondary hydrogenation reaction process, and at least part secondary hydrogenation is raw Logistics at oil composition enters three sections of hydrogenation processes.The flowage structure of the method for hydrotreating of more multistage, according to mentioned above principle class It pushes away.Multi-stek hydrogenation method, refer to initial hydrocarbon feedstock process include liquid material processing flow be serial operation " by The flow model of three or more different hydrogenation processes and hydrogenation products gas-liquid separation process " composition.
Three sections of method of hydrotreating, it is serial operation that the process for referring to initial hydrocarbon feedstock, which includes liquid material processing flow, The flow model formed " by three different hydrogenation processes and hydrogenation products gas-liquid separation process ", according to this definition, It is obvious that the gas-liquid separation process of the difference section hydrogenation products, can independently carry out, can also partly or entirely combine into Row.
Below in conjunction with direct hydrogenation liquefaction of coal reaction process, middle coalite tar heavy oil RU-F1 hydrogenation process into Row description.
For problem analysis, the present invention cannot liquefied coal component (packet by discharge direct hydrogenation liquefaction of coal reaction process Include ash content, inertinite point), being considered as can not liquefaction coal component.
For direct hydrogenation liquefaction of coal reaction process, the present invention drips liquefiable coal component and direct hydrogenation liquefaction of coal product Green matter is considered as the main hydrogen supply object or hydrogen-abstracting agent of hydrogen supply dissolvent, and the hydrogen supply in specific reaction process point reaction medium is molten The operability that agent/(liquefiable coal component+asphalitine) ratio is considered as the process point of direct hydrogenation liquefaction of coal reaction process is special Value indicative K300, it is the hydrogen supply hydrocarbon of reaction process point and the quantity ratio for taking hydrogen object by force.
For direct hydrogenation liquefaction of coal reaction process, the present invention is by the coal dust and coal in specific reaction process point reaction medium Hydrogen direct liquefaction product asphalitine is added to be considered as liquid phase dispersion medium, by (hydrogen supply dissolvent+direct hydrogenation liquefaction of coal product is retortable Oil) it is considered as potential solvent phase, by (hydrogen supply dissolvent+retortable oil of direct hydrogenation liquefaction of coal product)/(liquefiable coal component+drip Green matter) ratio be considered as the potential solution dilution characteristic value K700 of direct hydrogenation liquefaction of coal reaction process point, it is thermal condensation The dilution of potential object.
For using the heavy-oil hydrogenation reaction process of hydrogen supply dissolvent, the present invention cannot reduce boiling point for be discharged reaction process Oil ingredient (including carbon residue, asphalitine, metal, solid), being considered as can not lighting component.
For using the heavy-oil hydrogenation reaction process of hydrogen supply dissolvent, the present invention can lighting the hydrocarbon component (original can lightweight Carburetion and its intermediate product that secondary lighting reaction occurs) be considered as the main hydrogen supply object of hydrogen supply dissolvent, by hydrogen supply dissolvent/ The ratio of (can lighting the hydrocarbon component) is considered as the maneuverability features value K300 of heavy-oil hydrogenation reaction process, is mainly used for existing big Measure the stage of reaction problem analysis of hydrogen-abstracting agent.
For using the heavy-oil hydrogenation reaction process of hydrogen supply dissolvent, the present invention will non-lighting heavy oil component and thermal condensation production Object is considered as liquid phase dispersion medium, and (hydrogen supply dissolvent+retortable oil of heavy oil lighting product) is considered as potential solvent phase, (will supply Hydrogen solvent+retortable the oil of heavy oil lighting product)/the ratio of (non-lighting heavy oil component and thermal condensation product) is considered as heavy oil and adds The potential solution dilution characteristic value K700 of hydrogen reaction process is mainly used for analyzing there are the stage of reaction of a large amount of hydrogen-abstracting agents and ask Topic.
Hydrocarbon material hydrogenation process RU of the present invention includes either shallow hydrogenation process or front reaction process or preceding Portion conversion zone RUA, deep hydrogenation reaction process or rear portion reaction process or rear portion conversion zone RUB, two sections of the present invention add Hydrogen methods, distribution ratio of the matter hydrocarbon in the gas phase and liquid phase of the general reaction material of front conversion zone RUA is relatively close to 1 in utilization The feature of (usually 0.5~2.0) recycles way by the middle matter solvent hydrocarbon in the gas-phase product of front conversion zone RUA Diameter improves the maneuverability features value K300 of front conversion zone RUA or improves potential solution dilution characteristic value K700 or reduction The outer ratio for long circulating hydrogen supply dissolvent oil；Meanwhile the quantity for the middle matter hydrocarbon that conversion zone RUB in rear portion is fed is adjusted or reduced to drop The K300 or K700 of its low relative surplus improve high boiling hydrocarbon concentration in liquid phase and improve hydrogenation reaction selectivity, improve liquid phase Middle catalyst concn, raising reactive hydrogen supply rate, raising goal response speed shorten thermal response time etc.；Pass through adjusting Middle matter hydrocarbon front conversion zone RUA, rear portion conversion zone RUB reaction mass in distribution, realize front conversion zone RUA and rear portion The relative equilibrium of the K300 or K700 of conversion zone RUB, the reaction selectivity for improving general reaction process solvent oil (are reduced negative anti- Answer) and for hydrogen efficiency, optimize W-response process, make heat from hydrogenation cracking reaction speed, hydrogen supply speed (reaction of hydrogen supply agent hydrogen supply, Hydrogen-abstracting agent hydrogen abstraction reaction) relative equilibrium, inhibit thermal condensation reaction, reduces excessive heat cracking reaction, makes mid-boiling point hydrogen supply agent and height The hydrogen supply depth relative equilibrium of boiling point hydrogen supply agent, and then realize the optimization of whole hydrogenation process operating condition.
The normal boiling point of middle coalite tar is higher than the original that 350 DEG C or the double distilled higher than 450 DEG C or higher than 530 DEG C are grouped as Hydrocarbon RU-F1 is expected, because comprising coal tar pitch and certain solid, suitable method of hydrotreating is anti-using up flow type expanded bed plus hydrogen Answer process RU；Hydrogenation process RU can be the process based on hydrofining reaction and a large amount of hydrofining reaction occur With the hydrocracking reaction of relatively small amount；Hydrogenation process RU is also possible to heat from hydrogenation cracking process and a large amount of hot tearing occurs Change reaction and the reaction of a large amount of stabilized hydrogenation.
Direct hydrogenation liquefaction of coal reaction process, because comprising coal dust and the possible circulation dregs of fat, suitable method of hydrotreating is Use the hydrogenation process RU of up flow type expanded bed；Hydrogenation process RU is usually to be swollen reaction, pyrolytic reaction plus hydrogen Reaction process based on heat cracking reaction, the reaction of free radical stabilized hydrogenation, but the pyrocondensation of pyrolysis intermediate product heavy hydrocarbon also occurs It closes reaction and generates asphaltene, preasphaltene even coke, the secondary heat scission reaction that generation is pyrolyzed intermediate hydrocarbon products generates small Molecule hydrocarbon and gas.
The either shallow hydrogenation process RUA refers to that its liquid product also needs deep hydrogenation to convert, and should not be understood as this The hydrogen consumption of step is low；Similarly, deep hydrogenation process RUB refers to that further hydro-conversion has occurred in its liquid phase feed, and The hydrogen consumption that should not be understood as the step is high.It is concentrated due to easy reactive component majority in front conversion zone and carries out hydrogenation reaction, it is more In number situation, if averagely dividing front conversion zone RUA and rear portion conversion zone according to reaction time, either shallow hydrogenation process is The unit feed hydrogen consumption of front reaction process RUA is typically much deeper than the unit feed hydrogen consumption of rear portion reaction process RUB.
Using the heat from hydrogenation cracking reaction process for the heavy oil that normal boiling point is 230~400 DEG C of hydrogen supply dissolvent oil, front is anti- Answer section need hydrogen supply dissolvent oil in a manner of liquid phase hydrogen supply hydrogen supply with accelerate reactive hydrogen supply rate, reduce liquid phase viscosity, reduce Liquid film surface tension reduces reaction heat, increases heat carrier quantity i.e. reduction reaction temperature rising；But when the initial stage hot tearing of macromolecular Change reaction and has occurred and that certain degree, for example when the lightweight rate of heavy oil reaches 50~65%, Light hydrocarbon products are had been able to When to the sufficient solvent naphtha of the heavy oil offer quantity of remaining non-lighting, the solvent naphtha in such rear portion conversion zone RUB can go out It is existing excessive, it needs to try to be isolated out reaction system, because a large amount of thermal cracking can occur for these excessive solvent naphthas Negative reaction as a result, reducing liquid yield, increasing the negative interactions such as reaction compartment, dilution target material concentration, and increases investment And energy consumption.
The normal boiling point of middle coalite tar is higher than 350 DEG C or the heavy distillat raw material hydrocarbon higher than 450 DEG C or higher than 530 DEG C RU-F1, the hydrocarbon component of the low boiling hydrocarbon fraction, that is, normal boiling point lower than 330 DEG C and high boiling hydrocarbon of intermediate product therein evaporate i.e. often The hydrocarbon component of the rule boiling point higher than 330 DEG C is compared, and usual impurity content is lower, residual carbon content is lower, and streaming is swollen in use During the hydrofining reaction of swollen bed such as suspension bed, low boiling hydrocarbon fraction is usually therein compared with high boiling hydrocarbon-fraction Impurity element be easier plus hydrogen hydrogenolysis abjection, colloid therein be easier plus hydrogen take off carbon residue, therefore with add hydrogen degree deepen, it is low Boiling hydrocarbon fractions plus hydrogen removing impurities matter, plus hydrogen take off carbon residue task complete first, but at this time high boiling hydrocarbon fraction plus hydrogen removing impurities Matter, plus hydrogen take off carbon residue task not yet completes, if continue combined depth add hydrogen, be bound to cause low-boiling fraction excessive hydrogenation, Excessive thermal cracking, and the deep hydrogenation process of high boiling hydrocarbon-fraction certainly will need more subsequent reactions spaces, and low boiling The intermediate hydrogenation products of point fraction reduce the concentration of high boiling hydrocarbon fraction as diluent therefore reduce reaction speed, and low boiling point evaporates The intermediate hydrogenation products divided participate in the competitive Adsorption of catalyst surface and the contention to reactive hydrogen, at this point, in order to improve higher boiling The selectivity of hydrocarbon hydrogenation process is wished low boiling point intermediate product such as routine gaseous hydrocarbon, naphtha component, diesel oil hydrocarbon in technique Reaction process is discharged in component and foreign gas in time, and higher boiling intermediate product is continued deep hydrogenation reaction or recycled to add Hydrogen reaction；Circulation plus hydrogen, the viscosity that can use overall liquid phase under low boiling point raw material components existence condition are greatly lowered, are high boiling The advantage that the diffusion velocity of point component is accelerated accelerates hydrogenation reaction, and high boiling hydrocarbon component plus hydrogen final products quality can be with It is controlled by realizations such as flexibly adjustment recycle ratio, reaction temperatures, in other words, is certainly existed at this time by heavy distillat unconverted oil Composition adds hydrogen recycle oil.The front conversion zone that these circulation heavy oil return to hydrogenation process is reacted, and consumption is corresponding Hydrogen supply dissolvent oil.
The normal boiling point of middle coalite tar is higher than the original that 350 DEG C or the double distilled higher than 450 DEG C or higher than 530 DEG C are grouped as Material hydrocarbon RU-F1 usually can not in use in the single hop one way heat from hydrogenation cracking reaction process RU of streaming expanded bed such as suspension bed It is able to achieve 100% full conversion, because excessively high heat from hydrogenation cracking conversion per pass will lead in raw material and intermediate hydrogenation products Low boiling hydrocarbon overcracking fecund gas, the more green coke charcoals of the excessive thermal condensation of high boiling hydrocarbon, severe exacerbation product distribution shorten continuously The cycle of operation, in other words, in order to utilize to greatest extent, feedstock oil, raising liquid yield improve, extension reaction process is continuously transported The row period usually certainly exists the overhydrocracking process of heavy distillat unconverted oil.These circulation heavy oil return to hydrogenation reaction The front conversion zone of process is reacted, and corresponding hydrogen supply dissolvent oil will be consumed.
In direct hydrogenation liquefaction of coal reaction process, liquid yield is improved in order to improve lique faction of coal rate, it is often desirable that coal Middle active component (vitrinite, chitin group) is bordering on whole liquefaction and inert component (inertinite) moderately liquefies, but because in coal Active component (vitrinite, chitin group) is easy to liquefy and inert component (inertinite) is difficult to liquefy, so, inert component (lazy matter Group) the liquefied rear portion conversion zone of appropriateness, be exactly the secondary pyrolysis reaction section of active component liquefaction products, necessarily raw material caused to supply The overcracking fecund gas of hydrogen agent and intermediate product hydrocarbon consumes hydrogen more, reduces liquid receipts, severe exacerbation product distribution, in other words It says, the nonideal depth that conventional gas-liquid parallel type direct hydrogenation liquefaction of coal hydrogenation process usually certainly exists a middle matter hydrocarbon adds Hydrogen cracking reaction process.
Under the premise of there are overhydrocracking reaction process, the raw material the hydrocarbon component of deep hydrogenation heat cracking reaction process Concentration (mid-boiling point hydrocarbon, high boiling hydrocarbon), directly it is strong influence hydrogenation reaction selectivity, the object reaction time, catalyst concn, Reactor volume etc., and then the secondary pyrolysis stoichiometric number amount of matter hydrocarbon in directly strong influence, decide the superiority and inferiority success or failure of technical process. And for hydrocarbon powder adds hydrogen direct liquefaction process, there is also be difficult to realize be prepared with hydrogen supply dissolvent to convey for the prior art Ultrahigh concentration powder starches technical problem, restricts the economy of process.
It is of the present invention to match defeated coal slurry agent coal ratio, refer to that coal slurry enters initial position (the usually coal slurry of high-pressure system Pump discharge position) when, possessed agent coal ratio is the index for measuring the efficiency of coal slurry preparation method, it is often desirable that agent Coal is than rationally reducing (i.e. coal agent is than rationally improving), to reduce solvent naphtha dosage.This solvent naphtha is referred to as solvent naphtha with slurry.
Direct hydrogenation liquefaction of coal reactant coal ratio of the present invention refers to that participate in reacting into reaction process comes from coal The overall conventional liq hydrocarbon of slurry solvent oil participates in the weight ratio of the coal dust reacted with reaction process is entered, and is that measurement coal hydrogenation is straight Connect the index of the solvent naphtha efficiency of liquefaction process, it is often desirable that reactant coal is reduced than rationally, is made to reduce reaction process Long circulating solvent naphtha dosage.This solvent naphtha is referred to as reaction dissolvent oil.
Direct hydrogenation liquefaction of coal of the present invention reacts liquid phase agent coal ratio, refers to that entering reaction process participates in depositing for reaction It is the weight for the coal dust that the overall conventional liq hydrocarbon from coal slurry solvent naphtha in liquid phase is reacted with into reaction process participation Ratio is the finger for measuring the core reaction i.e. solvent naphtha efficiency of liquid-phase hydrogenatin reaction process of direct hydrogenation liquefaction of coal technique Mark, it is often desirable that reactant coal is reduced than rationally, to reduce solvent naphtha dosage；Liquid phase agent coal ratio is reacted, there are lower limit values, are lower than The offline Value Operations, by mutability cause reaction condition to deteriorate, and will cause apparent heavy hydrocarbon such as asphaltene, preasphaltene Thermal condensation reaction, reduces the retortable oil yield of direct hydrogenation liquefaction of coal, shortens the operation cycle.It is anti-that this solvent naphtha is referred to as liquid phase Answer solvent naphtha.
In direct hydrogenation liquefaction of coal reaction process, since coal dust almost all is present in liquid phase, and coal slurry solvent naphtha is total It is partly to vaporize into gas phase, therefore, in direct hydrogenation liquefaction of coal reaction process, reacts liquid phase agent coal and be lower than than always Reactant coal ratio；Under conditions of other conditions are constant, the low boiling hydrocarbon in solvent naphtha is more, then reacts liquid phase agent coal ratio, anti- Answer agent coal bigger than the difference of the two, the cyclic process of overall hydrogen supply dissolvent oil it is lower for hydrogen efficiency, lead to solvent oil hydrogenation The scale for stablizing reaction system is higher, increases its investment and energy consumption.
Chinese Shenhua Erdos coal oil branch company possesses the unique a set of commercialized 1,000,000 tons/year of coals in the world and adds Hydrogen direct liquefaction device, the direct hydrogenation liquefaction of coal project include direct hydrogenation liquefaction of coal reaction process RU, hydrogen supply dissolvent oil Stabilized hydrogenation process, stabilized hydrogenation distillate plus hydrogen grading process, a document for recording this kind of data is shown in: 1. publishing name Claim: " coal direct liquefaction technique and engineering "；2. retrieval is encoded with books: ISBN coding: 9-78703-04308-23；3. compiling It writes: Wu Xiuzhang, Shu Geping, Li Kejian, Xie Shunmin；4. publishing house: Science Press.
Chinese Shenhua Erdos coal oil branch company possesses the unique a set of commercialized 1,000,000 tons/year of coals in the world and adds The agent coal weight ratio of hydrogen direct liquefaction device, coal slurry is about hydrogen supply dissolvent: coal dust=54.95: 45.05, the production of many years is real It tramples and shows under the operating conditions such as its efficient direct hydrogenation liquefaction of coal catalyst used, the coal of the agent coal weight ratio The quantity of hydrogen supply dissolvent in direct hydrogenation liquefaction of coal reaction process is sufficient, superfluous, because after long-cycle production is stopped work It was found that the deposit on distribution plate, liquid collecting cup, wall in reactor is not coking deposit but granular deposit.Also It is to say, the quantity for the hydrogen supply dissolvent oil which uses is more, and causes the reason that hydrogen supply dissolvent is superfluous or utilization rate is low, no It is the intrinsic demand because in direct hydrogenation liquefaction of coal reaction process, is actually primarily due to coal slurry with transmission process, heating Other restrictive requirements of process cause solvent naphtha or hydrogen supply agent dosage excessive.
Existing direct hydrogenation liquefaction of coal technique, including gas-liquid fair current (parallel type) reaction equation direct hydrogenation liquefaction of coal process With solvent oil hydrogenation stabilization process, wherein there is the long circulating circuit of hydrogen supply dissolvent oil, which originates in solvent naphtha coal blending Slurry, coal slurry pressurization, coal slurry heating, fully enter and it is whole by direct hydrogenation liquefaction of coal reaction process, to leave coal hydrogenation direct Liquefaction reaction process enters and whole process is fractionated to obtain solvent naphtha predecessor by direct hydrogenation liquefaction of coal product separation/fractional distillation process Object, solvent naphtha precursor by stabilized hydrogenation process complete aromatic hydrocarbons partial hydrogenation saturated reaction be converted into stabilized hydrogenation product, The fractional distillation process of stabilized hydrogenation product isolates hydrogen supply dissolvent recycling；In the overall process of direct hydrogenation liquefaction of coal device, packet Include solvent naphtha with coal slurry, coal slurry pressurization, coal slurry heating, fully enter and it is whole by direct hydrogenation liquefaction of coal reaction process, from It opens direct hydrogenation liquefaction of coal process and passes through liquefaction products separation/fractional distillation process into simultaneously whole, hydrogen supply dissolvent oil is actually complete Journey is with solvent.
Existing gas and liquid flowing reaction equation direct hydrogenation liquefaction of coal reaction process is reacted externally to direct hydrogenation liquefaction of coal Input coal dust (or being referred to as to carry coal dust) in device (is taken out of direct hydrogenation liquefaction of coal reactor to external transportation of liquefied product With liquefaction residual solid), say in the carrying of liquefaction products fractional distillation process liquefaction residual solid effect, by and large, followed using length Loop back path hydrogen supply dissolvent oil, pulverized coal conveying enter the solvent naphtha quantity with slurry that high-pressure system process uses, similarly enter reaction Process participates in the solvent naphtha quantity of reaction, is equal to the solvent naphtha quantity with slurry of liquefaction products, is equal to the fractionation of liquefaction products Process solvent oil quantity, is equal to the solvent naphtha precursor quantity of solvent oil hydrogenation stabilization process, and such hydrogen supply dissolvent oil is practical On be a kind of whole full dose with solvent；In this way, direct hydrogenation liquefaction of coal process, becomes under " whole full dose is with solvent " concept " coal slurry add hydrogen direct liquefaction process, solvent naphtha precursor fractional distillation process (direct hydrogenation liquefaction of coal generate oily fractional distillation process) and Solvent naphtha recycles stabilized hydrogenation process " anabolic process, and solvent internal circulating load is limited by defeated coal technique with slurry, in other words, The reactant coal ratio needed in such a chemical process of direct hydrogenation liquefaction of coal reaction process, by defeated coal such one with slurry With slurry dose of coal ratio in a physical process is restricted, as soon as this certainly contains the concept of partial error, optimum response agent For coal is than index, with slurry dose of coal than be not usually its intrinsic demand optimum value, and in fact, be an excessive value, it Excessive portion reduces the economy of direct hydrogenation liquefaction of coal process, and the operation control of agent coal ratio flexibility is very poor (cannot It rationally reduces).
Existing direct hydrogenation liquefaction of coal technique, that is, gas-liquid fair current reaction equation direct hydrogenation liquefaction of coal technique, why cannot Large-scale commercial is promoted, and an important factor is to increase engineering throwing using a large amount of long circulating circuit hydrogen supply dissolvent oil Money and operating cost, reduce the economy of technique, have and show as unavoidable defect as described below:
1., by direct hydrogenation liquefaction of coal reaction process, a large amount of non-targeted property will occur for excessive solvent naphtha with coal dust Liquid hydrocarbon is lost in thermal cracking negative reaction, reduces the liquid hydrocarbon yield of overall direct hydrogenation liquefaction of coal process；
2. since excessive solvent naphtha passes through direct hydrogenation liquefaction of coal reaction process with coal dust, in order to inhibit excessive hot tearing Changing reaction then necessarily leads to the reduction of direct hydrogenation liquefaction of coal conversion ratio；In order to guarantee rationally high direct hydrogenation liquefaction of coal conversion Rate, necessarily leads to the excessive thermal cracking of solvent naphtha, solvent naphtha iterative cycles as a result, recycled solvent oil quantity present in system Insufficient and boiling point tends to be lower, i.e., there are the tendencies that lazy weight, component lighten for recycled solvent oil, and external supply is needed when serious Answer solvent naphtha, such case long-term existence on commercial plant；
3. excessive solvent naphtha generates oil by direct hydrogenation liquefaction of coal reaction process, direct hydrogenation liquefaction of coal with coal dust Fractional distillation process, or stablize reaction process by carrying out the solvent oil hydrogenation of aromatic moiety saturated reaction simultaneously, significantly increase Course-scale, increases considerably system investments and energy consumption；
4. excessive solvent naphtha generates oil by direct hydrogenation liquefaction of coal reaction process, direct hydrogenation liquefaction of coal with coal dust Fractional distillation process, or stablize reaction process by carrying out the solvent oil hydrogenation of aromatic moiety saturated reaction simultaneously, significantly increase The emission hydrogen quantity of chemical hydrogen consumption, physical dissolution amounts of hydrogen and hydrogen upgrading process, increases considerably hydrogen Cost.
Experimental results demonstrate be suitable for the conventional raw material coal of direct hydrogenation liquefaction of coal, reached with direct hydrogenation liquefaction of coal rate 90% is target, in 20~40% initial reaction stage for adding hydrogen direct liquefaction reaction process total reaction time, that is, is completed Most of pyrolysis task of coal and corresponding free radical stablize task, and direct hydrogenation liquefaction of coal rate can generally achieve 50~ 75%；A document for recording this kind of data is shown in: 1. publication title: " coal direct liquefaction ", page 37~page 38；2. examining Rope is encoded with books: ISBN coding: 978-7-122-02151-9；3. writing: Wu Chunlai；4. publishing house: chemical industry is published Society.
Experimental results demonstrate be suitable for the conventional raw material coal of direct hydrogenation liquefaction of coal, reached with direct hydrogenation liquefaction of coal rate 90% is target, in 20~40% initial reaction stage for adding hydrogen direct liquefaction reaction process total reaction time, is usually consumed Fall the 40~60% of total consumption hydrogen, as the time of direct hydrogenation liquefaction of coal reaction process extends, the organic matter for the coal that can be pyrolyzed Quantity is fewer and fewer, thus coal be once pyrolyzed free radical fragment, bitumen pyrolysis free radical fragment concentration increasingly Low, the stable molecule of pyrolysis of coal fragment resistate conversion gained is more and more, and the substance that can serve as hydrogen supply dissolvent is more and more, this Sample, the hydrogen supply dissolvent quantity phase in the initial reaction stage with the 20~40% of direct hydrogenation liquefaction of coal reaction process total reaction time Than relatively rich remaining (being actually usually a large amount of more than needed) occurs in the hydrogen supply dissolvent quantity of later stage, in order to improve confession The utilization rate of hydrogen substance, can be by the solid concentration of direct hydrogenation liquefaction of coal reaction process RU far below charging coal slurry solid concentration Intermediate liquid product or final liquid product, used as upstream slurry diluent, for example provide certain with adverse current echo plex mode The part hydrogen supply dissolvent that road charging coal slurry needs during direct hydrogenation liquefaction of coal initial reaction, that is to say, that be a kind of reality The economic means of the direct hydrogenation liquefaction of coal initial reaction process of existing high concentration coal slurry, that is, thick coal slurry, such direct liquid of coal hydrogenation The effective feed process for changing the high concentration coal slurry of reaction process, will be with great economic value.In fact, using product liquid Strong loop reactor, is exactly a kind of effective secondary mode using solvent naphtha or hydrogen supply dissolvent oil, and the hydrogen supply that it is recycled is molten Agent oil is mainly the high boiling hydrocarbon component of difficult vaporization, and herein referred to as (more accurate saying is high boiling to the short circulation loop of solvent naphtha The point short circulation loop of heavy hydrocarbon), this is also a set of commercialized 1,000,000 tons of Chinese Shenhua Erdos coal oil branch company/ The method of operation of year direct hydrogenation liquefaction of coal device.
It is an object of the present invention to further decrease the hydrogen supply dissolvent oil number in long circulating circuit in prior art basis Amount.
It is below pair with 1,000,000 tons/year of direct hydrogenation liquefaction of coal device direct hydrogenation liquefaction of coal reaction process of Chinese Shenhua As analyzing the variation tendency of K300, K700 in the direct hydrogenation liquefaction of coal reaction mechanism mechanism of reaction.
Table 1 is the material of 1,000,000 tons/year of direct hydrogenation liquefaction of coal device direct hydrogenation liquefaction of coal reaction process of Chinese Shenhua Sort balance table, K300, K700 numerical statistic table.
If direct hydrogenation liquefaction of coal reaction process is divided into preceding conversion zone and rear conversion zone, and analyze hydrogen supply dissolvent oil, Retortable oil, asphalitine, the relative populations of non-liquefaction coal solid (including hydrocarbon component and the ash content of not liquefying) during the reaction Variation tendency, then, it can be seen that rear conversion zone outlet K300 is 6.7 times of preceding conversion zone entrance K300, rear conversion zone outlet K700 is 9.4 times of preceding conversion zone entrance K700, and therefore, with the process of reaction, violent variation is had occurred in K300, K700, Its main body trend is:
1. preceding conversion zone forms the concentrated solution of " coal dust+asphalitine " compared with rear conversion zone, solvent is mutually relatively scarce Weary；
2. rear conversion zone forms " coal dust+asphalitine " weak solution compared with preceding conversion zone, solvent is mutually a large amount of excess 's.
Therefore, under the conditions of feasible, try the K300 or K700 of conversion zone after reducing, will have the advantage that
1. reducing excessive solvent naphtha, it is possible to reduce the thermal cracking negative reaction of partial solvent oil reduces liquid hydrocarbon damage It loses, the liquid hydrocarbon yield of overall direct hydrogenation liquefaction of coal process in contrast can be improved；
Excessive solvent naphtha, in default of the hydrogen abstraction action of hydrogen-abstracting agent (hydrogen acceptor), leading thermal response will supply The aromatization of reactive hydrogen (lose activity hydrogen), but heat cracking reaction, can largely generate gas, and consume excess hydrogen；
2. guaranteeing rationally high direct hydrogenation liquefaction of coal conversion ratio due to the use for avoiding excessive response solvent naphtha Meanwhile reduce the excessive thermal cracking of solvent naphtha, cyclic process as a result, recycled solvent oil quantity present in system can become It is relatively sufficiently or even superfluous, and the mean boiling point of recycled solvent oil opposite can tend to get higher, i.e. recycled solvent oil forming quantity fills Point, the relatively high rational state of boiling range, do not need external supply solvent naphtha, in fact such case is on commercial plant Low coal conversion ratio operating condition be verified (reduce reaction temperature, reduce oil product hot tearing rate)；
3. direct hydrogenation liquefaction of coal can be greatly lowered and reacted due to the use for avoiding excessive response solvent naphtha Journey, solvent oil hydrogenation stablize the scale of reaction process, and the energy consumption of the system is accordingly greatly lowered；
4. coal hydrogen consumption can be greatly lowered due to the use for avoiding excessive response solvent naphtha；
5. superfluous solvent naphtha is reduced, so that the concentration for improving the concentration of asphalitine, improving catalyst, is conducive to improve Heat cracking reaction selectivity and reaction speed are conducive to improve operation temperature；
6. superfluous solvent naphtha is reduced, to be conducive to the reactor volume of conversion zone after reducing.
The material of the Chinese 1,000,000 tons/year of direct hydrogenation liquefaction of coal device direct hydrogenation liquefaction of coal reaction process of Shenhua of table 1 Sort balance table, K300, K700 numerical statistic table
Project Into/maf.wt% Entrance, to hydrogen supply dissolvent oil Out/maf.wt% Outlet, to solvent naphtha raw material
Gas 0 0 14.20 0.1420
Solvent 122.22 1.0000 0 0.0000
Oily (220 DEG C of <) 0 0.0000 24.09 0.1971
Oily (220 DEG C of >) 0 0.0000 28.54 0.2335
Solvent materials 0 0.0000 122.22 1.0000
H2O 0 0.0000 11.67 0.0955
538 DEG C or more fractions 0 0.0000 14.46 0.1183
H2 5.37 0.0439 0 0.0000
Moisture-and-ash-free basis coal 95.1 0.7781 8.35 0.0683
Ash 4.9 0.0401 4.9 0.0401
Catalyst-Fe 1 0.0082 1 0.0082
Catalyst-other 0.58 0.0047 0.22 0.0018
Sulphur 1.14 0.0093 0.66 0.0054
DMKDS 0 0.0000 0 0.0000
It is total 230.32 1.8845 230.32 1.8845
Retortable oil is total 1 1.4306
Asphalitine 0 0.1183
Solid 0.8404 0.1238
Maneuverability features value K300 1.282 8.45=1.282 × 6.7
Solution dilution characteristic value K700 1.282 12.09=1.282 × 9.4
In fact, in the mid-term of direct hydrogenation liquefaction of coal reaction process, there are " (a hydrogen supplies from hydrogen object concentration analysis is taken by force Solvent+retortable the oil of direct hydrogenation liquefaction of coal product)/(accessible area+asphalitine of liquefiable coal component solid phase it is accessible Area) " ratio it is minimum (take by force hydrogen object at most, dispersion it is most wide) reaction interval, that is, direct hydrogenation liquefaction of coal reaction process The opposite the smallest reaction interval of hydrogen supply capacity, it is presently believed that this is the bottleneck point that coal liquid adds hydrogen direct liquefaction reaction process.This Be because, in the mid-term of direct hydrogenation liquefaction of coal reaction process, about direct hydrogenation liquefaction of coal rate be 70~80% reaction rank Section, it is still solid that the coal of part coal such as 20~30%, which not yet liquefies i.e., gas recovery ratio about 10~15%, direct hydrogenation liquefaction of coal Product be largely macromolecule bitumen such as yield be 40~45%, and retortable liquefaction oil yield very it is low such as Only 20~25%, and conventional boiling range be 230~280 DEG C low boiling point in matter hydro carbons yield it is very low be such as usually the 5 of coal dust ~8%；Before the mid-term, non-liquefaction coal ratio is higher, but the external surface area of the coal dust as a large amount of molecular aggregates is (i.e. With the contact area of hydrogen supply dissolvent molecule) it is (i.e. molten with hydrogen supply much smaller than the external surface area of direct hydrogenation liquefaction of coal product asphalitine The contact area of agent molecule), therefore the hydrogen abstraction reaction before mid-term is relatively fewer；After the mid-term, direct hydrogenation liquefaction of coal The speed and product amounts for generating asphalitine, the speed and product amounts of retortable oil are converted into far fewer than asphalitine, in coal plus Under hydrogen direct liquefaction catalyst action, more retortable oil conversions are for hydrogen supply agent, and as reaction depth is deepened, K700 can add Speed becomes larger, therefore the relatively rapid reduction of the hydrogen abstraction reaction after mid-term.
Herein, the fresh hydrogen supply dissolvent for direct hydrogenation liquefaction of coal reaction process being added is referred to as long circulating hydrogen supply dissolvent Or rich reactive hydrogen solvent, leave the boiling point highest of direct hydrogenation liquefaction of coal reaction process, residence time longest hydrogen supply dissolvent turns Compound is referred to as poor reactive hydrogen solvent.
In following analysis direct hydrogenation liquefaction of coal reaction process, the heating power scholarship and moral conduct of different boiling ranges different phase solvent oil ingredient To analyze its remaining hydrogen supply capacity for leaving direct hydrogenation liquefaction of coal reaction process, and then propose half way hydrogen supply dissolvent concept, leading to Recycling half way hydrogen supply dissolvent is crossed, makes it in the abundant hydrogen supply of direct hydrogenation liquefaction of coal reaction process.
Existing direct hydrogenation liquefaction of coal reaction process, the solvent naphtha used are the hydrocarbon that conventional boiling range is 200~530 DEG C Class, host component therein are that conventional boiling range is 230~400 DEG C of hydro carbons, can be greatly classified into conventional boiling range be 200~ The heavy hydrocarbon that 230 DEG C of light hydrocarbons, 230~400 DEG C of middle matter hydro carbons, conventional boiling range are 400~530 DEG C；According to them Phase-state change trend in direct hydrogenation liquefaction of coal reaction process, is analyzed as follows:
1. the heavy hydrocarbon that conventional boiling range is 400~530 DEG C, usual gas-liquid distribution is smaller to be such as lower than 0.1~0.5, It is the basic liquid phase component and optimal liquid phase component of direct hydrogenation liquefaction of coal process；
The major part of these components is usually discharged from the outlet of last reactor, molten from hydrogen supply in liquid phase The hydrocarbon component of agent oil has turned to poor reactive hydrogen solvent；
2. matter hydro carbons in the higher boiling that conventional boiling range is 280~400 DEG C, reaction process can be vaporized partially in the early stage, grasping Making the high late phase reaction process of temperature can largely vaporize, usual gas-liquid distribution ratio near 1 such as between 0.5~2.0, It is the important liquid phase component of direct hydrogenation liquefaction of coal process, is the excellent solvent naphtha of hydrogen supply function；
In these components, residence time of the matter hydro carbons in reactor in unboiled higher boiling is 400 with conventional boiling range ~530 DEG C of heavy hydrocarbon is almost the same, is usually discharged from the outlet of last reactor, molten from hydrogen supply in liquid phase The hydrocarbon component of agent oil has turned to poor reactive hydrogen solvent；
In these components, vaporization enters matter hydro carbons in the higher boiling of gas phase during the reaction, with gas phase quickly through anti- Answer device；First, its residence time in reactor is shorter than the residence time for the heavy hydrocarbon that conventional boiling range is 400~530 DEG C； Second, due in gas phase the distance between molecule much larger than distance between molecule in liquid phase, heat fortune occurs for molecule in gas phase The probability of warm-up movement collision occurs far below molecule in liquid phase for the probability of dynamic collision；Third, other molecules present in gas phase Average molecular weight collides and the probability of chemical reaction is caused to be far below much smaller than the average molecular weight of remaining molecule present in liquid phase Collision in liquid phase causes the probability of chemical reaction；Fourth, the molecular concentration of hydrogen-abstracting agent present in gas phase is much smaller than in liquid phase The molecular concentration of existing hydrogen-abstracting agent, the probability that collision hydrogen-abstracting agent causes hydrogen supply to react cause chemistry far below the collision in liquid phase The probability of reaction；
In short, matter hydro carbons retains its intrinsic category in the higher boiling in gas phase compared with matter hydro carbons in the higher boiling in liquid phase Property ability it is much better than, therefore, usually from last reactor outlet discharge these higher boilings vaporized in matter Hydro carbons, these the hydrocarbon components from hydrogen supply dissolvent oil not yet have turned to poor reactive hydrogen solvent completely, still have centainly Remaining hydrogen supply capacity；
3. matter hydro carbons in the low boiling point that conventional boiling range is 230~280 DEG C, in direct hydrogenation liquefaction of coal process, in the early stage instead It answers process that can partially vaporize, can largely be vaporized in the high late phase reaction process of operation temperature, usual gas-liquid distribution ratio is near 4 Such as between 2~6；Therefore, matter hydro carbons in the low boiling point that conventional boiling range is 230~280 DEG C, is that the conveying with slurry of coal dust is molten Agent component, still, it is simultaneously not all reaction process liquid phase component；
But conventional boiling range is the hydrogen supply dissolvent of matter hydro carbons in 230~280 DEG C of low boiling point, usually twin nuclei The aromatic hydrocarbons of fractional saturation such as naphthane or tetrahydro naphthalene series substance are to carry the high rationality hydrogen supply dissolvent component used by emphasis of hydrogen amount；
Based on Such analysis, matter hydro carbons is withed a hook at the end the ability of its build-in attribute in the low boiling point in gas phase, therefore, usually from Matter hydro carbons in these low boiling points vaporized of the outlet discharge of last reactor, these hydrocarbon from hydrogen supply dissolvent oil Component still retains considerable degree of remaining hydrogen supply capacity, herein referred to as half way hydrogen supply dissolvent；
Particularly, in the direct hydrogenation liquefaction of coal reaction process using 2 or multiple conversion zones, when using hydrogen cocurrent Or when counter-current modes of operation, the first conversion zone of direct hydrogenation liquefaction of coal reaction process will be expelled directly out leading portion gas-phase product, this Matter hydro carbons (and hydro carbons of higher boiling point) in low boiling point before kind in the gas-phase product of conversion zone, still retains considerable degree of confession Hydrogen Energy power, herein referred to as half way hydrogen supply dissolvent；
4. the light hydrocarbons that conventional boiling range is 200~230 DEG C, in direct hydrogenation liquefaction of coal process, reaction process in the early stage It can largely vaporize, higher in the meeting almost all vaporization of interim response process in operation temperature, usual gas-liquid distribution ratio is greater than 6；Therefore, the light hydrocarbons that conventional boiling range is 200~230 DEG C, are the conveying solvent compositions with slurry of coal dust, still, it is not anti- Process liquid phase component is answered, therefore, there is no need to it with good hydrogen supply capacity.
As seen from the above analysis, the low boiling point in solvent naphtha that existing direct hydrogenation liquefaction of coal reaction process uses The hydro carbons that the such as conventional boiling range of hydrocarbon is 200~230 DEG C, should not need to protect by direct hydrogenation liquefaction of coal reaction process It is stayed to match the function of defeated coal dust；For not passing through the solvent oil ingredient of direct hydrogenation liquefaction of coal reaction process, do not need to make With hydrogen supply dissolvent with high costs.
The low boiling that conventional boiling range in the gas-phase product of existing direct hydrogenation liquefaction of coal reaction process is 230~280 DEG C Matter hydro carbons in point, it is mainly made of the conversion product based on hydrogen supply dissolvent oil, this is because common direct hydrogenation liquefaction of coal is anti- The ratio i.e. agent coal ratio of the hydrogen supply dissolvent oil weight and coal dust weight of answering process is 1.5~2.0 times, and the direct liquid of Shenhua coal hydrogenation Disguising the agent coal ratio set for 1.22 is very advanced level, wherein 230~280 DEG C of fraction section ratios are 20~25%；And coal Adding the retortable oil yield in hydrogen direct liquefaction reaction product is the 50~60% of coal dust, wherein 230~280 DEG C of fraction section ratios Be 30~35%, in this way, in direct hydrogenation liquefaction of coal reaction product 230~280 DEG C of fraction sections yield be coal dust 15~ 21%；In this way, the conventional boiling range in the final overall gas-phase product of direct hydrogenation liquefaction of coal reaction process is 230~280 DEG C Low boiling point in matter hydro carbons, the conversion product of hydrogen supply dissolvent also occupies 50~70% ratio.
Particularly, in the direct hydrogenation liquefaction of coal reaction process using 2 or multiple conversion zones, when using hydrogen cocurrent Or when counter-current modes of operation, the first conversion zone of direct hydrogenation liquefaction of coal process will be expelled directly out leading portion gas-phase product, before this The middle matter hydro carbons (and hydro carbons of higher boiling point) that conventional boiling range in the gas-phase product of conversion zone is 230~400 DEG C, hydrogen supply is molten The ratio of the conversion product of agent will be higher, even higher up to 75~90%, and retain the hydrogen supply capacity of almost about half, be Qualified half way hydrogen supply dissolvent；This is because in direct hydrogenation liquefaction of coal first half term reaction process, its usual reactor body Product is only the 30~60% of general reaction body product, and the liquefaction reaction time of coal dust is only the 30~60% of the general reaction time, In direct hydrogenation liquefaction of coal first half term reaction product, it is still solid that the coal of part coal such as 20~30%, which not yet liquefies i.e., gas Body yield about 10~15%, direct hydrogenation liquefaction of coal object be largely macromolecule bitumen such as yield be 40~ 45%, it is such as only 20~25% that retortable liquefaction oil yield is very low, wherein in the low boiling point that conventional boiling range is 230~280 DEG C It is such as usually the 5~8% of coal dust that matter hydro carbons yield is very low；In view of the hydrogen supply of common direct hydrogenation liquefaction of coal reaction process Ratio, that is, agent coal ratio of solvent naphtha quantity weight and coal dust weight is 1.0~2.0 times, wherein 200~280 DEG C of fraction section ratios are 20~25%；It is obvious that in the leading portion gas-phase product that direct hydrogenation liquefaction of coal first half term reaction process is expelled directly out, it is therein normal It advises in the low boiling point that boiling range is 230~280 DEG C in matter hydro carbons, the conversion product of hydrogen supply dissolvent occupies 75~90% share.Analysis In the middle matter hydro carbons for showing conventional 280~400 DEG C of boiling range therein, the conversion product of hydrogen supply dissolvent occupies 50~70% share.
As seen from the above analysis, gas-phase product (the especially first half of existing direct hydrogenation liquefaction of coal reaction process The gas-phase product of journey reaction process) in conventional boiling range be 230~280 DEG C low boiling point in matter hydro carbons, conventional boiling range be 280~ The hydro carbons that matter hydro carbons and its conventional boiling range are 350~500 DEG C in 350 DEG C of higher boiling, especially conventional boiling range is 230~400 DEG C middle matter hydro carbons, be mainly made of the half way conversion product of hydrogen supply dissolvent, there is certain residual hydrogen supply capacity, be that a kind of half way supplies Hydrogen solvent can give full play to this remaining hydrogen supply capacity by way of recycling, and then reduce long circulating circuit hydrogen supply Amount of solvents, to improve the economy of process.
Half way hydrogen supply dissolvent cycles through front conversion zone, increases the middle matter hydrogen supply dissolvent total amount in the conversion zone of front, Based on the effect for the rule that balances each other, and then the quantity of middle matter hydrogen supply dissolvent in the liquid phase is increased, to give full play to its hydrogen supply The agent coal ratio of leading portion reaction process can be improved in ability, perhaps allows to process more coal dusts or allows to reduce long circulating confession Hydrogen solvent naphtha ratio.
So far, it has been found by the present inventors that in the direct hydrogenation liquefaction of coal reaction process, " half way hydrogen supply is recycled Solvent improves reaction liquid phase agent coal ratio or reduces long circulating hydrogen supply dissolvent ratio, especially improves the reaction liquid phase of front conversion zone Agent coal ratio or the long circulating hydrogen supply dissolvent ratio for reducing front conversion zone " has major economic value, and the direct liquid of existing coal hydrogenation There is not this concept in change technology, thus also without proposing corresponding Utilization plan.The present inventor is exactly in clear " half way confession While this concept of hydrogen solvent ", the present invention is proposed.In order to make full use of the hydrogen supply capacity of " half way hydrogen supply dissolvent ", propose The present invention is a natural event.Essence of the invention is, by human intervention (establishing intermediate range circulation), matter in increase Hot hydrogen supply reaction times of the hydrogen supply agent component in direct hydrogenation liquefaction of coal reaction process, are supplying that it with heavy hydrogen supply agent component Thermal response number during hydrogen is close, to improve for hydrogen efficiency, substantially can with reaction time or cycle-index come Characterization；It formally sees, the present invention is classified management to the circulating path of the hydrogen supply dissolvent of different boiling ranges, to improve Hydrogen supply dissolvent service efficiency can reduce long circulating circuit hydrogen supply dissolvent dosage, or can reduce the heavy hydrogen supply agent reaction time Reduce its cracking rate.
For the direct hydrogenation liquefaction of coal reaction process containing at least two conversion zone, the liquid material proposed using the present inventor The reactive mode that series connection, hydrogen are operated across flow short-circuit, can more retain the hydrogen supply capacity of matter solvent hydrocarbon in low boiling point, thus Cycle-index can be increased.
For the direct hydrogenation liquefaction of coal reaction process containing at least two conversion zone, the liquid material proposed using the present inventor The reactive mode of series connection, hydrogen parallel operation, or the liquid material proposed using the present inventor are connected, have hydrogen counter-current operation step Reactive mode, it is necessary to use the thermal high separator tank system of direct hydrogenation liquefaction of coal initial reaction product, hot high score gas washing Dedirt system, compression system of Returning reacting system of thermal high knockout drum liquid phase etc., in this way, implementing the present invention, " hydrocarbon material is shallow The stabilized hydrogenation object reuse method of middle matter hydrocarbon in degree heat from hydrogenation cracked gas product " hardly increases new system, therefore this hair Bright appearance has become certainty, and being applied in combination for two kinds of technique forms the higher direct hydrogenation liquefaction of coal reaction of integrated level Process.
In fact, the present inventor is exactly in proposition " the direct hydrogenation liquefaction of coal reaction side of hydrogen counter-current operation between conversion zone While method ", the present invention is proposed；Using direct hydrogenation liquefaction of coal reaction process RU of the invention, in conveying equivalent coal dust item About 20~35% that the hydrogen supply dissolvent amount in systemic circulation circuit can be reduced under part are even more, using equivalent systemic circulation in other words The coal dust about 20~35% that can more liquefy under conditions of the hydrogen supply dissolvent amount in circuit is even more, thus significantly lifting process mistake The economic benefit of journey.
Basic imagination of the invention is: the stabilized hydrogenation object of middle matter hydrocarbon returns in hydrocarbon material either shallow heat from hydrogenation cracked gas product With method, add suitable for using the direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation reaction process, kerosene of hydrogen supply dissolvent to refine altogether The stabilized hydrogenation of middle matter hydrocarbon in the gas phase RUA-HS-V of the reaction product RUA-P of the preceding conversion zone RUA of hydrogen reaction process converts Object is recycled to RUA reuse, forms two stage process i.e. " hydrogen supply obtained by the stabilized hydrogenation product of catalysis reaction intermediate gas phase product Hydrocarbon is recycled and/or is recycled with defeated target feedstock hydrocarbon ", the stripping step containing liquid product of settable RUA increases by half Journey hydrogen supply dissolvent internal circulating load can give full play to the hydrogen supply capacity of half way hydrogen supply dissolvent in gas phase RUA-HS-V or reduce secondary hot tearing Change the reaction time or reduce long circulating circuit hydrogen supply dissolvent dosage or reduce the heavy hydrogen supply dissolvent reaction time, confession is greatly lowered Hydrogen solvent cycle cost improves process economy.
Half way hydrogen supply dissolvent circulation loop of the present invention can be applied to appointing for direct hydrogenation liquefaction of coal reaction process The meaning stage；But since the second half of direct hydrogenation liquefaction of coal reaction process solvent naphtha quantity itself is superfluous, the present invention, It is preferably applied to the first half term of direct hydrogenation liquefaction of coal reaction process, coal can also be entered in this way to avoid fraction solvent naphtha in these Add the second half of hydrogen direct liquefaction reaction process that excessive negative reaction occurs and reduces process efficiency.
The stabilized hydrogenation object reuse method of middle matter hydrocarbon, is deposited in hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention And be effectively using the basic reason of half way hydrogen supply dissolvent oil: in the front conversion zone of hydrocarbon material hydrogenation process RU In RUA, the residence time of the component KC in liquid phase is longer than with the residence time of component KC in gas phase, and the component KC in liquid phase with Collision frequency, the response frequency of hydrogen-abstracting agent are much larger than collision frequency, response frequency in gas phase with component KC, and therefore, gas phase produces In contrast hydrogen supply dissolvent oil in object maintains more hydrogen supply capacity, therefore herein referred to as half way hydrogen supply dissolvent oil or half way Hydrogen supply dissolvent.Key of the invention is to propose the control concept of the thermal response number of effective hydrogen supply process of hydrogen supply dissolvent, It can substantially be characterized with reaction time.
The invention is particularly suited to the front conversion zones for the reaction system that 2 or multiple conversion zones form, because front is anti- The liquid material that the number for the thermal response for answering the hydrogen supply dissolvent component in section gas-phase product to undergo is discharged far fewer than the last one reactor In hydrogen supply dissolvent component experience thermal response number, in general, maintain most of hydrogen supply capacity, only repeatedly circulation makes With the number of the thermal response of the hydrogen supply dissolvent component experience in the liquid material that could be discharged with the last one reactor is close, i.e., in fact The relative equilibrium of existing thermal response number, to reach near-sighted homogeneity, the synchronism of the reaction mechanism mechanism of reaction, such heavy hydrogen supply dissolvent turns Compound, middle matter hydrogen supply dissolvent conversion product are synchronous to add hydrogen saturation by stabilized hydrogenation reaction process realization part aromatic ring, turns again Hydrogen supply dissolvent recycling is turned to, the internal circulating load of half way hydrogen supply dissolvent can be reduced, solvent oil hydrogenation is reduced and stablizes reaction process Scale, thus reduce investment, reduce energy consumption, reduce hydrogen consumption, reduce solvent naphtha pyrolysis rate etc.；On the other hand, in hot high score oil Solvent precursor is recycled, stablizes the raw material of reaction process as the solvent oil hydrogenation for the beaded catalyst for using multi-pore channel, it is necessary to Purify the solid particles such as semicoke, catalyst as much as possible, in fractional distillation process must by evaporation process could with solid particle, Asphalitine is separated from each other, this is the separation process of a highly energy-consuming, and the fractional distillation process of middle matter hydrocarbon and heavy hydrocarbon also consumes thermal energy； And it is of the invention, using the high temperature of direct hydrogenation liquefaction of coal reaction process, the air lift evaporation conditions of a large amount of hydrogen, realize circulation half Journey solvent is separated from each other with solid particle, asphalitine, it is only necessary to which removing such as conventional boiling range of light component is 200 DEG C or lower than 230 DEG C Hydro carbons, can be used as coal slurry solvent naphtha use, do not need neatly to remove solid, therefore, coal can be greatly lowered and add Hydrogen direct liquefaction generates the investment and energy consumption of the separation process of oil；The present invention is for using the coal and/or again of mid-boiling point hydrogen supply dissolvent The hydrogenation process of oil, all has similar effect.
It is said from the angle of defeated coal slurry, the present invention can increase small amount using centrifugal protected type and be pressurized in a high voltage state Amplitude realizes that half way hydrogen supply dissolvent returns to front conversion zone RUA, thus providing using empty with coal slurry technology for ultrahigh concentration Between, because the force (forcing) pump technology of ultrahigh concentration coal slurry has succeeded, after the pressurized pump input high-pressure system of ultrahigh concentration coal slurry, i.e., The coal slurry of normal concentration can be mixed into half way hydrogen supply dissolvent circulation fluid immediately, it is molten that long circulating hydrogen supply can be greatly lowered in this way Agent oil dosage reduces the energy consumption of coal slurry pressure process, reduces the quantity of expensive coal slurry booster pump, reduces investment.
The fractional distillation process that direct hydrogenation liquefaction of coal generates oil is high-temperature operation step, and there are the high-temperature operations of long residence time Process and with the direct hydrogenation liquefaction of coal of scarce hydrogen generate oil coexist, it is intended to so that half way hydrogen supply dissolvent component loses for Hydrogen Energy Power；The second half of direct hydrogenation liquefaction of coal reaction process, under the conditions of excessive solvent oil is existing, due to lacking hydrogen-abstracting agent, mistake It measures solvent naphtha to react the stabilized hydrogenation that the high consumption hydrogen of heat cracking reaction and hot cracked product free radical occurs, for example generates a large amount of The high conventional gas hydrocarbon of hydrogen content so that half way hydrogen supply dissolvent component lose hydrogen supply capacity and be converted into small molecule reduce circulation it is molten Dosage reduces the liquefaction oil yield of overall craft process；Therefore, make the half way hydrogen supply dissolvent of the condition of high temperature by the short time Turn the front reaction zone of return direct hydrogenation liquefaction of coal reaction process, or makes the half way hydrogen supply dissolvent of the condition of high temperature by short-term Between rapid cooling cooling keep its hydrogen supply capacity as coal blending slurry solvent oil repeat or be repeated several times pass through the direct liquid of coal hydrogenation The front reaction zone for changing reaction process, is ideal operation mode.
For direct hydrogenation liquefaction of coal reaction process, it is straight to be commonly referred to as last coal hydrogenation for front reaction zone The reaction zone that upstream direct hydrogenation liquefaction of coal reactor before connecing liquefying reactor is constituted, it can be liquid material serial operation First conversion zone RU1 of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones composition, he can be the more of liquid material serial operation The first conversion zone and/or the second conversion zone of the direct hydrogenation liquefaction of coal reaction process of a conversion zone composition, in general, slurries raw material In front, the reaction time of reaction zone accounts for slurries raw material and stops in the general reaction of whole direct hydrogenation liquefaction of coal reaction process Stay the 30~65% of time.
Middle matter hydrocarbon in condensation reuse gas-phase product of the present invention, cyclic process increase the mechanism of reaction zone amount of liquid phase Be: in reactor, circulation half way hydrogen supply dissolvent oil is partially gaseous state, is partially liquid, thus can form certain liquid gas Distribution ratio；Meanwhile its purity, Cycle Component and needs are improved in order to improve the selectivity of half way hydrogen supply dissolvent oil circulation process What it is into deep reaction process is usually that high boiling target components (such as non-liquefaction coal, gum asphalt) need that there are boiling points Difference, therefore, one word of matter hydrocarbon describes the hydrocarbon component that recycle hydrocarbons MKDS there must be in present invention selection, and middle matter hydrocarbon is generally also to follow The main body the hydrocarbon component of ring material, still, this cannot be understood to be to limit the hydrocarbon component source of cycle stock, in actual condition The hydrocarbon component situation of cycle stock is random, but necessarily comprising middle matter hydrocarbon and usual host component is middle matter hydrocarbon.
Half way hydrogen supply dissolvent oil proposed by the present invention, different from the fresh hydrogen supply dissolvent oil in long circulating circuit, because length is followed The one cycle process of the disengaging direct hydrogenation liquefaction of coal reaction process of the fresh hydrogen supply dissolvent oil of loop back path must pass through liquefaction Generate the fractional distillation process of oil, the fractional distillation process that solvent oil hydrogenation stablizes reaction process, solvent naphtha generation is oily, which leads to unit The production system investment of the hydrogen supply dissolvent oil of weight is big, energy consumption is high；Half way hydrogen supply dissolvent oil proposed by the present invention, also different from normal The middle oil for advising the discharge of direct hydrogenation liquefaction of coal reaction product fractional distillation process, because of the system complex of the separation process of the latter, energy consumption It is larger, and hydrogen content is low, lacks hydrogen supply capacity, has been polluted by the hydrocarbon component of the low hydrogen supply capacity of same boiling range.
According to the needs of the hydrogen supply capacity of half way hydrogen supply dissolvent oil and technical process, the circulation time of half way hydrogen supply dissolvent oil Number: can be with 1 time or 2 times or multiple, usually 1~3 time, generally 1~2 time.
It, can according to the requirement of the loop number of half way hydrogen supply dissolvent oil and to the control target of rear portion reaction zone feeds boiling range It can need using gas stripping gas, the half way hydrogen supply dissolvent oil and gas in the reaction zone liquid product of front to gas phase is participated in into half way hydrogen supply The intermediate range of solvent recycles；Gas stripping gas can be hot hydrogen-rich stream, can be circulating hydrogen, can be the secondary richness used Hydrogen gas stream.
Mechanism using the appropriate air lift half way hydrogen supply dissolvent of gas stripping gas is: direct hydrogenation liquefaction of coal reaction process is hydrogen consumption Huge reaction process, it is especially bigger in the hydrogen consumption of front conversion zone unit reaction compartment, therefore, in the process of reaction In, hydrogen is quickly gradually consumed, and simultaneously, the part hydrogen supply dissolvent component being present in gas phase, gradually liquefaction enters liquid Xiang Zhong, but its reaction mechanism mechanism of reaction is different from unvaporized high boiling component, says from thermal response number or thermal response time measuring angle, It is a kind of component close to half way hydrogen supply dissolvent, these liquefied hydrogen supply dissolvent or hydrogen supply dissolvent conversion products after first vaporizing are The candidate part of potential half way hydrogen supply dissolvent, also exactly using suitable quantity gas stripping gas can the half way hydrogen supply that uses of air lift it is molten Agent.
In order to improve efficiency of the invention, hydrogen air lift process can be applied in combination, improve in reaction product in higher boiling The vaporization rate of matter hydro carbons, and then circular flow is improved, the gas procedure is varied, it can be any one effective means, until It is few following several:
1. being mixed with gas stripping gas with the gas-liquid mixed phase product of front reaction zone, the method by increasing gas phase amount improves liquid phase The vaporization rate of middle half way hydrogen supply dissolvent oil；
2. being contacted with gas stripping gas with the product slurry of front reaction zone, air lift vaporizes half way hydrogen supply dissolvent oil；
3. 2 order reaction processes are divided into front reaction, gaseous product is discharged in each order of reaction, with increase gas phase amount The half way hydrogen supply dissolvent oil of differential responses course in method substep vaporization liquid phase, at the same can be improved reaction process liquid containing rate and Or reduce foreign gas concentration (improving density of hydrogen).
It is molten by circulation half way hydrogen supply under conditions of other conditions are constant for direct hydrogenation liquefaction of coal reaction process Agent oil, can be improved the liquid phase solvent oil quantity of front reaction zone, rear portion reaction zone, reduce the concentration of solid such as ash content, improve The mobility of slurries；Meanwhile using hydrogen cocurrent or countercurrent process, reaction system can be discharged in the foreign gas of upstream reaction zone Without entering downstream reaction area, hydrocarbon ils vaporization rate is reduced so as to which the hydrogen usage in downstream reaction area is greatly lowered With the concentration for increasing substantially amount of liquid phase, reducing solid such as ash content, therefore, the present invention is also a kind of high ash direct hydrogenation liquefaction of coal The effective ways of reaction.
It is direct to can be used as coal blending slurry solvent oil completion disengaging coal hydrogenation for the cyclic process of half way hydrogen supply dissolvent oil of the present invention The step of liquefaction reaction process, therefore, the present invention are also a kind of special coal slurry configuration and conveying side of economical advantage Method.
Under conditions of using gas stripping gas, the middle matter hydrocarbon vaporization in the temperature of high temperature slurry reaction product of front reaction zone enters gas In body, while part reaction heat being brought into gas phase, these air lift boil-offs, has released carrying in condensation cooling procedure Heat is simultaneously effectively recycled, and then half way hydrogen supply dissolvent oil cycle stock returns to direct hydrogenation liquefaction of coal front in the form of liquid material Reaction system, absorbing reaction heat heats up again in the reaction system of front and part vaporizes, therefore collects half way hydrogen supply dissolvent oil The process of cycle stock is also the removal process of reaction heat, and half way hydrogen supply dissolvent oil cycle stock plays the efficient carrying of reaction heat The effect of agent, therefore, the present invention are also a kind of method of efficient transfer reaction heat, are suitable for strongly exothermic direct hydrogenation liquefaction of coal Reaction process, for example hydrogen consumes high direct hydrogenation liquefaction of coal reaction process, dense coal slurry adds hydrogen direct liquefaction reaction process etc..
The hydrogen supply of " half way hydrogen supply dissolvent " is recycled in the preceding conversion zone of direct hydrogenation liquefaction of coal reaction process by the present invention Ability, at least have the characteristics that following advantage or:
1. in the low boiling point improved matter solvent naphtha for hydrogen efficiency, reduce systemic circulation circuit hydrogen supply dissolvent oil quantity, The scale of the stable reaction process of direct hydrogenation liquefaction of coal reaction process, solvent oil hydrogenation can be greatly lowered, accordingly significantly Reduce investment and the operating cost of the system；
2. in the low boiling point improved matter solvent naphtha for hydrogen efficiency, using the systemic circulation circuit hydrogen supply dissolvent oil of equivalent, More raw material coal dusts can be processed；
3. reducing matter solvent naphtha quantity in the low boiling point of rear conversion zone flowing, it is possible to reduce the hot tearing of partial solvent oil Change negative reaction, reduces liquid hydrocarbon loss, the liquid hydrocarbon yield of overall direct hydrogenation liquefaction of coal process in contrast can be improved；
Compared with rear conversion zone, preceding conversion zone is that " coal dust and asphalitine " overall hydrogen-abstracting agent concentration is high, operation temperature is lower Place, for the hot thermodynamic behavior of hydrogen supply based on the constant hydrogen supply aromatization of molecule carbon number, it is negative anti-that thermal cracking produces gas Should be largely suppressed, therefore, it is possible to reduce the thermal cracking negative reaction of partial solvent oil reduces liquid hydrocarbon loss, it is opposite and The liquid hydrocarbon yield of overall direct hydrogenation liquefaction of coal process can be improved in speech；
4. guaranteeing the rationally high direct liquid of coal hydrogenation due to the thermal cracking negative reaction for inhibiting matter solvent naphtha in low boiling point While changing conversion ratio, reduce the excessive thermal cracking of solvent naphtha, cyclic process as a result, recycled solvent oil present in system Quantity can become relatively sufficiently or even superfluous, and the mean boiling point of recycled solvent oil opposite can tend to get higher, i.e. recycled solvent oil The rational state that forming quantity is abundant, boiling range is relatively high does not need external supply solvent naphtha, and in fact such case exists Low coal conversion ratio operating condition on commercial plant is verified and (reduces reaction temperature, reduces oil product hot tearing rate)；
5. when due to reducing the heat cracking reaction of matter solvent naphtha in low boiling point in direct hydrogenation liquefaction of coal reaction process Between, reduce systemic circulation circuit hydrogen supply dissolvent oil quantity, direct hydrogenation liquefaction of coal reaction process, solvent naphtha can be greatly lowered The hydrogeneous destiny of emission of the chemical hydrogen consumption of stabilized hydrogenation reaction process, physical dissolution amounts of hydrogen and hydrogen upgrading process Amount, is greatly lowered hydrogen cost；
6. needing to expand first half term reaction compartment volume, it is equivalent to the reaction volume the second half reaction process, is transferred to First half term reaction process uses, to improve general reaction device efficiency；
7. the hydrogen supply capacity of middle matter hydrogen supply dissolvent can be given full play to, the reduction heavy hydrogen supply agent reaction time reduces its cracking Rate.
The present invention " the stabilized hydrogenation object reuse side of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product is applied in combination Method " and " the direct hydrogenation liquefaction of coal reaction method of hydrogen counter-current operation between conversion zone ", the direct hydrogenation liquefaction of coal collection constituted There is inundatory technology economy advantage to existing direct hydrogenation liquefaction of coal technique at technique, the present inventor is referred to as the 4th For direct hydrogenation liquefaction of coal technique.
Essentially, present invention finds the presence of half way hydrogen supply dissolvent and it is recycled, it is suitable corrects for traditional gas-liquid The part for including in " whole full dose is with solvent " this concept that stream (cocurrent) formula direct hydrogenation liquefaction of coal reaction method is formed Mistake, and then a kind of method for reducing long circulating circuit hydrogen supply dissolvent amount, therefore, commercial value of the invention are proposed naturally It is huge, occur being inevitable, one piece of cornerstone of forth generation direct hydrogenation liquefaction of coal technique can be referred to as.
It is direct with 1,000,000 tons/year of oil-producing of 1,000,000 tons/year of coal hydrogenations of Chinese Shenhua Erdos coal oil branch company For liquefying plant, if reducing by 20~25% long circulating circuit solvent naphtha dosage, it is replaced with half way hydrogen supply agent, passes through coal Add the first half term of hydrogen direct liquefaction reaction process, then can significantly reduce liquefaction products fractionating system, solvent oil hydrogenation stablizes reaction The scale of system, solvent oil hydrogenation fractionating system reduces construction investment and operating cost；In other words, in long circulating circuit hydrogen supply Under conditions of solvent naphtha quantity is constant, i.e., the liquefaction products fractionating system of same size, solvent oil hydrogenation stablize reaction system, It, can be with the feed coal of multi-processing 20~25%, it can it is molten to increase substantially hydrogen supply under conditions of solvent oil hydrogenation fractionating system Agent oil efficiency；Meanwhile because the circulation loop of half way hydrogen supply dissolvent is circulate operation, the flexibility of operation is huge.
The endless form of recycle hydrocarbons MR-KRDS is unrestricted, and there are many concrete mode, at least following several method:
1. returning to the first half term of direct hydrogenation liquefaction of coal reaction process；Oil gas can be increased to divide and then increase liquid number Amount can be used as the quench oil being added among reaction process and use reduction temperature rise；Cooperation high concentration coal slurry defeated slurry technology with slurry makes With multi-processing coal dust；
2. after pressurization, directly returning to the first half term of direct hydrogenation liquefaction of coal reaction process；
3. after pressurization, after heat exchange heating, directly returning to the first half term of direct hydrogenation liquefaction of coal reaction process；It can assist Adjust the thermal balance of reactive moieties；High concentration coal slurry defeated slurry technology with slurry is cooperated to use, multi-processing coal dust；
4. be used as coal slurry prepare solvent naphtha defeated coal with slurry, reduce long circulating circuit hydrogen supply dissolvent oil quantity, reduce investment and Energy consumption；
5. the spray of cold oil, the discharge gas of the high pressure hot separator or reactor as front reaction product RUAP is washed Wash oily use, complete wash dedirt while, some hydrocarbon in gas phase is condensed into liquid phase, thus directly return or with pump Any position of the first half term of direct hydrogenation liquefaction of coal reaction process is gone in conveying；
6. cold oil is used as Conduit rinse oil or pump flushing oil or instrument flushing oil etc., and eventually enters into coal hydrogenation Any position of the first half term of direct liquefaction reaction process.
Middle circulation loop solvent naphtha, can be with part or all of long circulating circuit hydrogen supply dissolvent oil (or high boiling solvent group Point) HC mixing conduct solvent naphtha with slurry, it can also be independently used as dedicated low boiling point solvent naphtha with slurry.
Half way hydrogen supply dissolvent MKDS, independently when solvent naphtha with slurry used as dedicated low boiling point, with high boiling solvent group The process with slurry of HC is divided to compare, operation temperature would generally be reduced to reduce volatilization, increase liquid phase viscosity, the coal of the coal slurry of preparation Concentration would generally be lower.
Direct hydrogenation liquefaction of coal reaction process realizes that mode of the invention is unrestricted, and there are many concrete mode, half way hydrogen supply The coal slurry that solvent MKDS is prepared, can or asynchronous participation synchronous with other coal slurries react, for example, half way hydrogen supply dissolvent MKDS matches The coal slurry of system, association response after being mixed with the intermediate reaction product of other coal slurries, so as to shorten middle circulation loop solvent naphtha Residence time of the MC in reaction process.
Use of the invention can be completed under the premise of not changing existing coal slurry and preparing with pressure-increasing unit technology, because This, is that the hydrogen supply dissolvent oil application method of an independent direct hydrogenation liquefaction of coal reaction process and a kind of independent coal add Hydrogen direct liquefaction reactor is into coal slurry technology.
The present invention can apply direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation heat cracking reaction mistake in various processes Cheng Zhong, for example for conventional liquid gas cocurrent tandem reactor process, connect for liquid material, reaction process of the hydrogen across stream operation, Reaction process for liquid material series connection, hydrogen parallel operation；It was reacted for liquid material series connection, the reverse-flow of hydrogen counter-current operation Journey, this is also of the invention to be recommended to use mode.
Raw material that present invention combination direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation heat cracking reaction process use produces Product propose specific process, also imply (in secret) possible potential flow model.
With there are many technologies similar in Process flow of the present invention, there is heavy oil expanded bed hydrocracking technology technique skill Art, direct hydrogenation liquefaction of coal technology, kerosene refine hydrogen addition technology altogether, are listed below the representational type of skill and compare.
The 1st kind of technology with the present invention with part similitude is heavy oil boiling bed hydrogenation cracking technology LC- Fining, a document for recording this category information are shown in: 1. publication title: " hydrofinishing ", page 308 to page 315；2. retrieval is used Books coding: ISBN coding: 978-7-80229-026-6；3. chief editor: direction morning；4. publishing house: Sinopec publishing house.? In the process flow of heavy oil boiling bed hydrogenation cracking technology LC-Fining, last boiling bed hydrogenation cracker it is anti- Product is answered, into being separated into hot high score gas and hot high score oil in high pressure hot separator, hot high score gas containing a large amount of hydrocarbon ils and is come It is anti-that the hydrocarbon ils (wax oil and its lower oil of boiling point) that self-heating high score oil is depressured flashed vapour condensate liquid enters hot high score gas hydro-upgrading Answer the diesel oil that low-sulfur, low nitrogen, the high saturation of low alkene, low aromatic hydrocarbons, high hexadecane are produced in device.Hot high score gas in the technique Hydro-upgrading reaction process, the stabilized hydrogenation reaction process with the hot high score gas RUA-PS-V of intermediate product of the invention exists Following essential distinction:
1. raw material high score gas source position is different, the raw material high score gas in LC-Fining technique is finally to be hydrocracked production The hot high score gas of object, raw material high score gas of the invention are the hot high score gas RUA-PS-V of intermediate product；
2. the composition difference for the hydro carbons that raw material high score gas carries is huge, the raw material high score gas in LC-Fining technique is carried Hydrogen hydro carbons to be added be the very low hydro carbons of HI SA highly saturated fragrant charcoal rate, the hydrogen hydro carbons to be added that raw material high score gas of the invention carries is The fragrant very high hydro carbons of charcoal rate；
3. the type difference for the leading hydrogenation reaction that hydro-upgrading reaction process occurs is huge, in LC-Fining technique The leading hydrogenation reaction that hydro-upgrading reaction process occurs is that (including depth hydrogenation of olefins is full for the deep hydrofinishing of middle matter hydrocarbon Hydrogen is added to split with deep hydrodesulfurizationof, deep hydrogenation denitrogenation, depth aromatic hydrocarbons saturation, even mild hydrocracking such as selective opening Change), target be produce low-sulfur, low nitrogen, the high saturation of low alkene, low aromatic hydrocarbons, high hexadecane diesel oil, the ten of diesel product The expectation of six alkane values reaches 45~59, and fragrant charcoal rate is usually less than 20% even lower than 5%；Hydro-upgrading reaction in present invention process The leading hydrogenation reaction that process occurs is the appropriate aromatic hydrogenation saturated reaction (commonly referred to as stabilized hydrogenation reaction) of middle matter hydrocarbon, with Restore the hydrogen supply of hydrogen supply hydrocarbon, the fragrant charcoal rate of hydrogen supply hydrocarbon is usually 44~55%, and the Cetane number of diesel oil distillate is usually less than 25； There is essential gender gap in catalyst, the reaction condition etc. that above-mentioned two hydro-upgrading reaction process uses；
4. the whereabouts difference of hydro-upgrading reaction product is huge, the hydro-upgrading reaction product in LC-Fining technique is made For the sale of fine-quality diesel oil product；For hydro-upgrading reaction product in present invention process as high-quality hydrogen supply hydrocarbon, part is (usually big Part) leading portion hydrogenation process is returned as the recycling of liquid hydrogen supply agent, part (usually small part) adds into other Hydrogen grading process uses after further increasing quality as clear gusoline.
Hot high score gas hydro-upgrading reaction process in present invention process, with heavy oil boiling bed hydrogenation cracking technology LC- Hot high score gas hydro-upgrading reaction process in Fining changes in workflow position, raw material sources, hydrogen hydro carbons to be added composition plus hydrogen Matter dominates hydrogenation reaction type, is hydrogenated to oil nature, hydrogenated oil whereabouts and purposes etc. that there is the differences of essence It is different, it is evident that be two different technical process.
The 2nd kind of technology with the present invention with part similitude is heavy oil floating bed hydrocracking technology Canmet Unionfining treatment process, a document for recording this category information is shown in: 1. publication title: " hydrofinishing ", page 315 are extremely Page 318；2. retrieval is encoded with books: ISBN coding: 978-7-80229-026-6；3. chief editor: direction morning；4. publishing house: China Petrochemical industry publishing house.In the Unionfining treatment process process flow of heavy oil floating bed hydrocracking technology Canmet, last The reaction product of platform slurry-bed hydrocracking device, into be separated into high pressure hot separator hot high score gas and hot high score oil, Hot high score gas containing a large amount of hydrocarbon ils enters in hot high score gas hydro-upgrading reactor the high saturation for producing low-sulfur, low nitrogen, low alkene The diesel oil of degree, low aromatic hydrocarbons, high hexadecane.The function myopia of the hydro-upgrading reaction process of hot high score gas in the technique is in aforementioned Heavy oil boiling bed hydrogenation cracking technology LC-Fining in hot high score gas hydro-upgrading reaction process, in of the invention Between the hot high score gas RUA-PS-V of product stabilized hydrogenation reaction process, there is essential differences.Heat in present invention process is high Divide the hot high score gas hydro-upgrading in gas hydro-upgrading reaction process, with heavy oil boiling bed hydrogenation cracking technology LC-Fining anti- Process is answered, dominates hydrogenation reaction type, hydrogenated oil in workflow position, raw material sources, hydrogen hydro carbons to be added composition, hydro-upgrading There is the differences of essence for property, hydrogenated oil whereabouts and purposes etc., it is evident that is two different technique mistakes Journey.
Additionally, there are some and heavy oil floating bed hydrocracking technology Canmet Unionfining treatment process process flows Essentially identical technique, Unionfining treatment process, Venezuela Intevep such as heavy oil floating bed hydrocracking technology VCC With the heavy oil floating bed hydrocracking technology HDHPLUS-SHP of French Axens cooperative development.Record heavy oil floating bed hydrocracking One document of this category information of the Unionfining treatment process of technology VCC is shown in: 1. publication title: " hydrofinishing ", page 315 are extremely Page 319；2. retrieval is encoded with books: ISBN coding: 978-7-80229-026-6；3. chief editor: direction morning；4. publishing house: China Petrochemical industry publishing house.In the Unionfining treatment process of heavy oil floating bed hydrocracking technology VCC, last floating bed hydrogenation is split Change reactor reaction product, into be separated into high pressure hot separator hot high score gas and hot high score oil, the heat containing a large amount of hydrocarbon ils High score gas, which enters in hot high score gas hydro-upgrading reactor, produces low-sulfur, low nitrogen, the high saturation of low alkene, low aromatic hydrocarbons, high by ten The diesel oil of six alkane.The function of the hydro-upgrading reaction process of hot high score gas in the technique, with heavy oil floating bed hydrogenation above-mentioned The hydro-upgrading reaction process of hot high score gas in the Unionfining treatment process process flow of cracking technology Canmet is identical, with The stabilized hydrogenation reaction process of the hot high score gas RUA-PS-V of intermediate product of the invention, there is essential difference, be two not Same technical process.
The 3rd kind of technology with the present invention with part similitude is direct hydrogenation liquefaction of coal technology IGOR+ technique, A document for recording this category information is shown in: 1. publication title: " coal direct liquefaction technique and engineering ", page 141 to page 142； 2. retrieval is encoded with books: ISBN coding: 9-78703-04308-23；3. writing: Wu Xiuzhang, Shu Geping, Li Kejian, Xie Shun It is quick；4. publishing house: Science Press.In direct hydrogenation liquefaction of coal technology IGOR+ technique, last suspension bed coal hydrogenation is straight The reaction product for connecing liquefying reactor contains a large amount of hydrocarbon ils into hot high score gas and hot high score oil is separated into high pressure hot separator Hot high score gas enter in hot high score gas hydro-upgrading reactor production hydrogen supply hydrocarbon.The hydro-upgrading of hot high score gas in the technique The function of reaction process, the stabilized hydrogenation reaction process with the hot high score gas RUA-PS-V of intermediate product of the invention, there are following Essential distinction:
1. raw material high score gas source position is different, the raw material high score gas in IGOR+ technique is that last suspension bed coal adds The hot high score gas of the product of hydrogen direct liquefaction reactor, raw material high score gas of the invention are that front conversion zone suspension bed coal hydrogenation is straight Meet the hot high score gas RUA-PS-V of the i.e. direct hydrogenation liquefaction of coal reaction intermediate of product of liquefying reactor；
2. the composition difference for the hydro carbons that raw material high score gas carries is huge, raw material high score gas in IGOR+ technique carry to Hydrogenated hydrocarbons class is that experienced the hydrogen supply hydrocarbon thermal cracking conversion product of back segment direct hydrogenation liquefaction of coal reactor, and by a large amount of coal liquefactions Middle matter hydrocarbon (fragrant charcoal rate is higher) is polluted, and is the poor hydro carbons of hydrogen supply capacity；What the raw material high score gas in present invention process carried Hydrogen hydro carbons to be added does not undergo the heat from hydrogenation cracking process of back segment direct hydrogenation liquefaction of coal reactor, is to remain certain degree Conversion product after the hydrogen supply hydrocarbon hydrogen supply reaction of hydrogen supply capacity, and only by matter hydrocarbon in a small amount of coal liquefaction intermediate product (fragrant charcoal rate is higher) It pollutes in other words substantially without contaminated, is the stronger hydro carbons of hydrogen supply capacity；
3. the type difference for the leading hydrogenation reaction that hydro-upgrading reaction process occurs is huge, in IGOR+ technique plus hydrogen The leading hydrogenation reaction that modification reaction process occurs is appropriate aromatic hydrogenation saturated reaction (the commonly referred to as stabilized hydrogenation of middle matter hydrocarbon Reaction), to restore the hydrogen supply of hydrogen supply hydrocarbon, since hydrogen hydro carbons to be added is that matter hydrocarbon produces in hydrogen supply hydrocarbon thermal cracking conversion product and coal liquefaction The mixture of object is haveed the characteristics that same boiling range different hydrocarbons virtue charcoal rate produces not big, stabilized hydrogenation reaction product, is existed with boiling Journey different hydrocarbons virtue charcoal rate produces not big disadvantage, is unfavorable for regulating and controlling virtue of the reaction condition to realize different hydrocarbons in hydrogen supply hydrocarbon products Charcoal rate reaches optimum range simultaneously；Although the leading hydrogenation reaction that the hydro-upgrading reaction process in present invention process occurs is also The appropriate aromatic hydrogenation saturated reaction (commonly referred to as stabilized hydrogenation reaction) of middle matter hydrocarbon is to restore the hydrogen supply of hydrogen supply hydrocarbon, still, Due to hydrogen hydro carbons to be added be hydrogen supply hydrocarbon hydrogen supply reaction after conversion product, only by matter hydrocarbon (fragrant charcoal in a small amount of coal liquefaction intermediate product Rate is higher) it pollutes in other words substantially without contaminated, therefore it is not small with the production of boiling range different hydrocarbons virtue charcoal rate, stabilized hydrogenation is anti- It answers in product, has the advantages that same boiling range different hydrocarbons have the not small i.e. structure of fragrant charcoal rate production uniform, be conducive to regulation reaction condition To realize the fragrant charcoal rate of different hydrocarbons in hydrogen supply hydrocarbon products while reach optimum range, that is, there is the feedstock property base of optimization operation Plinth；, there is proximity in catalyst, the reaction condition etc. that above-mentioned two hydro-upgrading reaction process uses, still, product hydrogen supply The hydrogen supply performance of hydrocarbon, it is pure in bigger difference；
4. the circulating path area difference of hydro-upgrading reaction product is huge, the hydrogen supply hydrocarbon in IGOR+ technique is recycled as and matches Coal slurry solvent naphtha then passes through front conversion zone suspension bed direct hydrogenation liquefaction of coal reactor, rear portion conversion zone suspension bed coal adds Hydrogen direct liquefaction reactor experienced backend hydrogenation thermal cracking in the conversion zone suspension bed direct hydrogenation liquefaction of coal reactor of rear portion Process, and polluted by matter hydrocarbon in a large amount of coal liquefactions (fragrant charcoal rate is higher), it is the poor hydro carbons of hydrogen supply capacity；In present invention process Hydrogen supply hydrocarbon, can be recycled for use as coal blending slurry solvent oil, then pass through front conversion zone suspension bed direct hydrogenation liquefaction of coal reactor Afterwards, into the hot high score gas of the thermal high separation process of leading portion direct hydrogenation liquefaction of coal reaction product, therefore, rear portion is not suffered from Conversion zone suspension bed direct hydrogenation liquefaction of coal reactor is avoided in rear portion conversion zone suspension bed direct hydrogenation liquefaction of coal reactor In it is pure backend hydrogenation thermal cracking process, also avoid being polluted by matter hydrocarbon in a large amount of coal liquefactions (fragrant charcoal rate is higher), be only by Matter hydrocarbon (fragrant charcoal rate is higher) pollutes basic without contaminated in other words in a small amount of coal liquefaction intermediate product, is that hydrogen supply capacity is stronger Hydro carbons can reduce the suspension of rear portion conversion zone while without rear portion conversion zone suspension bed direct hydrogenation liquefaction of coal reactor Bed direct hydrogenation liquefaction of coal reactor volume reduces investment, and the thermal cracking gas making yield that can reduce hydrogen supply dissolvent reduces hydrogen Consumption improves liquid yield.
Hot high score gas hydro-upgrading reaction process in present invention process adds hydrogen to change with the hot high score gas in IGOR+ technique Qualitative response process dominates hydrogenation reaction result in workflow position, raw material sources, hydrogen hydro carbons to be added composition, hydro-upgrading plus hydrogen is raw The sides such as the reaction occurred at oil nature, hydrogenated oil, that is, hydrogen supply agent circulating path, hydrogenated oil, that is, hydrogen supply agent circulating path There is the differences of essence in face, it is evident that is two different technical process.
Additionally, there are some and essentially identical techniques of IGOR+ technique Unionfining treatment process process flow, such as day Brown coal liquefaction technique, that is, improved B CL technique of this NEDO exploitation,.A document for recording improved B CL technique information is shown in: 1. Publication title: " coal direct liquefaction technique and engineering ", page 152 to page 157；2. retrieval is encoded with books: ISBN coding: 9- 78703-04308-23；3. writing: Wu Xiuzhang, Shu Geping, Li Kejian, Xie Shunmin；4. publishing house: Science Press.In coal plus In hydrogen Direct liquefaction technology improved B CL technique, the reaction product of last suspension bed direct hydrogenation liquefaction of coal reactor, into Enter to be separated into hot high score gas and hot high score oil in high pressure hot separator, the hot high score gas containing a large amount of hydrocarbon ils enters hot high score gas and adds hydrogen Hydrogen supply hydrocarbon is produced in reforming reactor.The function of the hydro-upgrading reaction process of hot high score gas in the technique, and it is of the invention The stabilized hydrogenation reaction process of the hot high score gas RUA-PS-V of intermediate product, it to be two different techniques that there is essential differences Process.
For heavy hydrocarbon heat from hydrogenation cracking reaction process inferior, another advantage of the invention is also resided in, and can subtract Enter the quantity that rear portion is hydrocracked the middle fraction hydrocarbon of the i.e. overhydrocracking section of section less, being equivalent to reduces saturated hydrocarbons extractant Quantity, conducive to maintain inferior heavy oil such as residual oil heat from hydrogenation cracking reaction material liquid phase colloidal solution system stabilization, Become second liquid phase conducive to preventing colloid, asphalitine over-saturation to be precipitated to aggravate thermal condensation, coking reaction.This point, for Ebullated bed or suspension bed poor quality heavy hydrocarbon heat from hydrogenation cracking reaction process, influence great.
The technical solution similar with the present invention has not been reported.
Based on hydrogen supply dissolvent direct hydrogenation liquefaction of coal reaction process, heavy hydrocarbon heat from hydrogenation cracking reaction process inferior effect There is similar or identical feature with the mechanism of action, the present invention is by direct hydrogenation liquefaction of coal reaction process, heavy hydrocarbon heat from hydrogenation inferior The feed coal (coal of usually high hydrogen content, low impurity content) of cracking reaction process, inferior heavy oil (usually low hydrogen content, The heavy oil of high impurity content) uniformly it is classified as the hydrocarbon material of heavy (Heavy Hydrocarbon).
The present invention, the other related patents technologies applied with the present inventor from after in January, 2012, together constitutes system The efficient direct hydrogenation liquefaction of coal technology of change, heavy hydrocarbon heat from hydrogenation cracking technology inferior, these technologies are in square entropy (vector Change Entropy Changes) the inevitable conclusion of mathematical calculation process under theoretical direction, the circumstantial evidence of the verifying or homogeneous processes also tested, Therefore, the present inventor is by the hydrocarbon material heat from hydrogenation cracking reaction process H-HC of heavy and its product recovery process, energy recovery process Above-mentioned technology be referred to as square (Moment) entropy (Entropy) heavy hydrocarbon material (Heavy Hydrocarbon) heat from hydrogenation cracking Lighting (To Light Hydrocarbon) engineering technology, together simply referred to as the ME-HTL technology of the hydrocarbon material of heavy, it is such as described Direct hydrogenation liquefaction of coal engineering technology be referred to as ME-CTL technology, the inferior heavy oil heat from hydrogenation cracking engineering technology is referred to as For ME-HOTL technology.
The present invention is the direct hydrogenation liquefaction of coal reaction method using hydrogen supply hydrocarbon.
The present invention is the heavy-oil hydrogenation heat cracking reaction method using hydrogen supply hydrocarbon.
The balance of the lightweight hydrogen supply agent of the present invention and the hydrocarbon material heat from hydrogenation cracking reaction process of heavy, heavy hydrogen supply agent Application method.
The present invention and 2 grades or multistage hydrocarbon material heat from hydrogenation cracking reaction method.
The present invention, and with 2 or the hydrocarbon material heat from hydrogenation cracking reaction method of multiple hydrogenators.
The stage division of the present invention and the hydrocarbon material heat from hydrogenation cracking reaction process of heavy.
Therefore, the first object of the present invention is the stabilized hydrogenation of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Object reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, and hydrocarbon material can be coal and/or heavy oil, Hydrocarbon solid powder can be coal, waste plastics, scrap rubber etc..
Second purpose of the invention is the stabilized hydrogenation object for proposing middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, using 2 sections or multistage reaction process, make Tandem reaction system with hydrogen short circuit across stream.
The purpose of third of the present invention is the stabilized hydrogenation object for proposing middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, using 2 sections or multistage reaction process, make With the reaction system of hydrogen adverse current.
4th purpose of the invention is the stabilized hydrogenation object for proposing middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, using 2 sections or multistage reaction process, make With the reaction system of hydrogen parallel fluid flow.
5th purpose of the invention is the stabilized hydrogenation object for proposing middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, using hydrogen rich gas stripping step, to improve Recycling amount of the middle matter hydrogen supply dissolvent oil in leading portion reaction process.
6th purpose of the invention is the stabilized hydrogenation object for proposing middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, secondary use hydrogen-rich stream.
7th purpose of the invention is the stabilized hydrogenation object for proposing middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, and the middle matter hydrocarbon of reuse is used as molten with slurry Agent oil enters direct hydrogenation liquefaction of coal reaction process, and slurry can be coal slurry and catalyst pulp.
8th purpose of the invention is the stabilized hydrogenation object for proposing middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, and reaction process uses hydrogen supply hydrocarbon.
9th purpose of the invention is the stabilized hydrogenation object for proposing middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Reuse method, middle matter hydrocarbon stabilized hydrogenation conversion product return to front reaction zone and are recycled, and front reaction zone uses 2 or multiple strings Join the reactor of operation.
Tenth purpose of the invention is to propose that a kind of dirty coal adds hydrogen direct liquefaction reaction method.
11st purpose of the invention is to propose a kind of coal slurry configuration and conveying with half way hydrogen supply dissolvent for solvent naphtha with slurry Method is suitable for direct hydrogenation liquefaction of coal reaction process.
12nd purpose of the invention is the direct hydrogenation liquefaction of coal reaction method for proposing a kind of efficient transfer reaction heat, is suitble to In strongly exothermic direct hydrogenation liquefaction of coal reaction process, for example hydrogen consumes high direct hydrogenation liquefaction of coal reaction process, dense coal slurry adds Hydrogen direct liquefaction reaction process etc..
Summary of the invention
The stabilized hydrogenation object reuse method of middle matter hydrocarbon, feature in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention It is to comprise the steps of:
(1) in hydrocarbon material hydrogenation process RU, there are hydrogen, conventional liq hydrocarbon, there may be solid particles simultaneously Under the conditions of mixed phase material, hydrogenation reaction RU-R at least is carried out containing the first raw material RU-F1 of carbon and protium and is converted into most Whole hydrogenation reaction product RU-P；Recycle final hydrogenation reaction product RU-P；
First raw material RU-F1 includes liquid material RU-F1L and solid particulate materials RU-F1S that may be present；
Hydrogenation reaction RU-R, the hydrofining reaction comprising at least part liquid material RU-F1L include at least one The hydrocracking reaction for dividing liquid material RU-F1L, the stabilized hydrogenation comprising the free radical that at least part heat cracking reaction generates Reaction may include the hydrogenation liquefaction reaction of at least part solid particulate materials RU-F1S that may be present；
Hydrogenation reaction RU-R may use catalyst RU-CAT；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon for the hydrocarbon component for being 230~400 DEG C containing normal boiling point is used；
In hydrocarbon material hydrogenation process RU, the external of the hydrogen supply hydrocarbon SH for being 230~400 DEG C containing normal boiling point may be used Hydrogen supply hydrocarbon OUT-TO-RU-DS；
In hydrocarbon material hydrogenation process RU, it is possible to create the hydrogen supply the hydrocarbon component RU- that normal boiling point is 230~400 DEG C PRO-DSC；
Hydrocarbon material hydrogenation process RU uses hydrogenator RU-XE, final hydrogenation reaction product RU-P, to contain hydrogen Gas, conventional liq hydrocarbon simultaneously may the mixed phase material containing solid particle, with 1 tunnel or 2 tunnels or multichannel when leaving reactor RU-XE The form of material RU-P-X occurs, and material RU-P-X is gas phase or liquid phase or gas-liquid mixed phase or gas-liquid-solid three-phase logistics；
In hydrocarbon material hydrogenation process RU, setting may include at least two reaction of the serial operation of the liquid material of solid Section；
One conversion zone refers to that the gas-liquid separation comprising liquid material hydrogenation reaction step and the step gas-liquid product walks Rapid technical process；
The front conversion zone RUA of the hydrocarbon material hydrogenation process RU, refers to hydrocarbon material hydrogenation process RU's Any upstream reaction section of the last one conversion zone RUJ or whole upstream reaction sections；
In hydrocarbon material hydrogenation process RU, at least 2 hydrogenator RU-XE are used；
Separating liquid RUAP-HS-L is separated into separation process RUAP-HS, at least part leading portion hydrogenation reaction product RUAP With the separation gas RUAP-HS-V for the hydrocarbon component for being 230~400 DEG C containing normal boiling point；
Separating liquid RUAP-HS-L is converted into rear portion reaction product RUBP into rear portion conversion zone RUB；
The logistics of the hydrocarbon component that containing normal boiling point is 230~400 DEG C of at least part based on separation gas RUAP-HS-V Used as material MR-F, it is understood that there may be residual gas RUAP-HS-V used as material RUAP-HS-V-BYPASS；
(2) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR- F is converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, and the hydro carbons in material MR-F carries out the portion of aromatic hydrocarbons Divide plus hydrogen saturated reaction MRR is converted into hydrogen supply the hydrocarbon component MR-DS；
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Recycle hydrocarbons MR-KRDS enters hydrocarbon material hydrogenation process RU；
At least part recycle hydrocarbons MR-KRDS returns to hydrocarbon material hydrogenation process RU's as MR-KRDS-TO-RUA Front reaction zone RUA participates in hydrocarbon material hydrogenation reaction RUA-R.
The present invention, in general, using at least 2 hydrogenator RU-XE, at least 1 in hydrocarbon material hydrogenation process RU Hydrogenator is up flow type expanded bed hydrogenator.
The present invention, common operation target is: the hydro carbons in return course TLOOP, recycle hydrocarbons MR-KRDS is in weight Mainly it is made of the hydrocarbon component that normal boiling point is 230~400 DEG C.
The present invention can be with simultaneous processing hydrogen supply hydrocarbon precursor MR-FK in stabilized hydrogenation reaction process MR；
In stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, hydrogen supply hydrocarbon predecessor Object MR-FK, material MR-F are converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, in material MR-F The partial hydrogenation saturated reaction MRR that hydro carbons carries out aromatic hydrocarbons is converted into hydrogen supply the hydrocarbon component MR-DS.
The present invention, in hydrocarbon material hydrogenation process RU, the hydrogenator of front conversion zone RUA and separation process The equipment that RUAP-HS is used, can be mutually indepedent.
The present invention, in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA, which has, to be produced Object part takes off liquid separation function, obtains separating liquid and gas-liquid mixed phase material, and separation process RUAP-HS can be in front conversion zone It is carried out in last hydrogenator of RUA.
The present invention, in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA, which has, to be produced The clear separation function of object gas-liquid, obtain separating liquid and separation gas, separation process RUAP-HS can front conversion zone RUA most It is carried out in latter hydrogenator.
The present invention, in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA, which has, to be produced The clear separation function of object gas-liquid, obtain separating liquid and separation gas, separation process RUAP-HS front conversion zone RUA last It is carried out in platform hydrogenator, last hydrogenator mode of operation can be gas-liquid counter current operation mode.
The present invention can be used as object based on separation gas RUAP-HS-V at least partially in hydrocarbon material hydrogenation process RU Expect that MR-F is used.
The present invention, the operation mode for obtaining material MR-F may is that
(1) in hydrocarbon material hydrogenation process RU, thermal high separation is entered based on separation gas RUAP-HS-V at least partially Process AP-HS is separated into hot high score gas AP-HS-V and hot high score oil AP-HS-L；
The logistics of the hydrocarbon component that containing normal boiling point is 230~400 DEG C of at least part based on hot high score oil AP-HS-L It is used as material MR-F.
The present invention, the operation mode for obtaining material MR-F may is that
(1) in hydrocarbon material hydrogenation process RU, thermal high separation is entered based on separation gas RUAP-HS-V at least partially Process AP-HS is separated into hot high score gas AP-HS-V and hot high score oil AP-HS-L；
The logistics of the hydrocarbon component that containing normal boiling point is 230~400 DEG C of at least part based on hot high score gas AP-HS-V It is used as material MR-F.
The present invention, the operation mode for obtaining recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
At least part stabilized hydrogenation reaction product MRP is used as recycle hydrocarbons MR-KRDS.
The present invention, the operation mode for obtaining recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Stabilized hydrogenation reaction product MRP is separated, the liquid for the hydrogen supply the hydrocarbon component for being 230~400 DEG C containing normal boiling point is obtained State logistics XXK, the logistics at least partially based on liquid stream XXK are used as recycle hydrocarbons MR-KRDS.
The present invention, the operation mode for obtaining recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Stabilized hydrogenation reaction product MRP is separated, the gas for the hydrogen supply the hydrocarbon component for being 230~400 DEG C containing normal boiling point is obtained State logistics YYK, the logistics at least partially based on gaseous stream YYK are used as recycle hydrocarbons MR-KRDS.
The circulate operation mode of the present invention, recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
At least part recycle hydrocarbons MR-KRDS enters hydrocarbon material hydrogenation process RU after mixing with the first raw material RU-F1.
The circulate operation mode of the present invention, recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
First raw material RU-F1 of at least part recycle hydrocarbons MR-KRDS and at least part solid powder shape is mixed into slurry After material, into hydrocarbon material hydrogenation process RU.
The present invention, operation target may is that
(1) hydrogen supply hydrocarbon RUA-DS is used in front conversion zone RUA in hydrocarbon material hydrogenation process RU；
Leading portion hydrogenation reaction RUA-R, uses catalyst RUA-CAT；
(3) hydro carbons in return course TLOOP, recycle hydrocarbons MR-KRDS.In weight mainly by normal boiling point be 230 ~400 DEG C of the hydrocarbon component composition.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU.
The present invention, operation target may is that
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is lower than hydrogenation reaction product RUAP 0~1.0MPa of operating pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is 350~480 DEG C.
The present invention, operation target may is that
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is lower than hydrogenation reaction product RUAP 0~0.5MPa of operating pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is 400~450 DEG C.
The present invention, operation target may is that
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is lower than hydrogenation reaction product RUAP 0~1.0MPa of operating pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, than hydrogenation reaction product RUAP's 5~80 DEG C of low operation temperature.
The present invention, operation target may is that
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is lower than hydrogenation reaction product RUAP 0~1.0MPa of operating pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, in the item for guaranteeing material noncoking Under part, the difference DT of operation temperature and the operation temperature of hydrogenation reaction product RUAP is small as far as possible.
The present invention, operation target may is that
(1) in hydrocarbon material hydrogenation process RU, setting may include 2 or multiple of the serial operation of the liquid material of solid Conversion zone wherein be existed between conversion zone in the presence of the series flow for the liquid material that may include solid with the liquid material that may include solid Flowing between conversion zone is forward direction, the type of flow classification of hydrogen material between conversion zone, a kind or several selected from following manner Kind:
1. hydrogen material flows to cocurrent in the same direction with the main body of serum materials, belong to liquid, gas cocurrent tandem reactor process；
2. slurry series connection, tandem reactor process of the hydrogen short circuit across stream；
3. gas-phase product does not enter the reaction process of other any conversion zones there are at least one conversion zone, gas is former Material do not use the hydrogen from other any conversion zones, belong to there are hydrogen material parallel operation reaction process；
4. reaction process receives the hydrogen product of downstream reaction section there are at least one conversion zone, belong in conversion zone Between there are the reaction process of hydrogen gas product counter-current operation.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, using by normal boiling point being mainly 230~400 DEG C The hydrogen supply hydrocarbon TO-RUA-DS of hydro carbons composition.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen supply hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V is used as material MR-F.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen supply hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
Warm high pressure separate section RUAP-HS-V-MS is set, separation gas RUAP-HS-V is separated into gas RUAP-HS-V- MS-V and separating liquid RUAP-HS-V-MS-L；The hydrocarbon for being 230~400 DEG C containing normal boiling point in separating liquid RUAP-HS-V-MS-L Component；
At least part separating liquid RUAP-HS-V-MS-L is used as material MR-F.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen supply hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
It is set using the warm high pressure separate section RUAP-HS-V-MS of gas stripping gas RUAP-HS-V-MS-BH, gas will be separated RUAP-HS-V is separated into gas RUAP-HS-V-MS-V and separating liquid RUAP-HS-V-MS-L；
Separating liquid RUAP-HS-V-MS-L and gas stripping gas RUAP-HS-V-MS-BH completes to separate, and is separated into air lift row The gentle extract RUAP-HS-V-MS-L-BL of deflation RUAP-HS-V-MS-L-BV；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid RUAP-HS-V-MS-L-BL；
At least part air lift liquid RUAP-HS-V-MS-L-BL is used as material MR-F.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen supply hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
It is set using the warm high pressure separate section RUAP-HS-V-MS of gas stripping gas RUAP-HS-V-MS-BH, gas will be separated RUAP-HS-V is separated into gas RUAP-HS-V-MS-V and separating liquid RUAP-HS-V-MS-L；
Separating liquid RUAP-HS-V-MS-L and gas stripping gas RUAP-HS-V-MS-BH completes to separate, and is separated into air lift row The gentle extract RUAP-HS-V-MS-L-BL of deflation RUAP-HS-V-MS-L-BV；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid RUAP-HS-V-MS-L-BL；
At least part air lift liquid RUAP-HS-V-MS-L-BL is used as material MR-F；
(3) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR- F is converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, and the hydro carbons in material MR-F carries out the portion of aromatic hydrocarbons Divide plus hydrogen saturated reaction MRR is converted into hydrogen supply the hydrocarbon component MR-DS；
(4) separation is separated into the separation process MRP-S using gas stripping gas MRP-S-BH, stabilized hydrogenation reaction product MRP The separating liquid MRP-L of gas MRP-V and the hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point；
Separating liquid MRP-L and gas stripping gas MRP-S-BH completes to separate, and it is gentle to be separated into air lift discharge gas MRP-L-BV Extract MRP-L-BL；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid MRP-L-BL；
Material of at least part based on air lift liquid MRP-L-BL is used as recycle hydrocarbons MR-KRDS.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, using by normal boiling point being mainly 230~400 DEG C The hydrogen supply hydrocarbon TO-RUA-DS of hydro carbons composition；
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V is used as material MR-F, existing residual gas RUAP-HS-V conduct Material RUAP-HS-V-BYPASS is used；
Material RUAP-HS-V-BYPASS enters separation process, is separated into gas RUAP-HS-V-BYPASS-V and containing normal Advise the lime set RUAP-HS-V-BYPASS-L for the hydrocarbon component that boiling point is 230~400 DEG C；
At least part lime set RUAP-HS-V-BYPASS-L, into hydrocarbon material hydrogenation process RU；
At least part lime set RUAP-HS-V-BYPASS-L returns to the front reaction zone of hydrocarbon material hydrogenation process RU RUA participates in hydrocarbon material hydrogenation reaction RUA-R.
The present invention, operation target when processing hydrocarbon powder RU-F1S may is that
(1) hydrocarbon material hydrogenation process RU adds hydrogen direct liquefaction reaction process RU for the hydrocarbon powder RU-F1S of raw material, 2 or multiple conversion zones of slurries serial operation are set；
One conversion zone refers to that the gas-liquid separation comprising slurry hyd reaction step and the step gas-liquid product walks Rapid technical process；
The front conversion zone RUA refers to any conversion zone in the upstream of the last one conversion zone or whole upstream reactions Section；
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, there are hydrogen, include conventional liq hydrocarbon, the carbon of hydrogen supply hydrocarbon Hydrogen powder and there may be under conditions of catalyst, carry out at least part hydrocarbon powder RU-F1S's plus hydrogen direct liquefaction it is anti- It answers RU-R to be converted into hydrocarbon powder and adds hydrogen direct liquefaction final reacting product RU-P；Final hydrogenation reaction product RU-P, be 1 tunnel or 2 tunnels or multichannel material；Recycle final hydrogenation reaction product RU-P；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon TO-RU- for the hydro carbons for being 230~400 DEG C containing normal boiling point is used DS；
In front conversion zone RUA, the hydrogen supply hydrocarbon RUA-DS for the hydro carbons for being 230~400 DEG C containing normal boiling point is used；
Add the front conversion zone RUA of hydrogen direct liquefaction reaction process RU in hydrocarbon powder, there are hydrogen, include hydrogen supply hydrocarbon Conventional liq hydrocarbon, hydrocarbon powder and there may be under conditions of catalyst, hydrocarbon powder RU-F1S carries out at least part Hydrocarbon powder adds hydrogen direct liquefaction front reaction RUA-R to be converted into hydrocarbon powder and adds hydrogen direct liquefaction front reaction product RUAP； Front reaction product RUAP is 1 tunnel or 2 tunnels or multichannel material；
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU, in the same of recycle hydrocarbons MR-KRDS of the processing from step (5) When, other hydrogen supply dissolvent oil BDS and hydrocarbon powder KS can be capable of processing；
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V used as material MR-F, it is understood that there may be residual gas RUAP-HS-V It is used as material RUAP-HS-V-BYPASS；
(3) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR- F is converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, and the hydro carbons in material MR-F carries out the portion of aromatic hydrocarbons Divide plus hydrogen saturated reaction MRR is converted into hydrogen supply the hydrocarbon component MR-DS；
(4) separation gas MRP-V is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP and contain normal boiling point For the separating liquid MRP-L of 230~400 DEG C of hydrogen supply the hydrocarbon component MR-DS；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
(5) enter hydrocarbon material hydrogenation process RU in return course TLOOP, recycle hydrocarbons MR-KRDS；
At least part recycle hydrocarbons MR-KRDS returns to hydrocarbon material hydrogenation process RU's as MR-KRDS-TO-RUA Front reaction zone RUA participates in hydrocarbon material hydrogenation reaction RUA-R.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
Material of a part based on separating liquid MRP-L, the rear portion for going hydrocarbon powder to add hydrogen direct liquefaction reaction process RU are anti- Answering a section RUB contact slurry to carry out hydrocarbon powder adds hydrogen direct liquefaction to react.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, at least two conversion zone of slurries serial operation is set, wherein There are the series flows of slurry between conversion zone, are forward direction, hydrogen object between conversion zone with flowing of the slurry between conversion zone The type of flow of material is classified, and a kind or several of following manner can be selected from:
1. hydrogen material flows to cocurrent in the same direction with the main body of serum materials, belong to liquid, gas cocurrent tandem reactor process；
2. slurry series connection, tandem reactor process of the hydrogen short circuit across stream；
3. gas-phase product does not enter the reaction process of other any conversion zones there are at least one conversion zone, gas is former Material do not use the hydrogen from other any conversion zones, belong to there are hydrogen material parallel operation reaction process；
4. reaction process receives the hydrogen product of downstream reaction section there are at least one conversion zone, belong in conversion zone Between there are the reaction process of hydrogen gas product counter-current operation.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, slurries raw material is when the reaction of front conversion zone RUA stops Between account for slurries raw material and add the 30~65% of the general reaction residence time of hydrogen direct liquefaction reaction process RU in whole hydrocarbon powder.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Most of hydro carbons in separating liquid MRP-L, can be selected from a kind or several in following conventional boiling range:
1. the conventional liquid hydrocarbon that normal boiling point is 230~400 DEG C；
2. the conventional liquid hydrocarbon that normal boiling point is 230~350 DEG C；
3. the conventional liquid hydrocarbon that normal boiling point is 230~300 DEG C.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
The weight of recycle hydrocarbons MR-KRDS is the 5~95% of separating liquid MRP-L weight.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(5) add hydrogen direct liquefaction anti-by hydrocarbon powder in return course TLOOP, at least part recycle hydrocarbons MR-KRDS Answering whole main body reaction compartments of the first reactor of the first conversion zone of process RU to carry out hydrocarbon powder adds hydrogen direct liquefaction anti- It answers.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(5) go hydrocarbon powder that hydrogen direct liquefaction is added to react in return course TLOOP, at least part recycle hydrocarbons MR-KRDS Process RU contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react, and working method can be selected from one of the following or several Kind:
1, at least part recycle hydrocarbons MR-KRDS are selected, the front that gravity flow returns to direct hydrogenation liquefaction of coal reaction process is anti- Section is answered, contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
2, at least part recycle hydrocarbons MR-KRDS are selected, the front conversion zone of direct hydrogenation liquefaction of coal reaction process is returned Contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
3, at least part recycle hydrocarbons MR-KRDS is selected to return to direct hydrogenation liquefaction of coal reaction process after heat exchange heating Front conversion zone, contact slurry carry out hydrocarbon powder and hydrogen direct liquefaction are added to react；
Selection 4, at least part recycle hydrocarbons MR-KRDS are used as coal slurry and prepare solvent naphtha configuration coal slurry MKDS-MJ, then coal Slurry MKDS-MJ enters direct hydrogenation liquefaction of coal reaction process, carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
Selection 5, at least part recycle hydrocarbons MR-KRDS are used as coal slurry and prepare solvent naphtha configuration coal slurry MKDS-MJ, then coal Slurry MKDS-MJ enters the front conversion zone of direct hydrogenation liquefaction of coal reaction process, carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
6, at least part recycle hydrocarbons MR-KRDS are selected, the washing oil in washing step DW, as gas RUAP-HS-V Using to wash the dust in abjection gas RUAP-HS-V；It, will be in gas RUAP-HS-V while completing to wash dedirt Some hydrocarbon is condensed into liquid phase DWL；
At least part liquid phase DWL returns to direct hydrogenation liquefaction of coal reaction process, and contact slurry carries out hydrocarbon powder and adds hydrogen Direct liquefaction reaction；
7, at least part recycle hydrocarbons MR-KRDS are selected, the washing oil in washing step DW, as gas RUAP-HS-V Using to wash the dust in abjection gas RUAP-HS-V；It, will be in gas RUAP-HS-V while completing to wash dedirt Some hydrocarbon is condensed into liquid phase DWL；
At least part liquid phase DWL returns to the front conversion zone of direct hydrogenation liquefaction of coal reaction process, and contact slurry carries out Hydrocarbon powder adds hydrogen direct liquefaction to react；
8, at least part liquid phase DWL are selected, direct hydrogenation liquefaction of coal reaction process contact slurry is returned and carries out hydrocarbon powder Before material plus the reaction of hydrogen direct liquefaction, it is used as Conduit rinse oil or pump flushing oil or instrument flushing oil.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
At least part recycle hydrocarbons MR-KRDS is used as hydrocarbon powder slurry preparation solvent naphtha and configures hydrocarbon powder slurry MR- KRDS-MJ, then hydrocarbon powder slurry MR-KRDS-MJ enters hydrocarbon powder and adds hydrogen direct liquefaction reaction process RU-RU, carries out carbon Hydrogen powder adds hydrogen direct liquefaction to react, and working method can be selected from one of the following or several:
1, recycle hydrocarbons MR-KRDS are selected, hydrocarbon powder slurry MR-KRDS- is prepared after mixing with other hydrogen supply dissolvent oil BDS BDS-MJ, hydrocarbon powder slurry MR-KRDS-BDS-MJ are used as hydrocarbon powder and starch MR-KRDS-MJ；
2, recycle hydrocarbons MR-KRDS are selected, hydrocarbon powder slurry preparation solvent naphtha is used alone as and configures hydrocarbon powder slurry MR- KRDS-MJ；
Other hydrogen supply dissolvent oil BDS prepare hydrocarbon powder and starch BDS-MJ.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
At least part recycle hydrocarbons MR-KRDS is used alone as hydrocarbon powder slurry preparation solvent naphtha and configures hydrocarbon powder slurry MR- KRDS-MJ；
Other hydrogen supply dissolvent oil BDS prepare hydrocarbon powder and starch BDS-MJ；
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the reaction time of hydrocarbon powder slurry MR-KRDS-MJ with The reaction time of hydrocarbon powder slurry BDS-MJ is not identical.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In washing process BW10, separates gas RUAP-HS-V and at least contacted 1 time with wash cooling liquid CWL, separate gas RUAP- At least part hydrocarbon gas in HS-V is changed into hydrocarbon liquid and enters in rich cleaning solution BW10-L, leaves washing process BW10 discharge gas BW10-V；The weight flow of rich cleaning solution BW10-L is greater than the weight flow of wash cooling liquid CWL；
At least part gas BW10-V is used as material MR-F.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In washing process BW10, separates gas RUAP-HS-V and at least contacted 1 time with wash cooling liquid CWL, separate gas RUAP- At least part hydrocarbon gas in HS-V is changed into hydrocarbon liquid and enters in rich cleaning solution BW10-L, leaves washing process BW10 discharge gas BW10-V；The weight flow of rich cleaning solution BW10-L is greater than the weight flow of wash cooling liquid CWL；
Rich cleaning solution BW10-L, whereabouts can be selected from one of the following or several:
1. being mixed into separating liquid RUAP-HS-L；
2. conversion zone RUA before going；
3. removing rear conversion zone RUB；
4. hydrocarbon powder process with slurry is gone to make to use with slurry solvent.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) in washing process BW10, the contact separation mode of operation of gas RUAP-HS-V and wash cooling liquid CWL are separated, it can Selected from one of the following or several:
1. separating after mixing, 1 contact, 1 separation is carried out；
2. counter current contacting carries out 2 contacts and 2 separation；
3. counter current contacting carries out multiple-contact and separating for several times.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) separation process RUAP-HS is carried out, most in last hydrogenator of leading portion hydrogenation process RUA Latter hydrogenator is unit equipment.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, hydrocarbon powder RU-F1S can a kind in following or It is several:
1. coal dust；
2. molding powder；
3. rubber powder；
4. direct hydrogenation liquefaction of coal reaction process RU mixes other hydrocarbon powders of refining.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, it is understood that there may be a kind or several in following of solid:
1. coal dust；
2. catalyst solid particle；
3. sulphur powder；
4. hydrocarbon ils coking material carrier semicoke particle；
5. molding powder；
6. rubber powder；
7. other solid powders that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to need to input.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process, can be selected from following work 1 kind or several during skill:
1. using the direct hydrogenation liquefaction of coal liquefaction process of hydrogen supply dissolvent oil；
2. not using the direct hydrogenation liquefaction of coal liquefaction process of hydrogen supply dissolvent oil；
3. kerosene refines process altogether；
4. coal faces hydrogen thermosol liquefaction process.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the hydrocarbon powder used adds hydrogen direct liquefaction reactor XRUE Working method can a kind or several in following:
1. suspended-bed reactor, that is, paste state bed reactor；
2. fluidized bed reactor；
3. suspension bed and ebullated bed combination type reactor.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the hydrocarbon powder used adds hydrogen direct liquefaction reactor XRUE Working method, can a kind or several in following:
Option 1, liquid material and gas material use the counter-current reactor of pure adverse current working method；
Option 2, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump Answer the fluidized bed reactor of device XRUE material inlet；
Option 3, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump Answer the suspended-bed reactor of device XRUE material inlet；
Option 4, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of device XRUE material inlet is answered, while circulating pump conveys circulation fluid, downstream transport liquid material product；
Option 5, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of device XRUE material inlet is answered, while circulating pump conveys circulation fluid, downstream transport liquid material product；
Option 6, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor for answering device XRUE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；
Option 7, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor for answering device XRUE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；
Option 8, reactor XRUE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport liquid Expect product, is not provided with the fluidized bed reactor system of liquid material product forced circulation；
Option 9, reactor XRUE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport liquid Expect product, is not provided with the suspended-bed reactor system of liquid material product forced circulation；
Option 10, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor XRUE material inlet and the combination type reactor of ebullated bed；
Option 11, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor XRUE material inlet and the combination type reactor of ebullated bed, while circulating pump conveys circulation fluid, downwards Trip conveying liquid material product；
Option 12, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor XRUE material inlet and the combination type reactor of ebullated bed are collected simultaneously other collection liquids warp of cup discharge Cross other dedicated feeding engine downstream transport liquid material products；
The suspended-bed reactor system of flow pattern under the center upstream surrounding of internal guide cylinder is arranged in option 13；
The suspended-bed reactor system of flow pattern in the dirty surrounding in center of internal guide cylinder is arranged in option 14；
Option 15, empty cylinder bubbling bed suspended-bed reactor system；
Option 16 is formed reactor top reaction zone liquid phase and is flowed down under Returning reactor using the external circulation pipe of reactor The device outside circulation of portion's reaction zone.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, conversion zone obtains the mode of product slurry, can be selected from down State a kind or several in mode:
1. the slurries that the gas-liquid separation process of autoreaction section reaction product is discharged, as final reaction section product slurry；
2. the final reactor of conversion zone uses pure counter-current reactor, the bottom liquid phase region of the final reactor of autoreaction section The slurries of discharge, as conversion zone product slurry；
3. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup warp in the final reactor of autoreaction section The slurries of diversion pipe discharge, as conversion zone product slurry；
4. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup warp in the final reactor of autoreaction section The slurries of diversion pipe discharge, as slurry to be de-gassed；
Slurry to be de-gassed is separated into the liquid stream rich in bubble, the liquid stream that lean gas steeps all the way all the way by cyclonic separation step；
The liquid stream of lean gas bubble, is used as conversion zone product slurry.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU, last hydrogenator RU19 of the first conversion zone in hydrocarbon powder, The reactor that there is part to take off liquid function of liquid collecting cup is set for top, and collection liquid RU19-DL-L derived from liquid collecting cup is as the One conversion zone product slurry, whereabouts can be selected from one of the following or several:
1. going the reaction step of the second conversion zone；
2. removing the gas-liquid separator of the first conversion zone product slurry, it is separated into degassing slurries and gas；
3. going the first conversion zone cyclic process；
4. portion collection liquid RU19-DL-L removes separation and recovery system after dropping valve is depressured.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
In separation and recovery process SYS300, recycles final hydrogenation reaction product RU-P and obtain hydrogen rich gas gas RH, at least one Part hydrogen rich gas gas RH returns to hydrocarbon powder and hydrogen direct liquefaction reaction process RU is added to be used as circulating hydrogen.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
The working method of separation and recovery process SYS300, hydrogen upgrading process H2UPU, H2UPU comprising hydrogen material can Selected from one of the following or several:
1. using membrane separation process concentrate hydrogen；
2. using PSA pressure swing adsorption technique concentrate hydrogen；
3. using deep cooling process for separating concentrate hydrogen.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
In separation and recovery process SYS300, recycles final hydrogenation reaction product RU-P and obtain hydrogen rich gas gas RH, work Mode can be selected from one of the following or several:
1. thermal high separation process RU-P-THPS, cold anticyclone separation process is arranged in separation and recovery process SYS300 CHPS；
Hot high score gas RU-P- is separated into thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P THPS-V and hot high score liquid material RU-P-THPS-L；
Cold high score gas CHPS-V and cold high score are separated into cold anticyclone separation process CHPS, hot high score gas RU-P-THPS-V Liquid material CHPS-L；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH；
2. in separation and recovery process SYS300, setting thermal high separation process RU-P-THPS, warm high pressure separation process MHPS, cold anticyclone separation process CHPS；
Hot high score gas RU-P- is separated into thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P THPS-V and hot high score liquid material RU-P-THPS-L；
Warm high score gas MHPS-V and Wen Gaofen are separated into warm high pressure separation process MHPS, hot high score gas RU-P-THPS-V Liquid material MHPS-L；
Cold high score gas CHPS-V and cold high score liquid material are separated into cold anticyclone separation process CHPS, warm high score gas MHPS-V CHPS-L；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH；
3. the thermal high separation process RU-P- with gas condensation collection step LCD is arranged in separation and recovery process SYS300 THPS, cold anticyclone separation process CHPS；
Hot high score gas RU-P- is first separated into thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P THPS-V and hot high score liquid material RU-P-THPS-L；Hot high score gas RU-P-THPS-V, in gas condensation collection step LCD cooling point From for condensate liquid LCD-L and de- liquid gas LCD-V；
Cold high score gas CHPS-V and cold high score liquid material CHPS- are separated into cold anticyclone separation process CHPS, de- liquid gas LCD-V L；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In separation process RUAP-HS, stripping step BH-S, which is arranged, using gas stripping gas BH makes leading portion hydrogenation reaction product The hydrocarbon component vapour based on hydrogen supply dissolvent oil that at least part normal boiling point in the liquid phase RUAP-L of RUAP is 230~400 DEG C Change and enter in separation gas RUAP-HS-V, increases the weight for the hydro carbons that normal boiling point is 230~400 DEG C in separation gas RUAP-HS-V Flow.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(1) add the working method of hydrogen direct liquefaction reaction process RU, stripping step BH-S in following in hydrocarbon powder One or more:
1. being mixed with gas stripping gas BH with the gas-liquid mixed phase product RUAP of front reaction zone, the hydro carbons in air lift slurries；
2. being contacted with gas stripping gas BH with the pure product slurry RUAP-LP of front reaction zone；
3. dividing front reaction process RUA to 2 grades of formula front reaction process RUA1, RUA2 for slurries serial operation, front The gas RUA1-P- for the hydrocarbon component based on hydrogen supply dissolvent oil that reaction process RUA1 discharge is 230~400 DEG C containing normal boiling point The gas for the hydrocarbon component based on hydrogen supply dissolvent oil that XV, front reaction process RUA2 discharge are 230~400 DEG C containing normal boiling point RUA2-P-XV, gas RUA1-P-XV and/or gas RUA2-P-XV are used as separation gas RUAP-HS-V.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(1) the gas stripping gas BH, Ke Yixuan for adding hydrogen direct liquefaction reaction process RU, stripping step BH-S to use in hydrocarbon powder From one or more of following materials:
1. the new hydrogen that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
2. the circulating hydrogen that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
3. the circulating hydrogen after the hydrogen upgrading that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
4. adding in hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the front reaction zone of product slurry RUA-LP is discharged The hydrogen rich gas material of the reaction zone discharge in downstream or its derivative gas；
5. hydrocarbon powder adds the matched hydrogen supply dissolvent in addition to MR reaction process of hydrogen direct liquefaction reaction process RU to add hydrogen Stablize hydrogen rich gas gas or its derivative gas that the reaction product of reaction process is isolated；
6. hydrocarbon powder adds the matched hydrocarbon powder liquefaction oil of hydrogen direct liquefaction reaction process RU to add hydrogen upgrading reaction process The hydrogen rich gas gas isolated of reaction product or its derive gas.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(4) in separation and recovery process SYS700, separation process MRP-S is set, stabilized hydrogenation reaction product MRP is separated into point From gas MRP-V and separating liquid MRP-L；
Separation and recovery process SYS700, working method are selected from one of the following or several:
1. thermal high separation process MRP-THPS is arranged in separation and recovery process SYS700；
Hot high score gas MRP-THPS-V is separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP With hot high score liquid material MRP-THPS-L；
Based on hot high score liquid material MRP-THPS-L, separating liquid MRP-L is obtained；
2. thermal high separation process MRP-THPS, cold anticyclone separation process MRP- is arranged in separation and recovery process SYS700 CHPS；
Hot high score gas MRP-THPS-V is separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP With hot high score liquid material MRP-THPS-L；
Cold anticyclone separation process MRP-CHPS, hot high score gas MRP-THPS-V be separated into cold high score gas MRP-CHPS-V and Cold high score liquid material MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or cold high score liquid material MRP-CHPS-L, separating liquid MRP-L is obtained；
3. in separation and recovery process SYS700, setting thermal high separation process MRP-THPS, warm high pressure separation process MRP- MHPS, cold anticyclone separation process MRP-CHPS；
Hot high score gas MRP-THPS-V is separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP With hot high score liquid material MRP-THPS-L；
Warm high pressure separation process MRP-MHPS, hot high score gas MRP-THPS-V be separated into warm high score gas MRP-MHPS-V and Warm high score liquid material MRP-MHPS-L；
Cold anticyclone separation process MRP-CHPS, warm high score gas MRP-MHPS-V be separated into cold high score gas MRP-CHPS-V and Cold high score liquid material MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or warm high score liquid material MRP-MHPS-L, separating liquid MRP-L is obtained；
4. the thermal high separation process with gas condensation collection step MRP-LCD is arranged in separation and recovery process SYS700 MRP-THPS, cold anticyclone separation process MRP-CHPS；
Hot high score gas MRP-THPS- is first separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP V and hot high score liquid material MRP-THPS-L；Hot high score gas MRP-THPS-V, in gas condensation collection step MRP-LCD cooling separation For condensate liquid MRP-LCD-L and de- liquid gas MRP-LCD-V；
Cold high score gas MRP-CHPS-V and cold high score are separated into cold anticyclone separation process CHPS, de- liquid gas MRP-LCD-V Liquid material MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or condensate liquid MRP-LCD-L, separating liquid MRP-L is obtained.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU, in the slurries MR-KRDS- that fabrication cycles hydrocarbon MR-KRDS is prepared While MJ, process the slurries BDS-MJ that other hydrogen supply dissolvent oil BDS are prepared, working method can in following one Kind:
1. slurries MR-KRDS-MJ, slurries BDS-MJ enter hydrocarbon powder and add hydrogen direct liquefaction reaction process RU after mixing Reactor in；
2. slurries MR-KRDS-MJ, slurries BDS-MJ, add that hydrogen direct liquefaction reaction process RU's is same into hydrocarbon powder In the same reaction space of a reactor；
3. positive on the basis of flowing through the main body flow direction in hydrogenation reaction space by slurries, the hydrocarbon material of slurries MR-KRDS-MJ adds The intermediate reaction product of hydrogen direct liquefaction enters subsequent hydrocarbon material and adds hydrogen direct liquefaction reaction process after mixing with slurries BDS-MJ In；
4. positive, the hydrocarbon material of slurries BDS-MJ on the basis of crossing the main body flow direction in hydrogenation reaction space by oil powder slurries stream The intermediate reaction product for adding hydrogen direct liquefaction enters subsequent hydrocarbon material and adds hydrogen direct liquefaction anti-after mixing with slurries MR-KRDS-MJ During answering.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrogen direct liquefaction reaction process RU, slurries MR-KRDS-MJ is added to enter hydrocarbon powder and add the direct liquid of hydrogen in hydrocarbon powder Changing the hydrocarbon powder of reaction process RU participation adds hydrogen direct liquefaction to react, and what is contacted first is other containing serum materials, can be selected from down One or more of column:
1. adding the hydrocarbon powder of participation of hydrogen direct liquefaction reaction process RU that hydrogen direct liquefaction is added to react into hydrocarbon powder Other slurries BDS-MJ；
2. hydrocarbon powder adds the hydrocarbon powder of participation of hydrogen direct liquefaction reaction process RU to add starch containing for hydrogen direct liquefaction reaction The recycle stock of liquid；
3. hydrocarbon powder add that hydrogen direct liquefaction reaction process RU generates containing serum materials, add hydrogen direct from hydrocarbon powder The intermediate product of liquefaction reaction process RU；
4. hydrocarbon powder add that hydrogen direct liquefaction reaction process RU generates containing serum materials, add hydrogen direct from hydrocarbon powder The final product of liquefaction reaction process RU.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, and setting slurries are connected At least two conversion zone of operation, whole oil powders slurry raw materials, which enter, to be participated in hydrocarbon powder in the reaction process of the first conversion zone and adds hydrogen Direct liquefaction reaction.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, the liquefied fraction of coal dust Greater than 85%.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, the liquefied fraction of coal dust It is 85~98%.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, while mixing the non-coal of refining Base weight oil FD.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, while mixing the non-coal of refining Base weight oil FD；The cracking conversion rate of heavy oil FD is greater than 90%.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, operating condition are as follows: Reaction temperature is 400~485 DEG C, and reactor pressure is 6~30MPa, vapor phase hydrogen volumetric concentration 50~95%, gas-liquid volume ratio For 300~1500NL/kg, deliquescence accelerant additive amount is 0.1~3 mass % of dry pulverized coal weight, and co-catalyst additive amount is Sulphur/catalyst activity metal molar ratio is 1.0~2.0 in co-catalyst, and coal slurry solid concentration is 40~60 mass %, reaction Residence time TRU is 0.5~4 hour.
In preceding conversion zone RUA, ratio, that is, agent coal ratio JK10 of hydrogen supply agent weight and coal dust weight is 0.5~2.0；
In rear conversion zone RUB, ratio, that is, agent coal ratio JK20 of hydrogen supply agent weight and coal dust weight is 0.5~2.0.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.30~0.95 of the agent coal ratio JK10 of preceding conversion zone RUA.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.45~0.80 of the agent coal ratio JK10 of preceding conversion zone RUA.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.50~0.70 of the agent coal ratio JK10 of preceding conversion zone RUA.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, into hydrocarbon powder Adding hydrogen direct liquefaction reaction process RU to participate in hydrocarbon ils at least part of direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply At least part of solvent DS is used as the solvent for preparing coal slurry；
The ratio of the weight flow rate KS-W of the weight flow rate DS-W and coal dust KS of hydrogen supply dissolvent DS are agent coal ratio K100= (DS-W)/(KS-W), K100 are 0.5~2.0.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, into hydrocarbon powder Adding hydrogen direct liquefaction reaction process RU to participate in hydrocarbon ils at least part of direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply At least part of solvent DS is used as the solvent for preparing coal slurry；
Hydrogen supply dissolvent DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, and the weight of part saturation aromatic hydrocarbons contains It is 0.35~0.70 that amount, which is greater than 15%, aromatic carbon rate,.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, into hydrocarbon powder Adding hydrogen direct liquefaction reaction process RU to participate in hydrocarbon ils at least part of direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply At least part of solvent DS is used as the solvent for preparing coal slurry；
Hydrogen supply dissolvent DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, and the weight of part saturation aromatic hydrocarbons contains It is 0.45~0.60 that amount, which is greater than 25%, aromatic carbon rate,.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, the coal hydrogenation used Direct liquefaction catalyst is a kind of composite hydrogenation catalyst, includes high-activity component and low activity component；The high activity group It is 1: 10 to 10: 1 that parting, which belongs to the weight ratio of low activity component metals,；The high-activity component is the water soluble salt chemical combination of molybdenum Or mixtures thereof object；The low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, direct hydrogenation liquefaction of coal catalyst water content are lower than 2wt%；Direct hydrogenation liquefaction of coal catalyst particle diameter be 1~ 100 μm of powdered granule.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, the coal hydrogenation used Direct liquefaction catalyst be nanometer ultra-fine grain aqua oxidation iron catalyst and/or iron oxide and/or pyrite and/or bloodstone and Or molybdenum oxide and/or molybdenum sulfide and/or ammonium molybdate and/or nickel sulfide.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, into hydrocarbon powder Adding hydrogen direct liquefaction reaction process RU to participate in hydrocarbon ils at least part of direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS.
Mode of operation of the invention may is that
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C is used Hydrocarbon TO-RU-DS；
Hydrogen supply hydrocarbon TO-RU-DS, the external hydrogen supply including the hydrogen supply hydrocarbon SH for being 230~400 DEG C containing normal boiling point may be used Hydrocarbon OUT-TO-RU-DS, including recycle hydrocarbons MR-KRDS；
The weight flow rate heavy oil RU-F1L-W of the weight flow rate TO-RU-DS-W and heavy oil RU-F1L of hydrogen supply hydrocarbon TO-RU-DS Ratio be oil ratio KP80, KP80=(TO-RU-DS-W)/(RU-F1L-W), KP70 be 0.05~1.0.
Mode of operation of the invention may is that
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
It is converted in the heavy hydrocarbon HNBPC heat from hydrogenation cracking reaction of hydrocarbon material hydrogenation process RU, front reaction zone RUA Rate is selected from one of the following or several:
1. heat from hydrogenation cracking reaction conversion ratio is lower than 20% stage of reaction；
2. heat from hydrogenation cracking reaction conversion ratio is lower than 35% stage of reaction；
3. heat from hydrogenation cracking reaction conversion ratio is lower than 50% stage of reaction.
Mode of operation of the invention may is that
(4) in separation and recovery process SYS700, separation process MRP-S is set, stabilized hydrogenation reaction product MRP is separated into point From gas MRP-V and separating liquid MRP-L；
The whereabouts of gas MRP-V is separated, one of the following or several is selected from:
1. at least part hydrogen rich gas gas MRP-V becomes cold anticyclone and separates gas MRP-V- after cooling and dewatering, de-oiling CHPS-V, at least part MRP-V-CHPS-V use return direct hydrogenation liquefaction of coal reaction process RU to use as recycle hydrogen；
2. at least part hydrogen rich gas gas MRP-V becomes cold anticyclone and separates gas MRP-V- after cooling and dewatering, de-oiling CHPS-V, at least part MRP-V-CHPS-V deviate from least part non-hydrogen gas by hydrogen purification process HUPSYS, Obtain high-purity hydrogen MRP-V-CHPS-V-PH；At least part high-purity hydrogen MRP-V-CHPS-V-PH makes as recycle hydrogen It is used with direct hydrogenation liquefaction of coal reaction process RU is returned；
3. at least part hydrogen rich gas gas MRP-V becomes warm high pressure and separates gas MRP-V- after cooling and dewatering, de-oiling KMHPS-V, the warm high pressure separation gas MRP-V-KMHPS-V gravity flow of at least part is into direct hydrogenation liquefaction of coal reaction process RU's The secondary use of the lower reaction zone of operating pressure；
4. at least part hydrogen rich gas gas MRP-V, gravity flow enters the operation pressure of direct hydrogenation liquefaction of coal reaction process RU The secondary use of the lower reaction zone of power；
5. at least part hydrogen rich gas gas MRP-V, into the removal process of rear portion reaction zone RUB product.
Mode of operation of the invention may is that
(1) in hydrocarbon material hydrogenation process RU, the removal process of front reaction zone RUA product, with rear portion reaction zone RUB The removal process of product partly or entirely shares.
Mode of operation of the invention may is that
(1) in hydrocarbon material hydrogenation process RU, the removal process of the gaseous product of front reaction zone RUA is anti-with rear portion The removal process of the gaseous product of area RUB is answered, is partly or entirely shared.
Mode of operation of the invention may is that
(1) in hydrocarbon material hydrogenation process RU, the removal process of the liquid material product of front reaction zone RUA is anti-with rear portion The removal process of the liquid material product of area RUB is answered, is partly or entirely shared.
Mode of operation of the invention may is that
(1) in hydrocarbon material hydrogenation process RU, the removal process of the product slurry of front reaction zone RUA is anti-with rear portion The removal process of the product slurry of area RUB is answered, is partly or entirely shared.
Mode of operation of the invention may is that
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply being mainly made of the hydro carbons that normal boiling point is 230~530 DEG C is used Hydrocarbon TO-RU-DS；
The hydrogen supply hydrocarbon TO-RU-DS of 50 weight % or more, is provided by recycle hydrocarbons MR-KRDS；
In hydrocarbon material front hydrogenation process RUA, using being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C Hydrogen supply hydrocarbon TO-RUA-DS；
The hydrogen supply hydrocarbon TO-RUA-DS of 50 weight % or more, is provided by recycle hydrocarbons MR-KRDS.
Mode of operation of the invention may is that
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply being mainly made of the hydro carbons that normal boiling point is 230~530 DEG C is used Hydrocarbon TO-RU-DS；
In hydrocarbon material front hydrogenation process RUA, using being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C Hydrogen supply hydrocarbon TO-RUA-DS；
The hydrogen supply hydrocarbon TO-RUA-DS of 100 weight %, is provided by recycle hydrocarbons MR-KRDS.
Detailed description of the invention
Below in conjunction with the flow chart of some detailed process types of direct hydrogenation liquefaction of coal reaction process, to describe this hair Bright, still, it cannot limit application field and Process flow of the invention.
The present invention, one conversion zone contain at least one direct hydrogenation liquefaction of coal reaction step and separate the reaction Step gas-liquid product obtain at least one volume in the gassiness material being mainly made of gas phase and at least one volume mainly by The step of material containing liquid of liquid material composition；In the reaction step of one conversion zone, 1 reactor can be used only, 2 or more reactors can be used in series；Whether there is gas-liquid separating function according to reactor, gas may be used in conversion zone Liquid/gas separator does not use gas-liquid separator.
Direct hydrogenation liquefaction of coal reaction process RU of the present invention, the work side of the direct hydrogenation liquefaction of coal reactor assembly used Formula and structure type, at least can a kind or several in the following option:
Option 1, liquid material and gas material use the counter-current reactor of pure adverse current working method；
Option 2, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump Answer the fluidized bed reactor of device XRUE material inlet；
Option 3, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump Answer the suspended-bed reactor of device XRUE material inlet；
Option 4, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of device XRUE material inlet is answered, while circulating pump conveys circulation fluid, downstream transport liquid material product；
Option 5, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of device XRUE material inlet is answered, while circulating pump conveys circulation fluid, downstream transport liquid material product；
Option 6, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor for answering device XRUE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；
Option 7, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor for answering device XRUE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；
Option 8, reactor XRUE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport liquid Expect product, is not provided with the fluidized bed reactor system of liquid material product forced circulation；
Option 9, reactor XRUE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport liquid Expect product, is not provided with the suspended-bed reactor system of liquid material product forced circulation；
Option 10, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspension bed of reactor XRUE material inlet and the combination type reactor of ebullated bed；
Option 11, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspension bed of reactor XRUE material inlet and the combination type reactor of ebullated bed, while circulating pump conveys circulation fluid, downwards Trip conveying liquid material product；
Option 12, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspension bed of reactor XRUE material inlet and the combination type reactor of ebullated bed are collected simultaneously other collection liquids warp of cup discharge Cross other dedicated feeding engine downstream transport liquid material products；
The suspended-bed reactor system of flow pattern under the center upstream surrounding of internal guide cylinder is arranged in option 13；
The suspended-bed reactor system of flow pattern in the dirty surrounding in center of internal guide cylinder is arranged in option 14；
Option 15, empty cylinder bubbling bed suspended-bed reactor system；
Option 16 is formed reactor top reaction zone liquid phase and is flowed down under Returning reactor using the external circulation pipe of reactor The device outside circulation of portion's reaction zone；
Option 17, the collection liquid of the top setting liquid collecting cup with 2 upper reaction zones are forced after being pressurizeed by circulating pump It is recycled back into the combination type reactor of the ebullated bed of reactor XRUE material inlet；
Option 18, the collection liquid of the top setting liquid collecting cup with 2 upper reaction zones are forced after being pressurizeed by circulating pump It is recycled back into the combination type reactor of the suspension bed of reactor XRUE material inlet；
Option 19, the collection liquid of the top setting liquid collecting cup with 2 upper reaction zones are forced after being pressurizeed by circulating pump It is recycled back into the suspension bed of reactor XRUE material inlet and the combination type reactor of ebullated bed.
For direct hydrogenation liquefaction of coal reaction process RU, since the counter-current reactor of pure adverse current working method inherently has Have to the heating of light component, air lift effect in raw material coal slurry, it is therefore, pure inverse the invention is particularly suited to be used with liquid material with gas material The counter-current reactor of stream working method is applied in combination.
For direct hydrogenation liquefaction of coal reaction process RU, since the counter-current reactor of pure adverse current working method is inherently simultaneous There are reactor, gas-liquid separator function, therefore, 1 pure counter-current reactor can constitute a complete conversion zone.
The direct hydrogenation liquefaction of coal reaction process of the known hydrogenator operated using gas-liquid counter current, is had using pure inverse The Pyrosol technique of flow reactor, the technique are developed by German coal liquefaction company GFK, are two sections of coal liquefaction crafts, and first segment is Coal Liquefaction, second segment be liquefied residue plus hydrogen coking, process and technical description be shown in document A01: 1. publication title: " coal direct liquefaction ", page 121 to page 124；2. retrieval is encoded with books: ISBN 978-7-122-02151-9；3. writing: Wu Spring；4. publishing house: Chemical Industry Press
The purpose of direct hydrogenation liquefaction of coal reaction process RU of the present invention, core be in the reaction mechanism mechanism of reaction coal gradually liquefy turn Become liquid oil, it is therefore, positive on the basis of the bulk flow direction of coal dust or coal slurry.In this way, straight in 1 pure adverse current coal hydrogenation It connects in liquefying reactor, hydrogen bulk flow direction belongs to reverse flow, and slurries flow from up to down belongs to forward flow, slurries The front half section of flow process belongs to preceding conversion zone, and the second half section of slurries flow process belongs to rear conversion zone.Similarly, pure inverse at 2 Flow direct hydrogenation liquefaction of coal reactor group at 2 sections of reaction process in, first reactor from middle and upper part receive coal slurry, first reaction The flowing that the slurries of device bottom discharge enter second reactor middle and upper part belongs to forward flow, and second reactor is received from middle and lower part Hydrogen feed, the flowing that the gas of second reactor top discharge enters first reactor middle and lower part belong to reverse flow, and first Reactor belongs to preceding conversion zone, and second reactor belongs to rear conversion zone.
About Pyrosol technique, it is presently believed that the core process with substantial worth of its disclosed counter-current reactor One of feature is exactly that the vaporization of low boiling hydrocarbon possessed by counter-current reactor top feed coal slurry and hot hydrogen counter-current operation is de- in fact From this function of reaction process, he can prevent low boiling point hydrogen supply dissolvent from excessive thermal cracking occurring in reaction process longer-term persistence Reaction, but the use value of this function is not discovered, because the air lift vaporization function of simple pure adverse current leads to the work Skill is not almost available the hydrogen supply dissolvent for the middle matter hydro carbons that conventional boiling range is 230~350 DEG C, although these hydrogen supply dissolvent components are logical It is often the aromatic hydrocarbons such as naphthane or tetrahydro naphthalene series substance of the fractional saturation of twin nuclei, is to carry the high rationality hydrogen supply dissolvent group of hydrogen amount Point；And appearance of the invention, the drawbacks described above of pure counter-current reactor can be made up, to carry out technological improvement to it.
Liquid collecting cup is set for direct hydrogenation liquefaction of coal reaction process, in reactor and collection liquid is made to pass through circulating pump and is pressurizeed The product liquid forced cyclic type suspension bed Coal liquefaction system for forming Liquid product recycle operation is currently the only to be advised greatly The direct hydrogenation liquefaction of coal reactor of mould commercial plant successful application, while it has a unique advantage, that is, it utilizes The density contrast of liquid material and gas phase forms the relative separation of liquid material and gas phase in reactor head, therefore, 1 this reactor Also a complete conversion zone can be constituted, only its product slurry contains a small amount of bubble, and top product is gas-liquid mixed phase material, The slurries that most of such as 80~90% can of course be controlled enter product slurry, so that top gas-liquid product be made only to contain slurries The 10~20% of product；Since the material walked between multiple conversion zones is not final products, gas material entrainment is certain It is acceptable that the liquid material or liquid material of quantity, which carry a certain number of gas material secretly, gas entrainment liquid material and be entrained liquid material can be with What can be regarded when being recycled back into recycles as additional liquid material, and liquid material carries a certain number of gas material secretly and is entrained gas material and can recycle What can be regarded when return recycles as additional gas material, as long as stable operation, so that it may the high pressure hot separator between reactor is saved, So as to create conditions to construct new process.
For direct hydrogenation liquefaction of coal reaction process, the final production of other reactor discharges without gas-liquid separating function Product are gas-liquid mixed phase material, it usually needs using the knockout drum with gas-liquid separating function, are by gas-liquid mixed phase feed separation Gas, liquid material are separately recovered；The knockout drum of final reacting product should use clear knockout drum, it is often desirable that gaseous product Solid is not contained as far as possible, it is desirable to liquid material product not bubbles as far as possible.
It can be seen from the above description that since final gas can not be carried out in reactor of the gas and liquid flowing by reaction compartment The clear dedirt of phase product, de- liquid function you must use 1 gas-liquid separator with clear dedirt, de- liquid function.Make With the necessity and effect of front end gas-liquid separator, rear end gas-liquid separator totally 2 gas-liquid separators, set application is of the invention Set in the direct hydrogenation liquefaction of coal reaction process that the hydrogen counter flow series of 2 conversion zones utilize, performance it is more intuitive, it is also Closest to the simplest near-sighted operating process of pure counter-current reactor.
For direct hydrogenation liquefaction of coal reaction method of the present invention, it is related to various possible Process flows, for example react Process includes 1 or 2 or multiple conversion zones.
Direct hydrogenation liquefaction of coal reaction method of the present invention, can contain at least two or multiple conversion zones, wherein conversion zone it Between there are the series flow of slurries, be forward direction with flowing of the slurries between conversion zone, the flowing of hydrogen material between conversion zone Mode at least can choose a kind or several of following manner:
1. the gas and liquid flowing tandem reactor process of liquid material series connection, hydrogen fair current；
2. liquid material series connection, tandem reactor process of the hydrogen short circuit across stream；
3. the reaction process of liquid material series connection, hydrogen parallel operation；
4. liquid material series connection, the reaction process for having hydrogen counter-current operation step.
For direct hydrogenation liquefaction of coal reaction process RU, the mode of product slurry is discharged in final reaction section, at least can be with Select a kind or several of following manner:
1. being discharged from the gas-liquid separation process of final reaction section reaction product, usually it is discharged from high pressure hot separator lower part；
2. being discharged from the final reactor of final reaction section, for example it is discharged from pure counter-current reactor bottom liquid phase region, than As the liquid collecting cup in autoreactor is discharged through diversion pipe；Product slurry, can be by cyclonic separation step abjection at least portion Become primary degassing product slurry after dividing bubble, can be produced after degassing tank deviates from over-saturation bubble as primary degassing slurries Object, the primary product slurry that deaerates go recovery system after being used as the decompression of final product slurry.
The present invention mostly can prepare slurry using the stabilized hydrogenation conversion product of recycle hydrocarbons MKDS under conditions of license MKDS-MJ, to reduce the quantity of systemic circulation circuit hydrogen supply dissolvent oil；Although it is an object of the present invention to be recycled containing conventional Boiling point is the MR-KRDS of 230~400 DEG C of the hydrocarbon components, still, allows circulation logistics to contain conventional boiling range lighter lower than 230 DEG C Hydro carbons, conventional boiling range be higher than 400 DEG C of heavier hydro carbons.
According to the variation of detailed process operating condition, most of hydro carbons in recycle hydrocarbons MR-KRDS, can selected from it is following often Advise a kind or several in boiling range:
1. the conventional liquid hydrocarbon that normal boiling point is 230~400 DEG C；
2. the conventional liquid hydrocarbon that normal boiling point is 230~350 DEG C；
3. the conventional liquid hydrocarbon that normal boiling point is 230~300 DEG C.
It can be seen that from the above operation target and realize that the object of the invention mode is at least following several:
Hydrocarbon powder is gone to add hydrogen direct liquefaction reaction process in return course TLOOP, at least part recycle hydrocarbons MR-KRDS RU contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react, and working method is selected from one of the following or several:
1, at least part recycle hydrocarbons MR-KRDS are selected, the front that gravity flow returns to direct hydrogenation liquefaction of coal reaction process is anti- Section is answered, contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
2, at least part recycle hydrocarbons MR-KRDS are selected, the front conversion zone of direct hydrogenation liquefaction of coal reaction process is returned Contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
3, at least part recycle hydrocarbons MR-KRDS is selected to return to direct hydrogenation liquefaction of coal reaction process after heat exchange heating Front conversion zone, contact slurry carry out hydrocarbon powder and hydrogen direct liquefaction are added to react；
Selection 4, at least part recycle hydrocarbons MR-KRDS are used as coal slurry and prepare solvent naphtha configuration coal slurry MKDS-MJ, then coal Slurry MKDS-MJ enters direct hydrogenation liquefaction of coal reaction process, carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
Selection 5, at least part recycle hydrocarbons MR-KRDS are used as coal slurry and prepare solvent naphtha configuration coal slurry MKDS-MJ, then coal Slurry MKDS-MJ enters the front conversion zone of direct hydrogenation liquefaction of coal reaction process, carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
6, at least part recycle hydrocarbons MR-KRDS are selected, in washing step DW, the washing oil as gas RUA-PS-V makes To wash the dust in abjection gas RUA-PS-V；While completing to wash dedirt, by the part in gas RUA-PS-V Hydro carbons is condensed into liquid phase DWL；
At least part liquid phase DWL returns to direct hydrogenation liquefaction of coal reaction process, and contact slurry carries out hydrocarbon powder and adds hydrogen Direct liquefaction reaction；
7, at least part recycle hydrocarbons MR-KRDS are selected, in washing step DW, the washing oil as gas RUA-PS-V makes To wash the dust in abjection gas RUA-PS-V；While completing to wash dedirt, by the part in gas RUA-PS-V Hydro carbons is condensed into liquid phase DWL；
At least part liquid phase DWL returns to the front conversion zone of direct hydrogenation liquefaction of coal reaction process, and contact slurry carries out Hydrocarbon powder adds hydrogen direct liquefaction to react；
8, at least part liquid phase DWL are selected, direct hydrogenation liquefaction of coal reaction process contact slurry is returned and carries out hydrocarbon powder Before material plus the reaction of hydrogen direct liquefaction, it is used as Conduit rinse oil or pump flushing oil or instrument flushing oil.
For middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention stabilized hydrogenation object reuse method and Speech, in order to improve reflux liquid yield, can be set stripping step BH-S air lift reaction product slurries；Realize middle matter hydrocarbon group in slurry Divide the mode of vaporization unrestricted, there are many concrete mode, according to the source type of corresponding gas stripping gas material BH, can at least select 1 kind or several for selecting following materials:
1. the new hydrogen that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
2. the circulating hydrogen that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
3. the circulating hydrogen after the hydrogen upgrading that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
4. adding in hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the front reaction zone of product slurry RUA-LP is discharged The hydrogen rich gas material of the reaction zone discharge in downstream or its derivative gas；
5. hydrocarbon powder adds the reaction of the matched hydrogen supply dissolvent stabilized hydrogenation reaction process of hydrogen direct liquefaction reaction process RU The hydrogen rich gas gas or its derivative gas that product is isolated；
6. hydrocarbon powder adds the matched hydrocarbon powder liquefaction oil of hydrogen direct liquefaction reaction process RU to add hydrogen upgrading reaction process The hydrogen rich gas gas isolated of reaction product or its derive gas.
When using air lift hydrogen, the present invention form it is a kind of comprising catalysis reaction step and middle fraction solvent naphtha air lift, Stabilized hydrogenation, condensation, reflow step " catalytic process and high pressure separation " integrated technique, middle matter hydrogen supply dissolvent can be given full play to Hydrogen supply capacity reduces long circulating circuit hydrogen supply dissolvent dosage, improves process economics.
The present invention, compared with the direct hydrogenation liquefaction of coal reaction process of routine techniques, process complexity be increased, but It is that can be effectively reduced long circulating circuit hydrogen supply dissolvent oil quantity, reduce the rule that coal liquefaction generates oil separation abjection solid process Mould.
The present invention is condensing and separating process MRP-S, and stabilized hydrogenation reaction product MRP is separated into separation gas MRP-V and contains The separating liquid MRP-L for the hydrogen supply the hydrocarbon component MR-DS that normal boiling point is 230~400 DEG C separates the whereabouts of gas MRP-V, selected from following One or more of:
1. at least part separation gas MRP-V becomes cold anticyclone and separates gas MRP-V-CHPS-V after cooling and dewatering, de-oiling, At least part MRP-V-CHPS-V uses return direct hydrogenation liquefaction of coal reaction process RU to use as recycle hydrogen；
2. at least part separation gas MRP-V becomes cold anticyclone and separates gas MRP-V-CHPS-V after cooling and dewatering, de-oiling, At least part MRP-V-CHPS-V deviates from least part non-hydrogen gas by hydrogen purification process RUA-HUPSYS, obtains High-purity hydrogen MRP-V-CHPS-V-PH；At least part high-purity hydrogen MRP-V-CHPS-V-PH is used as recycle hydrogen to be returned Direct hydrogenation liquefaction of coal reaction process RU is returned to use；
3. at least part separation gas MRP-V becomes warm high pressure and separates gas MRP-V-KMHPS-V after cooling and dewatering, de-oiling, The warm high pressure separation gas MRP-V-KMHPS-V gravity flow of at least part enters the operating pressure of direct hydrogenation liquefaction of coal reaction process RU The lower secondary use of reaction zone；
4. at least part separation gas MRP-V, gravity flow into direct hydrogenation liquefaction of coal reaction process RU operating pressure compared with The secondary use of low reaction zone.
For the present invention, for 2 sections of reaction process, even if 1 reactor is used only in every section of reaction process, then only 2 The combination of the different structure form of platform reactor, at least more than 100 kinds, therefore, using the method for exhaustion enumerate it is of the invention can Energy Process flow, then concrete form is too many.
For the present invention, for 3 sections of reaction process, even if 1 reactor is used only in every section of reaction process, then only 3 Therefore the combination of the different structure form of platform reactor, at least more than 1000 kinds enumerate possibility stream of the invention using the method for exhaustion Journey form, then concrete form is too many, it is virtually impossible to all descriptions.
For the present invention, for 4 sections of reaction process, even if 1 reactor is used only in every section of reaction process, then only 4 Therefore the combination of the different structure form of platform reactor, at least more than 10000 kinds enumerate possibility of the invention using the method for exhaustion Process flow, then concrete form is too many, can not all describe.
For the present invention, for the Process flow more than 4 sections of reaction process, its possible process is enumerated using the method for exhaustion Form, then concrete form is even more too many, can not all describe.
If it is considered that increase important additional process feature on the basis of above-mentioned main flow, such as at least partly gaseous product It crosses adjacent upper section conversion zone and countercurrently enters more upstream conversion zone, such as a certain downstream reaction section gassiness of multistage reaction process produces Object independently recycles and is not involved in the operation of hydrogen counter flow series, and such as at least partly liquid material product is crossed adjacent downstream conversion zone and bypassed Upstream reaction section circulation behaviour is returned into further downstream conversion zone, such as a certain downstream reaction section liquid material product of multistage reaction process Make, etc., then its possible Process flow is enumerated using the method for exhaustion, then concrete form is even more too many, can not all describe.
Therefore, the combination that the present invention is described using process concept verbal description and typical process flow diagram, as far as possible Technological principle of the invention, process structure principle are comprehensively expressed, and then describes base of the invention with broad concept language This technological principle, process construct basic principle；According to these principles, any appropriate technical application form can be constructed, to the greatest extent Them are managed without all directly descriptions in the description of the present invention, but has made description in implicit manner.
Fig. 1 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention Principle process schematic diagram.
As shown in Figure 1, the front conversion zone comprising coal process for preparation M10, direct hydrogenation liquefaction of coal reaction process RU RUA, front conversion zone RUA product RUAP thermal high separation process RUAP-HS, direct hydrogenation liquefaction of coal reaction process RU after Portion conversion zone RUB, the thermal high separation process RUBP-HS of rear portion conversion zone RUB product RUBP, hot high score gas RUAP-HS-V take Stabilized hydrogenation with hydrocarbon obtain the process MR-UNIT of the i.e. SR-DS of recycle hydrocarbons MR-KRDS, hot high score oil RUBP-HS-L separation/ Fractionating section RUBP-HS-L-DTS, hot high score gas RUBP-HS-V post processing system RUBP-HS-V-GUNIT, stabilized hydrogenation mistake Post processing system RUAP-HS-V-AUNIT, the long process circulation solvent hydrogenation modification of the hydrogen-rich gas of journey MR-UNIT discharge are anti- Answer separation/fractionating section LR- of process R20, R20 product thermal high separation process R20P-HS, hot high score oil R20P-HS-L DSF。
As shown in Figure 1, different from conventional direct hydrogenation liquefaction of coal technique, the present invention is provided with hot high score gas RUAP-HS- The stabilized hydrogenation process MR-UNIT of V obtains short route recycle hydrocarbons MR-KRDS.
As shown in Figure 1, the precursor hydro carbons R20F of long process hydrogen supply dissolvent LR-DS, enters solvent oil hydrogenation through pipeline 151 Stablize reaction process R20, it is full that aromatic hydrogenation part occurs under hydrogen, long process solvent oil hydrogenation rugged catalyst existence condition And reaction, it is converted into the product R20P rich in hydrogen supply hydrocarbon, separation product R20P obtains the hydrocarbon liquid logistics LS-DS rich in hydrogen supply hydrocarbon, It is used as the coal dust SF solvent naphtha for preparing coal.
As shown in Figure 1, as needed, circulation raffinate VSR enters coal process for preparation M10, supplying oil through pipeline 1451 In coal slurry RUF.
As shown in Figure 1, solvent oil hydrogenation reaction product R20P, enters thermal high separation process R20P-HS points through pipeline 155 From for hot high score gas R20P-HS-V and hot high score oil R20P-HS-L.
R20P-HS-V includes most of hydrogen, part low boiling hydrocarbon in R20P, and there are many ways of recycling of R20P-HS-V, It can be the hydrogen-rich gas for being separated into hydrocarbon ils and recycling.
When the pressure of R20P-HS-V is higher than the operating pressure of direct hydrogenation liquefaction of coal reaction process RU, at least part Hot high score gas R20P-HS-V can be by secondary use.As shown in Figure 1, entering direct hydrogenation liquefaction of coal reaction process through pipeline 165 RU adds such as the entrance hydrogen of the front reactor of direct hydrogenation liquefaction of coal reaction process RU, the entrance of rear portion reactor Hydrogenation, the hydrogen that cools, flushing hydrogen, air lift hydrogen such as direct hydrogenation liquefaction of coal reaction process RU；It is remaining Hot high score gas R20P-HS-V, can be used as hot high score process RUAP-HS gas stripping gas use, or with the gas gas-phase objects based on RU product Flow mixed processing.
As shown in Figure 1, hot high score oil R20P-HS-L includes part low boiling hydrocarbon in R20P, most of high boiling hydrocarbon, lead to Often, the hot high score oil R20P-HS-L of at least part enters separation/fractionating section LR-DSF abjection low boiling component through pipeline 166 After isolate long process circulation hydrogen supply dissolvent LR-DS.
As shown in Figure 1, long process recycles hydrogen supply dissolvent LR-DS, solvent naphtha LR- with slurry can be used as through pipeline 175,1751 DS-TO-RUA enters coal process for preparation M10, and coal dust SF enters coal process for preparation M10 through pipeline 101, what M10 was obtained Raw material RUF of the coal as direct hydrogenation liquefaction of coal reaction process RU such as front conversion zone feeds coal slurry RUAF；As needed, In coal process for preparation M10, direct hydrogenation liquefaction of coal catalyst, vulcanizing agent etc. can be incorporated in coal RUF.
As shown in Figure 1, whole coal RUAF rich in hydrogen supply hydrocarbon were reacted through pipeline 111 into direct hydrogenation liquefaction of coal In the front conversion zone RUA of journey RU, hydrogen, direct hydrogenation liquefaction of coal catalyst existence condition issue the swelling of soft coal, pyrolysis, It is hydrocracked, the coal liquefactions hydrogenation reaction such as stabilized hydrogenation, while raffinate VSR's that may be present plus hydrogen saturation occurs plus hydrogen is de- The reaction such as impurity hydrogenolysis, heat from hydrogenation cracking, hydrogen supply dissolvent DS play hydrogen supply effect, and the dehydrogenation product of hydrogen supply hydrocarbon can be turned with repeated hydrogenation Hydrogen supply hydrocarbon repetition hydrogen supply is turned to play a part of transmitting reactive hydrogen.
As shown in Figure 1, whole coal RUAF enters direct hydrogenation liquefaction of coal front conversion zone RUA, to be converted into coal hydrogenation straight It meets liquefaction front conversion zone product RUAP, product RUAP and is separated into hot height into thermal high separation process RUAP-HS through pipeline 121 Divide gas RUAP-HS-V and hot high score oil RUAP-HS-L.
As shown in Figure 1, the RUAP-HS-V that pipeline 131 conveys includes most of hydrogen, part low boiling hydrocarbon, heat in RUAP High score gas RUAP-HS-V recycles hydrogen supply dissolvent hydrogenation modification process MR-UNIT by short route, and it is molten to generate short route circulation hydrogen supply Agent SR-DS and hydrogen-rich gas XH.
As shown in Figure 1, hydrogen-rich gas XH enters post processing system RUAP-HS-V-AUNIT, separation and recovery through pipeline 341 Hydrogen-rich gas XH obtains hydrogen-rich gas XHV, usually also obtains the hydrocarbon ils XHL being discharged through pipeline 196.
Post processing system RUAP-HS-V-AUNIT, cooling, water filling washing, gas typically at least including hydrogen-rich gas XH The processes such as liquid separation or gas and oil water three phase separation, the purpose is to the hydrogen-rich gases for obtaining to be recycled and recycling hydrogen-rich gas The operation temperature of hydro carbons in XH, the gas-liquid separation or gas and oil water three phase separation process: it is usually 10~80 DEG C, is generally 20~70 DEG C, preferably 30~55 DEG C.
It is recycled in general, at least part hydrogen-rich gas XHV returns to hydrogenation process, as shown in Figure 1, a part of hydrogen rich gas Body XHV can return to direct hydrogenation liquefaction of coal front conversion zone RUA by pipeline 195 as RH-TO-RUA and be recycled, a part Hydrogen-rich gas XHV can be used as RH-TO-R20 can enter the stable reaction process R20 use of solvent oil hydrogenation by pipeline 196,
As shown in Figure 1, new hydrogen FH is conveyed through pipeline 250, RUA-HF can enter the direct liquid of coal hydrogenation by pipeline 251 all the way Change front conversion zone RUA and be used as the uses such as chemistry consumption hydrogen, after RUB-HF can enter direct hydrogenation liquefaction of coal by pipeline 253 all the way Portion conversion zone RUB is used as chemistry consumption hydrogen etc. and uses, and R20-HF can enter circulation solvent hydrogenation modification reaction by pipeline 252 all the way Process R20 is used as chemistry consumption hydrogen etc. and uses.
As shown in Figure 1, hot high score oil RUAP-HS-L is after pipeline 132 enters direct hydrogenation liquefaction of coal reaction process RU In portion conversion zone RUB, soft coal liquefaction hydrogenation reaction is issued in hydrogen, direct hydrogenation liquefaction of coal catalyst existence condition, hydrogen supply is molten Agent DS plays hydrogen supply effect, and the dehydrogenation product of hydrogen supply hydrocarbon can be converted into hydrogen supply hydrocarbon repetition hydrogen supply with repeated hydrogenation and play transmitting activity The effect of hydrogen.
As shown in Figure 1, rear portion conversion zone RUB is converted into direct hydrogenation liquefaction of coal rear portion conversion zone product RUBP, product RUBP is separated into hot high score gas RUBP-HS-V and hot high score oil RUBP- into thermal high separation process RUBP-HS through pipeline 1401 HS-L。
As shown in Figure 1, the RUBP-HS-V that pipeline 1403 conveys includes most of hydrogen, part low boiling hydrocarbon, heat in RUBP High score gas RUBP-HS-V enters post processing system RUBP-HS-V-GUNIT, separates and recovers hot high score gas RUBP-HS-V and obtains Hydrogen-rich gas RUB-XHV usually also obtains the hydrocarbon ils RUB-XHL being discharged through pipeline 1415.
Post processing system RUBP-HS-V-GUNIT, cooling, water filling typically at least including hydrogen-rich gas RUBP-HS-V The processes such as washing, gas-liquid separation or gas and oil water three phase separation, the purpose is to the hydrogen-rich gas for obtaining to be recycled and recycling The operation temperature of hydro carbons in hydrogen-rich gas, the gas-liquid separation or gas and oil water three phase separation process: usually 10~80 DEG C, Generally 20~70 DEG C, preferably 30~55 DEG C.
It is recycled in general, at least part hydrogen-rich gas RUB-XHV returns to hydrogenation process RU such as rear portion conversion zone RUB, As shown in Figure 1, at least part hydrogen-rich gas RUB-XHV can be used as RH-TO-RUB can by pipeline 1411 return rear portion it is anti- Answer section RUB to be recycled, as needed, at least part hydrogen-rich gas RUB-XHV can enter front conversion zone RUA use or Stablize reaction process R20 into solvent oil hydrogenation to use.
As needed, post processing system RUBP-HS-V-GUNIT, post processing system RUAP-HS-V-AUNIT, can be with Partly or entirely share.
As shown in Figure 1, hot high score oil RUBP-HS-L enters separation/fractionation of hot high score oil RUBP-HS-L through pipeline 1408 Part RUBP-HS-L-DTS isolates gas, liquefaction products distillate ML, liquefied residue VS.
In general, partial liquefaction product frac oil ML enters down stream processing steps, part liquid through pipeline 148 as product TP1 Biology R20F-A is through the stable reaction process of the entrance solvent oil hydrogenation of pipeline 143 before change product frac oil ML can be used as hydrogen supply agent In R20 and/or MR-UNIT.
As shown in Figure 1, having in general, partial liquefaction residue VS enters down stream processing steps through pipeline 1452 as product VSP The effect of solid waste is discharged, as needed, partial liquefaction residue VS enters oily coal through pipeline 1451 as circulation raffinate VSR Process for preparation M10 is starched, is incorporated in coal RUF.
Direct hydrogenation liquefaction of coal reaction process RU generates direct hydrogenation liquefaction of coal and generates oil RUP-O, in general, in hot high score oil The tower bottom for the vacuum distillation tower that the separate section RUBP-HS-L-DTS of RUBP-HS-L is used obtains mainly being higher than by normal boiling point VACUUM TOWER BOTTOM material containing solid-liquid VS, that is, raffinate of the present invention of 500~540 DEG C of the hydrocarbon component and solid composition, most techniques are by portion Point VACUUM TOWER BOTTOM material containing solid-liquid VS returns to direct hydrogenation liquefaction of coal reaction process RU as cycle stock VSR so that portion is used repeatedly Divided catalyst particle, deep conversion part heavy hydrocarbon (colloid, asphaltene, preasphaltene), while discharge part VACUUM TOWER BOTTOM contains Solid-liquid material VS be discharged as raffinate product VSP spent catalyst particles, can not liquefied coal skeleton particle, while in raffinate VS Entrainment of heavy hydrocarbon such as oil, colloid, asphaltene, preasphaltene, the softening point of raffinate VS is usually above 100~150 DEG C.
The circulation raffinate VSR of direct hydrogenation liquefaction of coal reaction process RU is returned to, because containing can not liquefied dead catalyst Particle, can not liquefied coal skeleton particle, while carry secretly part heavy hydrocarbon be difficult to plus hydrogen lighting polycyclic aromatic hydrocarbon, glue Matter, asphaltene, preasphaltene, therefore the presence of cycle stock VSR, although can recovery section oil product, be significantly degrading coal The operating condition for adding hydrogen direct liquefaction reaction process RU and its related system shortens the continuous operation period, limits or have compressed Raw material coal range (mainly proposes upper limit requirement to the content of ashes of fine coal and inertinite content).
As shown in Figure 1, the present invention forms the short circuit current journey of direct hydrogenation liquefaction of coal reaction process light solvent oil.
Solvent oil hydrogenation stablizes reaction process R20, can process the distillate R20F-A from pipeline 143, can process Such as warm high score separation process of the suitable distillate R20F-B of the boiling range conveyed through pipeline 1415 of RUBP-HS-V-GUNIT discharge obtains The warm high score oil arrived, can also process other suitable distillates.
Solvent oil hydrogenation stablizes reaction process R20, can process 2 or multiple hydrogen supply hydrocarbon precursors, can be using mixing The synchronization of raw material hydrocarbon adds hydrogen mode.
Solvent oil hydrogenation stablizes reaction process R20, and the boiling range of 2 hydrogen supply hydrocarbon precursors of processing, molecular structure may When differing greatly, this 2 road hydrocarbon stream can be using nonsynchronous plus hydrogen mode, for example can be distillate R20F-A by pre-add Pre- hydrogenation products obtained by hydrogen add hydrogen after mixing with distillate R20F-B together；For example it can be distillate R20F-B by pre-add hydrogen The pre- hydrogenation products of gained add hydrogen after mixing with distillate R20F-A together；For example it can be distillate R20F-A, distillate R20F- B parallel connection adds products therefrom mixing after hydrogen to separate together respectively；For example it can be distillate R20F-A, distillate R20F-B parallel connection point Plus after hydrogen hydrogen is not added again after products therefrom mixing together；Such as can be distillate R20F-A, distillate R20F-B adds respectively Products therefrom carries out thermal high separation respectively after hydrogen, and at least part of each hot high score gas enters direct hydrogenation liquefaction of coal reaction Process RU.
As shown in Figure 1, solvent oil hydrogenation stablizes reaction process R20,2 for can processing or multiple hydrogen supply hydrocarbon precursors, It is carried out in a set of high-pressure system, therefore investment is smaller, energy consumption is lower.
As shown in Figure 1, the present invention is molten provided with short route circulation is prepared using the hydrocarbon component in hot high score gas RUAP-HS-V Agent hydrogenation modification process MR-UNIT, overall goal is:
1. preparing short route circulation hydrogen supply dissolvent SR-DS using the hydrocarbon component in hot high score gas RUAP-HS-V；
2. recycling in hot high score gas RUAP-HS-V and not entering into short route circulation solvent hydrogenation modification process MR-UNIT Bypass hydrogen, these bypass hydrogen can through pipeline 341 enter post processing system RUP-HS-V-AUNIT Combined Treatment.
As shown in Figure 1, short route recycle solvent hydrogenation modification process MR-UNIT, as needed, may use through pipeline The such as new hydrogen of raw material XF or recycle hydrogen logistics or gas hydrogen of 315 conveyings, according to the needs of practical flow scheme, it is possible to create The material XP such as hydrogen conveyed through pipeline 390 and/or hydrocarbonaceous product deliver into rear portion conversion zone RUB through pipeline 391 Hydrogen supply agent.
As shown in Figure 1, hydrogen supply agent SR- can be used only in front conversion zone RUA in direct hydrogenation liquefaction of coal reaction process RU DS, at this point, a small amount of higher boiling hydrogen supply agent is used only in front conversion zone RUA.Certainly, front conversion zone RUA can be simultaneously using short Journey hydrogen supply agent SR-DS, long-range hydrogen supply agent LR-DS.
As shown in Figure 1, rear portion conversion zone RUB only can directly receive long-range in direct hydrogenation liquefaction of coal reaction process RU Hydrogen supply agent LR-DS, at this point, less low boiling point hydrogen supply agent can be used only in rear portion conversion zone RUB.Certainly, rear portion conversion zone RUB Short distance hydrogen supply agent SR-DS, long-range hydrogen supply agent LR-DS can be used simultaneously.
The main object of the present invention is, for hydrocarbon material hydrogenation process RU, to be obtained based on front conversion zone product RUAP It is obtained by stabilized hydrogenation reaction process MR containing confession to separation gas RUA-PS-V based on the hydro carbons that separation gas RUA-PS-V is carried Hydrogen hydrocarbon products MRP, based on product MRP anteriorly conversion zone RUA provide the hydrocarbon containing hydrogen supply circulation hydrocarbon stream MR-KRDS, attached drawing 2~ Figure 21 shows several working methods.
Fig. 2 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The principle process that the 1st kind of technical solution of the MR-UNIT of short route hydrogen supply hydrocarbon is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V shows It is intended to.
As shown in Fig. 2, being the rear-mounted online stabilized hydrogenation side that hot high score gas RUAP-HS-V is directly entered reaction process MR The purpose of method, technique is: separation stabilized hydrogenation product MRP obtains hydrocarbon ils MRP-TS-L, deviates from after hydrocarbon ils MRP-TS-L decompression low Boiling point component obtains circulation hydrocarbon stream MR-KRDS；Its process includes: to prepare the hydrogenation modification reaction process of short route circulation solvent The thermal high separation process MRP-HS of MR, MR product MRP, the delivery pump KA-PUMP that may be used, the separation process that may be used S500。
As shown in Fig. 2, the precursor of short route hydrogen supply dissolvent SR-DS is the hydro carbons in hot high score gas RUAP-HS-V, heat is high Divide gas RUAP-HS-V to enter short route hydrogen supply dissolvent oil stabilized hydrogenation reaction process MR through pipeline 131, is supplied in hydrogen, short route The reaction of aromatic hydrogenation fractional saturation occurs under hydrogen solvent oil hydrogenation rugged catalyst existence condition, is converted into the production rich in hydrogen supply hydrocarbon Object MRP.
As shown in Fig. 2, as needed, hydrogen gas stream MRHF enters short route hydrogen supply dissolvent oil stabilized hydrogenation through pipeline 3155 Reaction process MR.
As shown in Fig. 2, product MRP is separated into gas MRP-TS-V i.e. into high pressure separation process MRP-TS through pipeline 311 XH2 and liquid MRP-TS-L, MRP-TS-V are used as logistics XH2.
As shown in Fig. 2, high pressure separation process MRP-HS, can be used any appropriate operating condition, usually few as far as possible condensation Normal boiling point is lower than 200 DEG C of hydrocarbon component.Usual MRP-TS-L is mainly higher than 280 DEG C by normal boiling point or higher than 230 DEG C Hydro carbons composition, the operation temperature of the gas-liquid separation process: can for 20~420 DEG C, be usually 150~330 DEG C, general It is 180~280 DEG C, preferably 200~250 DEG C.
As shown in Fig. 2, as needed, the air lift hydrogen conveyed through pipeline 3158 can be used in high pressure separation process MRP-TS Gas MRP-TS-BV contacts liquid existing for thermal high separation process MRP-TS, with air lift low boiling component therein, impurity group Point, gas stripping gas may finally be entered in hot high score gas MRP-TS-V.
The scheme shown in Fig. 2, its advantage is that reuse hydrogen in hot high score gas RUAP-HS-V and process is simple, The disadvantage is that not being avoided that the foreign gas such as H of hot high score gas RUAP-HS-V2O、NH3、CO、CO2, HCL introducing MR, these impurity Gas severe exacerbation MR catalyst operation efficiency (cause MR catalyst life short, hydrogen supply dissolvent unstable quality).Therefore, should The hot high score gas RUAP- of the process reaction process low particularly suitable for foreign gas content such as heavy-oil hydrogenation heat cracking reaction process In contrast HS-V is poorly suited for the heat of the high reaction process of foreign gas content such as direct hydrogenation liquefaction of coal reaction process High score gas RUAP-HS-V.
As shown in Fig. 2, hot high score gas RUAP-HS-V has been directly entered reaction process MR, and therefore, the behaviour of liquid MRP-TS-L Make the operating pressure that pressure is lower than direct hydrogenation liquefaction of coal front conversion zone RUA, liquid MRP-TS-L is through pipeline 351, dropping valve F77, the conveying of pipeline 3161 are used as S500-F.
It, can be using at least part MRP-TS-L as taking off light group as shown in Fig. 2, de- light component step S500 can be set The charging S500-F of S500 is used step by step, is separated into de- light group that the hydrocarbon component mainly by normal boiling point higher than 100 DEG C forms Liquid separation S500-L and other separation product S500-LB.In de- light component step S500, S500-F is generally separated out mainly by routine The de- light component lime set S500-L that boiling point is higher than 200 DEG C, is generally mainly made of 200~400 DEG C of the hydrocarbon component.Then, at least The de- light component lime set S500-L of a part, can be used as recycle hydrocarbons MR-KRDS use, prepare solvent naphtha for example as coal slurry, Coal slurry configuration section M10 prepares coal slurry, and enters in the front conversion zone RUA of direct hydrogenation liquefaction of coal reaction process, contact slurry Material carries out hydrocarbon powder and hydrogen direct liquefaction is added to react.Certainly, part takes off light component lime set S500-L, and it is direct can to enter coal hydrogenation In the rear portion conversion zone RUB of liquefaction reaction process, contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react.
De- light component step S500 as shown in Figure 2, any appropriate operating condition can be used according to lock out operation target, Usually using separator, stripper, fractionating column be one such or several equipment.
Fig. 3 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The principle process of the 2nd kind of technical solution of short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V Schematic diagram.
As shown in figure 3, increasing high pressure separating liquid MRP-HS-L by pump KA-PUMP pressurization compared with the scheme shown in Fig. 2 Afterwards, it conveys through pipeline 352 and is used directly as recycle hydrocarbons MR-KRDS, that is, SR-DS-TO-RUA.
As shown in figure 3, product MRP is separated into hot high score gas MRP- into thermal high separation process MRP-HS through pipeline 311 HS-V and hot high score oil MRP-HS-L, hot high score gas MRP-HS-V are used as logistics XH2, and hot high score oil MRP-HS-L uses crop Flow SR-DS.
As shown in figure 3, thermal high separation process MRP-HS, the purpose is to obtain hydrogen supply hydrocarbon and isolate other groups to be grouped as Gas, can be used any appropriate operating condition, usually condensation normal boiling point is lower than 200 DEG C of hydrocarbon component less as far as possible.It is logical Hydro carbons of the normal hot high score oil MRP-HS-L mainly by normal boiling point higher than 280 DEG C or higher than 230 DEG C forms, the gas-liquid point Operation temperature from process: it is usually 150~330 DEG C, generally 180~280 DEG C, is preferably 200~250 DEG C.
As shown in figure 3, hot high score gas RUAP-HS-V has been directly entered reaction process MR, and therefore, hot high score oil MRP-HS-L Operating pressure be lower than direct hydrogenation liquefaction of coal front conversion zone RUA operating pressure, hot high score oil MRP-HS-L is through pipeline 351 Into after pump KA-PUMP pressurization, direct hydrogenation liquefaction of coal front conversion zone RUA can be entered through pipeline 352 and be used as logistics SR- DS。
As shown in figure 3, as needed, the air lift conveyed through pipeline 3158 can be used in thermal high separation process MRP-HS Hydrogen MRP-HS-BV contacts liquid existing for thermal high separation process MRP-HS, with air lift low boiling component therein, gas stripping gas It may finally be entered in hot high score gas MRP-HS-V.
As shown in figure 3, de- light component step S500 can be set, it can be using part MRP-HS-L as de- light component step The charging S500-F of S500 is used.
Fig. 4 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The principle process of the 3rd kind of technical solution of short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V Schematic diagram.
As shown in figure 4, increasing the pre-separation process MRP- of hydrogenation modification reaction product MRP compared with the scheme shown in Fig. 3 PS, pre-separation process MRP-PS are usually thermal high separation process, and the purpose is to isolate part higher boiling hydrogen supply the hydrocarbon component to make For pre-separation liquid MRP-PS-L exclusive use.
As shown in figure 4, product MRP enters pre-separation process, that is, thermal high separation process MRP-PS through pipeline 311, it is separated into Hot high score gas MRP-PS-V and hot high score oil MRP-PS-L.
As shown in figure 4, thermal high separation process MRP-PS, the purpose is to obtain higher boiling hydrogen supply hydrocarbon and isolate other groups Any appropriate operating condition can be used in the gas being grouped as, and usually condenses the hydro carbons group that normal boiling point is lower than 350 DEG C less as far as possible Point.Hydro carbons of the usual hot high score oil MRP-PS-L mainly by normal boiling point higher than 300 DEG C or higher than 380 DEG C forms, described The operation temperature of gas-liquid separation process: it is usually 150~330 DEG C, generally 180~280 DEG C, is preferably 200~250 DEG C.
As shown in figure 4, hot high score gas MRP-PS-V is entered in thermal high separation process MRP-HS, wherein the hydrogen supply carried Hydro carbons of the hydrocarbon mainly by normal boiling point lower than 350 DEG C or lower than 400 DEG C forms.
As shown in figure 4, hot high score oil MRP-PS-L can be conveyed through pipeline 32 as confession after pump KA2-PUMP pressurization Hydrogen hydrocarbon stream SR-DS-TO-RU removes rear portion conversion zone RUB；Front conversion zone can certainly be removed, decanting point position can not It is same as the decanting point of SR-DS-TO-RUA logistics.
It, can be using at least part MRP-PS-L as taking off light group as shown in figure 4, de- light component step S520 can be set The charging S520-F of S520 is used step by step, is separated into de- light group that the hydrocarbon component mainly by normal boiling point higher than 100 DEG C forms Liquid separation S520-L and other separation product S520-LB.In de- light component step S520, S520-F is generally separated out mainly by routine The de- light component lime set S520-L that boiling point is higher than 200 DEG C, is generally mainly made of 200~400 DEG C of the hydrocarbon component.Then, at least The de- light component lime set S520-L of a part, can be used as hydrogen-containing hydrocarbon stream SR-DS-TO-RU use, prepare for example as coal slurry molten Agent oil is prepared coal slurry in coal slurry configuration section M10, and is entered in the front conversion zone RUA of direct hydrogenation liquefaction of coal reaction process, Contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react.Certainly, part takes off light component lime set S520-L, can add into coal In the rear portion conversion zone RUB of hydrogen direct liquefaction reaction process, contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react.
De- light component step S520 as shown in Figure 4, any appropriate operating condition can be used according to lock out operation target, Usually using separator, stripper, fractionating column be one such or several equipment.
The shortcomings that in order to overcome scheme shown in Fig. 2~Fig. 4, proposes the hot high score gas RUAP- of setting shown in Fig. 5~Figure 11 The process of the warm high pressure separation process RUAP-HS-V-MS of HS-V, hot high score gas RUAP-HS-V is in warm high pressure separation process RUAP- HS-V-MS is separated into warm high score gas RUAP-HS-V-MS-V and warm high score oil RUAP-HS-V-MS-L, warm high score oil RUAP-HS- V-MS-L enters short route hydrogen supply dissolvent oil stabilized hydrogenation reaction process MR, and advantage avoids that hot high score gas RUAP-HS-V's is miscellaneous Matter gas such as H2O、NH3、CO、CO2, HCL introducing MR, so as to improve MR catalyst operation efficiency (improve catalyst work live Property, extend MR catalyst life it is short, improve hydrogen supply dissolvent quality stability).Therefore, which contains particularly suitable for foreign gas In contrast the hot high score gas RUAP-HS-V for measuring high reaction process such as direct hydrogenation liquefaction of coal reaction process, is poorly suited for The hot high score gas RUAP-HS-V of the low reaction process of foreign gas content such as heavy-oil hydrogenation heat cracking reaction process.
Fig. 5 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The principle process of the 4th kind of technical solution of short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V Schematic diagram.
As shown in figure 5, increasing warm high pressure separation process RUAP-HS-V-MS, hot high score gas compared with the scheme shown in Fig. 2 RUAP-HS-V enters warm high pressure separation process RUAP-HS-V-MS through pipeline 131, is separated into warm high score gas RUAP-HS-V-MS-V Enter short route hydrogen supply dissolvent oil through pipeline 305 with warm high score oil RUAP-HS-V-MS-L, warm high score oil RUAP-HS-V-MS-L Stabilized hydrogenation reaction process MR, hot high score gas MRP-HS-V are used as logistics XH1.
As shown in figure 5, as needed, warm high pressure separation process RUAP-HS-V-MS can be used and convey through pipeline 3151 Air lift hydrogen RUAP-HS-V-MS-BV contact liquid existing for warm high pressure separation process RUAP-HS-V-MS, wherein with air lift Low boiling component, impurity composition, gas stripping gas may finally be entered in warm high score gas RUAP-HS-V-MS-V.
As shown in figure 5, warm high pressure separation process RUAP-HS-V-MS, the purpose is to obtain hydrogen supply hydrocarbon precursor and isolate The other groups of gases being grouped as, can be used any appropriate operating condition.Usually temperature high score oil RUAP-HS-V-MS-L mainly by Normal boiling point is higher than 250 DEG C or the hydro carbons composition higher than 200 DEG C, the gas of the warm high pressure separation process RUAP-HS-V-MS The operation temperature of liquid separation process: it is usually 150~330 DEG C, generally 180~280 DEG C, is preferably 200~250 DEG C.
The scheme shown in Fig. 5, its advantage is that avoiding the foreign gas such as H of hot high score gas RUAP-HS-V2O、NH3、CO、 CO2, HCL enter reaction process MR, the disadvantage is that the hydrogen in hot high score gas RUAP-HS-V can not be reused, if plus hydrogen The hydrogen stablized in reaction product MRP is not reused, it will causes air system flow complexity, investment big.
Fig. 6 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The principle process of the 5th kind of technical solution of short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V Schematic diagram.
As shown in fig. 6, increasing warm high pressure separation process RUAP-HS-V-MS, hot high score gas compared with the scheme shown in Fig. 3 RUAP-HS-V enters warm high pressure separation process RUAP-HS-V-MS through pipeline 131, is separated into warm high score gas RUAP-HS-V-MS-V Enter short route hydrogen supply dissolvent oil through pipeline 305 with warm high score oil RUAP-HS-V-MS-L, warm high score oil RUAP-HS-V-MS-L Stabilized hydrogenation reaction process MR, hot high score gas MRP-HS-V are used as logistics XH1.
Fig. 7 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The principle process of the 6th kind of technical solution of short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V Schematic diagram.
As shown in fig. 7, increasing warm high pressure separation process RUAP-HS-V-MS, hot high score gas compared with the scheme shown in Fig. 4 RUAP-HS-V enters warm high pressure separation process RUAP-HS-V-MS through pipeline 131, is separated into warm high score gas RUAP-HS-V-MS-V Enter short route hydrogen supply dissolvent oil through pipeline 305 with warm high score oil RUAP-HS-V-MS-L, warm high score oil RUAP-HS-V-MS-L Stabilized hydrogenation reaction process MR, hot high score gas MRP-HS-V are used as logistics XH1.
Fig. 8 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The principle process of the 7th kind of technical solution of short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V Schematic diagram.
As shown in figure 8, the booster pump KA-PUMP of short route hydrogen supply dissolvent is taken in process compared with the scheme shown in Fig. 6 Disappear, increase warm high score oil KB-PUNP booster pump, by the thermal high separation process MRP-HS's of reaction process MR, MR product MRP Operating pressure improves, and makes it higher than the operating pressure of direct hydrogenation liquefaction of coal reaction process RU, forms forward type and adds hydrogen steady online Determine method.
As shown in figure 8, temperature high score oil RUAP-HS-V-MS-L through pipeline 305 by pump KB-PUMP pressurization after, through pipeline 307 enter short route hydrogen supply dissolvent oil stabilized hydrogenation reaction process MR.
As shown in figure 8, temperature high score gas RUAP-HS-V-MS-V enters post processing system RUAP-HS-V- through pipeline 301 AUNIT。
As shown in figure 8, hot high score gas MRP-HS-V is conveyed through pipeline 341, direct hydrogenation liquefaction of coal can be entered and reacted Journey RU's needs position.
The scheme shown in Fig. 8, its advantage is that avoiding the foreign gas such as H of hot high score gas RUAP-HS-V2O、NH3、CO、 CO2, HCL enter MR, the hydrogen in stabilized hydrogenation reaction product MRP may be reused and process is simple, and the two of hydrogen It is secondary use can be multipaths point many places as new hydrogen, quenching hydrogen, rinse hydrogen, air lift hydrogen etc. uses, short route hydrogen supply dissolvent Using for oil can be multipaths point many places and use as hydrogen supply agent, flushing oil, cooling oil etc., and flexibility is bigger.
Fig. 9 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The principle process of the 8th kind of technical solution of short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V Schematic diagram.
As shown in figure 9, compared with the scheme shown in Fig. 7, in process by the booster pump KA-PUMP of short route hydrogen supply dissolvent, Booster pump KA2-PUMP cancels, and warm high score oil KB-PUNP booster pump is increased, by the thermal high of reaction process MR, MR product MRP The operating pressure of separation process MRP-HS improves, and makes it higher than the operating pressure of direct hydrogenation liquefaction of coal reaction process RU, is formed The online stabilized hydrogenation method of forward type.
Figure 10 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The 9th kind of technical solution that short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V principle stream Journey schematic diagram.
As shown in Figure 10, shown in Fig. 8 compared with scheme, by MR product MRP directly as containing hydrogen-containing hydrocarbon stream in process It recycles hydrocarbon stream MR-KRDS to use, also makes the hydrogen in product MRP by secondary use, eliminate separation, the transport Stream at rear portion Journey.As shown in Figure 10, the operating pressure of the thermal high separation process MRP-HS of reaction process MR, MR product MRP is higher than coal hydrogenation The operating pressure of direct liquefaction reaction process RU forms the online stabilized hydrogenation method of forward type, at least part product MRP conduct The hydrocarbon stream MR-KRDS containing hydrogen-containing hydrocarbon stream circulation is used, into the front conversion zone of direct hydrogenation liquefaction of coal reaction process RU RUA；Certainly, portion of product MRP can enter the rear portion conversion zone RUB of direct hydrogenation liquefaction of coal reaction process RU.
Figure 11 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention The 10th kind of technical solution that short route hydrogen supply hydrocarbon part MR-UNIT is prepared with hydrocarbon ils in hot high score gas RUAP-HS-V principle Flow diagram.
As shown in figure 11, shown in Fig. 9 compared with scheme, by MR product MRP directly as containing hydrogen-containing hydrocarbon stream in process It recycles hydrocarbon stream MR-KRDS to use, also makes the hydrogen in product MRP by secondary use, eliminate separation, the transport Stream at rear portion Journey.As shown in figure 11, the operating pressure of the thermal high separation process MRP-HS of reaction process MR, MR product MRP is higher than coal hydrogenation The operating pressure of direct liquefaction reaction process RU forms the online stabilized hydrogenation method of forward type, at least part product MRP conduct The hydrocarbon stream MR-KRDS containing hydrogen-containing hydrocarbon stream circulation is used, into the front conversion zone of direct hydrogenation liquefaction of coal reaction process RU RUA；Certainly, portion of product MRP can enter the rear portion conversion zone RUB of direct hydrogenation liquefaction of coal reaction process RU.
Figure 12 is the stabilized hydrogenation object reuse method of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention With hot high score gas RUAP-HS-V deviate from heavy hydrocarbon after produce reaction process MR charging MR-F principle process schematic diagram.
As shown in figure 12, hot high score gas RUAP-HS-V enters thermal high separation process AP-HS through pipeline 131, is separated into heat High score gas AP-HS-V and hot high score oil AP-HS-L；Hot high score oil AP-HS-L is conveyed through pipeline 1311, can be used as half way hydrogen supply Agent uses, and hot high score gas AP-HS-V enters short route hydrogen supply dissolvent oil stabilized hydrogenation through pipeline 1312 as charging MR-F and reacts Process MR.
As shown in figure 12, thermal high separation process AP-HS, the purpose is to produce the low heavy of reaction process MR after deviating from heavy hydrocarbon Matter hydrocarbon charging MR-F, can be used any appropriate operating condition.Usual hot high score oil AP-HS-L is mainly higher than by normal boiling point 400 DEG C or the hydro carbons composition higher than 450 DEG C, the operation temperature of the gas-liquid separation process of the thermal high separation process AP-HS Degree: it is usually 300~480 DEG C, generally 350~440 DEG C, is preferably 380~420 DEG C.
The scheme shown in Figure 12 enters its advantage is that avoiding the high boiling hydrocarbon carried secretly in hot high score gas RUAP-HS-V Reaction process MR reduces operating severity.
As shown in figure 12, as needed, the air lift conveyed through pipeline 3152 can be used in thermal high separation process AP-HS Hydrogen AP-HS-BV contacts liquid existing for thermal high separation process AP-HS, with air lift low boiling component therein, impurity group Point, gas stripping gas may finally be entered in AP-HS-V.
Scheme shown in Figure 12 can be used, technical solution shown in Fig. 2~Figure 11 is transformed.
Figure 13 is the basic flowsheet of coal preparation of the clear stripping step BS700 of the material of the invention containing product slurry.
As shown in figure 13, in stripping step BS700, the front reaction zone from direct hydrogenation liquefaction of coal reaction process RU The material RUA-X-LP containing product slurry of RUA is separated into gas after contacting at least once with the BG10 of material containing gas stripping gas completion BS700-V and slurries BS700-L makes 230~400 DEG C of at least part normal boiling point in the slurries of material RUA-X-LP Hydro carbons vaporization enters in gas BS700-V, the weight for the hydro carbons that the normal boiling point in gas BS700-V is 230~400 DEG C, greatly It is normal in the weight of hydro carbons that normal boiling point in the gas phase of material RUA-X-LP is 230~400 DEG C, the gas phase of material BG10 Advise the sum of the weight of hydro carbons that boiling point is 230~400 DEG C.
Material RUA-X-LP containing product slurry, can be the slurries for being substantially free of bubble, such as gas-liquid mixed phase reaction product Heat high separator discharge slurries；Material RUA-X-LP containing product slurry, can be the slurries containing a small amount of bubble, such as sets Set the slurry that the suspended-bed reactor of liquid collecting cup is discharged by liquid collecting cup；Material RUA-X-LP containing product slurry, can be gas-liquid Reaction product.
The BG10 of material containing gas stripping gas, can be the gas for being substantially free of liquid phase or slurries, such as new hydrogen or circulating hydrogen or de- Liquid gas is also possible to the gas of downstream reaction section RUB discharge or containing gas material, it might even be possible to be from other hydrogenation processes Gas, such as solvent oil hydrogenation stablizes the hydrogen (preferably de- liquid hydrogen gas) that reaction process is discharged plus hydrogen grading process is discharged Hydrogen (preferably de- liquid hydrogen gas)；The BG10 of material containing gas stripping gas can be the gas containing a small amount of liquid phase or slurries, as gas-liquid is anti- Answer the entrained drip of the high separator discharge of the heat of product or the gas of slurry；The BG10 of material containing gas stripping gas, can be gas liquid reaction The suspended-bed reactor of liquid collecting cup is such as arranged by the gas of reactor head discharge when liquid collecting cup discharge major part product slurry in product Liquid mixed phase product.
Figure 14~Figure 18 is several typical air lifts of the clear stripping step BS700 of the material of the invention containing product slurry With the basic flowsheet of coal preparation of gas-liquid separate mode.
Gas-liquid separator can be set partition and be separated out 2 or multiple gas-liquid separation subspaces, than if any subspace use In the gas-liquid separation of gas-liquid charging, some subspaces are for the operation of the air lift of slurries and gas stripping gas.
Figure 14 is the 1st kind of device structure function of the clear stripping step BS700 of the material of the invention containing product slurry Schematic diagram.
As shown in figure 14, the BG10 of material containing gas stripping gas that liquid phase or slurries may be contained, with being produced containing slurries for possible bubbles The material RUA-X-LP of object enters gas-liquid after the blending space before entering gas-liquid separation space is mixed into mixture M F700 Separated space such as knockout drum, hybrid position can be can even is that in pipeline or in the mixer of pipeline in reactor or In mixer in gas-liquid separator；In gas-liquid separation space such as high pressure hot separator BS700, it is separated into the gas flowed up The body BS700-V and liquid B S700-L to flow downward.
Figure 15 is the 2nd kind of device structure function of the clear stripping step BS700 of the material of the invention containing product slurry Schematic diagram.
As shown in figure 15, the BG10 of material containing gas stripping gas that liquid phase or slurries may be contained, at high pressure hot separator BS700 Portion space carries out gas-liquid separation, is separated into the gas BG10-V and liquid B G10-L flowed up；Possible bubbles contain slurries The upper space of the material RUA-X-LP of product in high pressure hot separator BS700 carries out gas-liquid separation, is separated into and flows up The herringbone for being set to middle upper section is flowed down through after gas RUA-X-LP-V and liquid RUA-X-LP-L, liquid RUA-X-LP-L distribution Shape column plate region Z1 becomes liquid B S700-I- after being vaporized flash distillation with the gas BG10-V counter current contacting flowed up herein Lower space DA is fallen under LP；Air lift mass transfer section Z1 ascending vapor and RUA-X-LP-V are used as hot high score gas BS700- after mixing V；Liquid B S700-I-LP and liquid B G10-L is used as BS700-L after mixing.
Figure 16 is the 3rd kind of device structure function of the clear stripping step BS700 of the material of the invention containing product slurry Schematic diagram.
As shown in figure 16, the BG10 of material containing gas stripping gas that liquid phase or slurries may be contained, with being produced containing slurries for possible bubbles The material RUA-X-LP of object enters gas-liquid after the blending space before entering gas-liquid separation space is mixed into mixture M F700 Separated space such as knockout drum；The area A in gas-liquid separation space such as high pressure hot separator BS700, is separated into and flows up Gas MF700-V and the liquid MF700-L that flows downward；Meanwhile the material MF600 of combined separation, in gas-liquid separation space Such as the area B in high pressure hot separator BS700, the liquid MF600- for being separated into the gas MF600-V flowed up and flowing downward L；Gas MF700-V and gas MF600-V is used as hot high score gas BS700-V after mixing；Liquid MF700-L and liquid MF600- L is used as BS700-L after mixing；Knockout drum BS700E at this time is a kind of to form relatively independent 2 separation using demarcation plate The combination trap in space, the top of demarcation plate GB, the connection of lower part gas-phase space.
Figure 17 is the 4th kind of device structure function of the clear stripping step BS700 of the material of the invention containing product slurry Schematic diagram.
It is the 4th kind of device structure of the clear stripping step BS700 of the material of the invention containing product slurry shown in Figure 17 And function, the 3rd kind of device structure with the clear stripping step BS700 for shown in Fig. 6 being the material of the invention containing product slurry And function the difference is that；The upper gaseous phase space connection of demarcation plate GB, lower part gas-phase space are not connected to, the lower part of demarcation plate GB Liquid Space connection.
Figure 18 is the 5th kind of device structure function of the clear stripping step BS700 of the material of the invention containing product slurry Schematic diagram.
It is the 5th kind of device structure of the clear stripping step BS700 of the material of the invention containing product slurry shown in Figure 18 And function, the 4th kind of device structure with the clear stripping step BS700 for shown in Fig. 7 being the material of the invention containing product slurry And function the difference is that: the connection of the upper gaseous phase space of demarcation plate GB, lower part gas-phase space be not connected to, lower liquid phase space It is not connected to, knockout drum BS700E, 2 liquid material products is discharged, a liquid material product is MF700-L i.e. BS700-L1, a liquid material Product is MF600-L i.e. BS700-L2.
Figure 19 is the basic flowsheet of coal preparation of the fuzzy stripping step BS750 of the material of the invention containing product slurry.
As shown in figure 19, in stripping step BS750, from direct hydrogenation liquefaction of coal reaction process RU containing product slurry Material RUA-X-LP completes to be separated into an opposite gas-liquid volume ratio at least once after contact greatly with the BG10 of material containing gas stripping gas Rich gas material BS750-MV, an opposite small rich solution material BS750-ML of gas-liquid volume ratio, make the slurries of material RUA-X-LP In at least part normal boiling point be 230~400 DEG C hydro carbons vaporization enter rich gas material BS750-MV in, rich gas material The weight flow for the hydro carbons that normal boiling point in BS750-MV is 230~400 DEG C, it is normal in the gas phase greater than material RUA-X-LP Advise the hydrocarbon that the weight flow of hydro carbons, the normal boiling point in the gas phase of material BG10 that boiling point is 230~400 DEG C are 230~400 DEG C The sum of weight of class；It is empty that this working method is present in the gas-liquid separation for taking off liquid or partly degassed for gas-liquid product section Between, floating bed hydrogenation reactor gas-liquid product portion possessed by the gas-liquid separation space on liquid collecting cup top as liquid collecting cup is arranged Divide de- liquid functional areas.
Figure 20~Figure 28 is the stripping regime of several typical structure reactors of the invention or returns with recycle hydrocarbons MR-KRDS The basic flowsheet of coal preparation of mode.
Gas stripping gas can add in the feeding pipe between the reactor for the serial operation that some conversion zone is included Enter.
Gas stripping gas can be added in reactor, and can be arranged after the coal addition position of gas stripping gas as needed Gas-liquid mixed area and reallocation disk, can be set wall of reactor baffle, taper aperture masking baffle, and the hydrogen for reducing ejection is dry Disturb symmetry, the stability in the flow field of lower space.
Gas stripping gas, usually therefore hydrogen rich gas gas injects gas hydrogen in reactor, can have supplement simultaneously Hydrogen or the effect for increasing hydrogen partial pressure are also conducive to reduce the gas-liquid volume ratio of the conversion zone before injection air lift hydrogen, increase The liquid of reaction compartment contains rate, improves reaction compartment efficiency.
Figure 20 is the stripping regime of pure counter-current reactor of the invention and the basic flowsheet of coal preparation of lime set echo plex mode.
The technological principle process of the stripping regime of pure counter-current reactor of the invention and lime set echo plex mode as shown in figure 20 Figure, direct hydrogenation liquefaction of coal reaction process use 1 direct hydrogenation liquefaction of coal reactor RU-X, are using liquid charging stock upper feeding And fed under discharge, gassiness materials stock under product liquid and on gas-phase product discharge counter-current reactor；Counter-current reactor Bottom has liquid material de-bubbled section, top to have gas to take off liquid section；In general, the liquid material of gas phase may be carried secretly simultaneously comprising liquid, solid Raw material RXLF is evenly distributed on the horizontal cross-section of reactor by the distributor X51 of reactor middle and upper part；Simultaneously comprising gas The hydrogen charging RXH that slurries may be carried secretly, is cut by the level that the distributor X55 of reactor middle and lower part is evenly distributed to reactor On face；In the main reaction region of counter-current reactor, liquid material main body flow direction is downlink, and bubble phase body gas flow direction is uplink.
As shown in figure 20, in counter-current reactor, distributor X51 or more is liquid degassing there are the region of big quantity of fluid Area is used for gas-liquid separation, and region more than top gas phase area, that is, dynamic Liquid Surface is that gas takes off liquid zone, and gaseous product is discharged from top Reactor；The following near zone of distributor X55 is Product liquid degassing district, is used for gas-liquid separation；Counter-current reactor bottom section For Product liquid buffer area, for adjusting the residence time of de-gas liq product；Counter-current reactor bottom structure, preferably taper, The discharge gate of product liquid is preferably provided in conical bottom, and the cone angle φ of conical bottom is usually 30 °≤φ≤120 °, generally 30 ° to 90 °, preferably 40 ° to 50 °.
As shown in figure 20, since the bottom of counter-current reactor is conical bottom, remaining coal after unreacted is complete or reaction Powder, ash content or semicoke will be assembled and by the conical bottoms, and by means of the sliding discharge function of conical bottom, the solids such as ash content can be suitable It is completely exhausted out counter-current reactor sharply, without depositing in counter-current reactor bottom, so that it is guaranteed that high ash direct hydrogenation liquefaction of coal Process is continuously run.Due to being collected, being discharged, the direct hydrogenation liquefaction of coal to product containing solid liquid phase using conical bottom The movable part not being collected to solid in reactor, structure is simple, and solid particle is not easy to deposit in reactor cylinder body, To realize direct hydrogenation liquefaction of coal reactor long period, smoothly run.Conical bottom can be by unreacted coal, catalyst, coal In ash and mink cell focus direct hydrogenation liquefaction of coal reactor is effectively discharged, without being deposited in reactor cylinder body, if this A little solid depositions will lead to the reaction useful space and reduce, reduce the treating capacity of direct hydrogenation liquefaction of coal reactor, increase reaction heat Point increases direct hydrogenation liquefaction of coal reactor operational risk.
As shown in figure 20, direct hydrogenation liquefaction of coal counter-current reactor system further includes passing for monitoring the liquid level of liquid level Sensor X75 and fluid level control valve X78, liquid product remove lower section reactor after discharge pipe, fluid level control valve, pipeline；Most The liquid material product of first stage reactor discharge afterwards obtains the direct liquid of coal hydrogenation after usually going middle pressure or the degassing of low-pressure gas-liquid separation system Metaplasia generally goes through fractionating section and is separated into narrow fraction oil product and containing solid at oily material, the oily material of direct hydrogenation liquefaction of coal generation Residue, the liquefaction of suitable boiling range generates oil distillate after the stabilized hydrogenation reaction process that part aromatic hydrogenation is saturated, as Hydrogen supply dissolvent oil prepares coal slurry and enters the use of direct hydrogenation liquefaction of coal reaction process, and the liquefaction of remaining suitable boiling range generates oil and evaporates It is allocated as going for product adding hydrogen upgrading reaction process or goes to add hydrogen upgrading reaction process again after stabilized hydrogenation reaction process.
As shown in figure 20, fluid level control valve X78 is arranged on discharge pipe, liquid level sensor X75 signal and Liquid level Valve X78 connection is monitored the liquid level in reactor cylinder body by liquid level sensor X75, and then liquid level sensor X75 will be examined The liquid level signal measured is delivered to fluid level control valve X78, and fluid level control valve X78 controls aperture according to the liquid level signal received Product withdraw speed is adjusted, so that reaction liquid level keeps stable liquid level, on the one hand can prevent from rushing tower, on the other hand may be used Effectively to control residence time of the material in direct hydrogenation liquefaction of coal reactor.Liquid level sensor X75 can be radioactive nucleus Material liquidometer is also possible to bellows differential pressure levelmeter, preferably radioactive nucleus material liquidometer.In addition, High Pressure Difference fluid level control valve X78, usually using high temperature resistant, wear-resistant material.
As shown in figure 20, in reactor RU-X system, fresh coal RXLF enters the middle and upper part of reactor RU-X, passes through Distributor X51 is evenly distributed on the horizontal cross-section of reactor RU-X, then downlink；Hydrogen feeds RXVF and passes through reactor RU-X The distributor X55 of middle and lower part is evenly distributed on the horizontal cross-section of reactor RU-X, then uplink；The hydrogen make-up that may be used RXH and other feed gas RXV, uses as RXVF；Reactor is discharged from top in gaseous product RU-X-PV, that is, RUA-X-PV Reactor RU-X is discharged from bottom under the flow control of regulating valve X78 in RU-X, liquid material product RU-X-LP, that is, RUB-X-LP, goes Downstream process process.
As shown in figure 20, the direct hydrogenation liquefaction of coal reaction system that counter-current reactor pure for separate unit is constituted, recycle hydrocarbons MR- KRDS enters section of the upper position of reactor RU-X on the ZLINE of line of demarcation, line of demarcation ZLINE be located at distributor X51, About middle position between X55；The position of recycle hydrocarbons MR-KRDS is lower than distributor X51 and cannot be too close from X51, because following After cyclic hydrocarbon MR-KRDS enters reactor, can gradually it be evaporated by counter-current gas air lift during downlink, recycle hydrocarbons MR-KRDS's Vaporizing section quickly can leave reaction interval and cannot walk front reaction zone, thus excessive reduction operating efficiency；Recycle hydrocarbons The position of MR-KRDS is higher than line of demarcation ZLINE but should not or cannot be below line of demarcation ZLINE, because, recycle hydrocarbons MR-KRDS Into after reactor, the group branch that cannot be vaporized in time during downlink enters in product slurry RU-X-LP, or can be rear Portion's reaction zone undergoes the too long residence time that excessive thermal cracking negative reaction occurs, to reduce reaction selectivity, reduce operation effect Rate.
As shown in figure 20, the direct hydrogenation liquefaction of coal constituted for 2 or the pure counter-current reactor of more serial operations reacts System, when slurries serial operation, back flow of gas serial operation, recycle hydrocarbons MR-KRDS can enter the line of demarcation of first reactor The position of section under ZLINE even close to distributor X55, naturally it is also possible into the upper position of second reactor.
As shown in figure 20, the air lift material BG10 that may be used, the position of reactor RU-X is entered positioned at recycle hydrocarbons MR-KRDS The close place for the lower part set, for the middle matter hydrocarbon in air lift front conversion zone decline slurries.
Figure 21 is the stripping regime of the reactor of setting liquid collecting cup of the invention and the technological principle stream of lime set echo plex mode Cheng Tu.
As shown in figure 21, the stripping regime of the reactor of setting liquid collecting cup of the invention and the technique of lime set echo plex mode are former Then flow chart, direct hydrogenation liquefaction of coal reactor RUA-X are fed using charging under liquid charging stock RXLF, under gas raw material RXVF Up-flow reactor；Raw material uplink is converted into product RUA-X-P after passing through main reaction region, in liquid collecting cup and reactor head device The part of wall composition takes off liquid zone, and under the effect of gravity, part liquid material product RUA-X-LP preferentially enters liquid collecting cup and by drain The discharge of pipe autoreactor bottom, the top discharge of remaining gas-liquid product RUA-X-MP autoreactor.
As shown in figure 21, direct hydrogenation liquefaction of coal reactor RUA-X includes using product liquid liquid collecting cup and catheter Gas, liquid, solid combined reaction raw material enter reactor from bottom, upstream is equal by distributor (being represented by dashed line in figure) It is even to be distributed on the horizontal cross-section of reactor, it is then upper by main reaction region, it is converted into product RUA-X-P；Product RUA-X-P Enter gas-liquid separation zone by the annular space channel upstream that collection cups lateral wall and reactor inner sidewall are formed, under the effect of gravity, Partially liq RUA-X-LP is gathered in collection cups, and reactor is discharged from top in remaining product RUA-X-MP.
As shown in figure 21, for separate unit reactor constitute direct hydrogenation liquefaction of coal reaction system, recycle hydrocarbons MR-KRDS into Enter in the bottom charging of reactor RUA-X；The direct hydrogenation liquefaction of coal constituted for the reactor of 2 or more serial operations is anti- Answer system, when slurries serial operation, back flow of gas serial operation, recycle hydrocarbons MR-KRDS is normally entered in first reactor；When When one conversion zone includes 2 of serial operation or more reactors, recycle hydrocarbons MR-KRDS can enter any of the first conversion zone In reactor.
As shown in figure 21, air lift material BG10 is and anti-into the reaction compartment of the close liquid collecting cup in reactor RUA-X After answering material to be sufficiently mixed, into top gas-liquid separation zone, matter hydrocarbon vaporization in the part in product is made to enter gas-liquid product RUA- Discharge at the top of autoreactor, reduces the middle matter hydrocarbon quantity in liquid RUA-X-LP in this way in X-MP.
Figure 22 is the stripping regime and lime set echo plex mode of the reactor of setting product liquid forced circulation of the invention Basic flowsheet of coal preparation.
As shown in figure 22, the stripping regime of setting liquid collecting cup of the invention and the reactor of product liquid forced circulation and solidifying The basic flowsheet of coal preparation of liquid echo plex mode, direct hydrogenation liquefaction of coal reactor RUA-X be using under liquid charging stock RXLF charging, The up-flow reactor fed under gas raw material RXVF；Raw material uplink is converted into product RUA-X-P after passing through main reaction region, is collecting Liquid cup and reactor head wall composition part take off liquid zone, under the effect of gravity, part liquid material product RUA-X-LP preferentially into Enter liquid collecting cup and by the discharge of catheter autoreactor bottom, the Returning reactor RUA-X after circulating pump RUA-X-PUMP pressurization Bottom cycle processing, the top discharge of gas-liquid product RUA-X-MP autoreactor.
As shown in figure 22, for separate unit reactor constitute direct hydrogenation liquefaction of coal reaction system, recycle hydrocarbons MR-KRDS into Enter in the bottom charging of reactor RUA-X；The direct hydrogenation liquefaction of coal constituted for the reactor of 2 or more serial operations is anti- Answer system, when slurries serial operation, back flow of gas serial operation, recycle hydrocarbons MR-KRDS is normally entered in first reactor；When When one conversion zone includes 2 of serial operation or more reactors, recycle hydrocarbons MR-KRDS can enter any of the first conversion zone In reactor.
As shown in figure 22, the present invention does not consider that air lift position is arranged in reactor, because carrying out air lift in reactor It is contradictory with overall goal of the invention.
Figure 23 is the stripping regime for the reactor that setting product liquid forced circulation and discharge liquor of the invention force air lift With the basic flowsheet of coal preparation of lime set echo plex mode.
Setting product liquid forced circulation of the invention and discharge liquor shown in Figure 23 force the air lift side of the reactor of air lift The basic flowsheet of coal preparation of formula and lime set echo plex mode, with reacting for setting product liquid forced circulation of the invention shown in Figure 12 The difference of the basic flowsheet of coal preparation of the stripping regime and lime set echo plex mode of device is only that: circulating pump while product slurry is discharged RUA-X-LP, product slurry RUA-X-LP become material MF700 after mixing with gas stripping gas material BG10, and material MF700 goes gas-liquid Knockout drum carries out gas-liquid separation.The advantages of this working method, is, using the gas-liquid separating function in reactor, can be convenient Realize that the Forced Mixing of product slurry RUA-X-LP and gas stripping gas material BG10 such as use pipe-line mixer Forced Mixing in ground.
Stripping regime shown in Figure 23 is the de- middle matter hydrocarbon process of air lift and the vaporization heat absorption of middle matter hydrocarbon of high temperature liquid material product The process for realizing the cooling of high temperature liquid material product, is a kind of the difunctional of matter hydrocarbon in the cooling and vaporization of liquid material containing easy coking component Scheme.
Figure 24 is that the stripping regime of the reactor of setting product liquid forced circulation and discharge liquor of the invention and lime set are returned The basic flowsheet of coal preparation for the mode of returning.
The stripping regime and lime set of the reactor of setting product liquid forced circulation of the invention and discharge liquor shown in Figure 24 The basic flowsheet of coal preparation of echo plex mode, it is believed that be the united application of two kinds of processes of Figure 11, Figure 12.
As shown in figure 24, air lift material BG10 is and anti-into the reaction compartment of the close liquid collecting cup in reactor RUA-X After answering material to be sufficiently mixed, into top gas-liquid separation zone, matter hydrocarbon vaporization in the part in product is made to enter gas-liquid product RUA- Discharge at the top of autoreactor, reduces the middle matter hydrocarbon quantity in liquid RUA-X-LP in this way in X-MP.Therefore, which is not suitable for In front conversion zone or the reactor of the first conversion zone, because carrying out air lift in reactor with overall goal of the invention is lance Shield.The process can be applied to the reactor of rear portion conversion zone or final reaction section, can because carrying out air lift in reactor To enter matter hydrocarbon vaporization in part in gas phase, and matter hydrocarbon in these is finally imported into secondary use among the first conversion zone.
Figure 25 is the reactor of the first conversion zone of the invention using the setting product liquid forced circulation of 2 serial operations Stripping regime and lime set echo plex mode basic flowsheet of coal preparation.
First conversion zone of the invention shown in Figure 25 uses the reaction of the setting product liquid forced circulation of 2 serial operations The stripping regime of device and the basic flowsheet of coal preparation of lime set echo plex mode, it is believed that it is a kind of mutation of Figure 12 process, therefore, Reaction process does not use air lift material, and recycle hydrocarbons MR-KRDS can enter the first reactor entrance or second of the first conversion zone Reactor inlet.
As shown in figure 25, direct hydrogenation liquefaction of coal reactor RUA-1 is former using charging, gas under liquid charging stock RUA-1-LF The up-flow reactor fed under material RUA-1-VF；Raw material uplink is converted into product RUA-1-P after passing through main reaction region, in liquid collecting The part of cup and reactor head wall composition takes off liquid zone, and under the effect of gravity, part liquid material product RUA-1-LP is preferentially entered Liquid collecting cup is simultaneously discharged by catheter autoreactor bottom, the bottom Returning reactor RUA-1 after circulating pump RUA-1-PUMP pressurization Portion's cyclic process, the top discharge of gas-liquid product RUA-1-MP autoreactor.
As shown in figure 25, it is charging, gas under RUA-2-MF that direct hydrogenation liquefaction of coal reactor RUA-2, which is used containing serum materials, Body raw material RUA-2-VF is the up-flow reactor of lower charging；Raw material uplink is converted into product RUA-2-P after passing through main reaction region, Liquid zone is taken off in the part that liquid collecting cup and reactor head wall form, under the effect of gravity, part liquid material product RUA-2-LP is excellent It is introduced into liquid collecting cup and is discharged by catheter autoreactor bottom, the Returning reactor after circulating pump RUA-2-PUMP pressurization The processing of RUA-2 bottom cycle, the top discharge of gas-liquid product RUA-2-MP autoreactor.
Figure 26 is the internal-circulation type suspended-bed reactor at medium upstream in setting internal guide cylinder of the invention and guide shell Stripping regime and lime set echo plex mode basic flowsheet of coal preparation.
As shown in figure 26, reactor types are the internal-circulation type suspended-bed reactor that internal guide cylinder is arranged, center is upper, Surrounding flows down Flow Field Distribution, and reactor head is discharged gas-liquid mixed phase product and enters in corresponding gas-liquid separator.The reactor Top has certain gas-liquid separating function, therefore can carry out air lift operation herein.
Shown in Figure 26, air lift material BG10, into the reaction sky of the top exit of the close guide shell in reactor RUA-X Between, after being sufficiently mixed with reaction mass, into top gas-liquid separation zone, matter hydrocarbon vaporization in the part in product is made to enter gas-liquid production Discharge at the top of autoreactor in object RUA-X-MP, reduces the middle matter hydrocarbon quantity in reflux slurries RUA-X-LP in this way.Therefore, should Process is not suitable for the reactor of front conversion zone or the first conversion zone because carried out in reactor air lift with it is of the invention total Body target is contradictory.The process can be applied to the reactor of rear portion conversion zone or final reaction section, because in reactor Carrying out air lift can enter matter hydrocarbon vaporization in part in gas phase, and finally import matter hydrocarbon in these two among the first conversion zone Secondary use.
Shown in Figure 26, recycle hydrocarbons MR-KRDS can enter starting response location or the intermediate reaction position of the first conversion zone, Such as enter among first reactor entrance or first reactor.
Shown in Figure 26, when the first conversion zone uses the reactor of 2 or more serial operations, recycle hydrocarbons MR-KRDS can To enter in any reactor of front reaction zone RUA.
Figure 27 is the internal-circulation type suspended-bed reactor that medium is dirty in setting internal guide cylinder of the invention and guide shell Stripping regime and lime set echo plex mode basic flowsheet of coal preparation.
Process flow chart shown in Figure 27, compared with process flow chart as shown in figure 16, the material trend of equipment room in process Identical, difference is only that: reactor types replace with the internal-circulation type suspended-bed reactor of setting internal guide cylinder, central medium It flows down, surrounding upstream Flow Field Distribution；Certainly, the form of gas stripping gas BG10 distributor is also adjusted with position.
Figure 28 is that empty cylinder of the invention is bubbled the stripping regime of bed suspended-bed reactor and the technique of lime set echo plex mode Principle flow chart.
As shown in figure 28, reactor interior main body flow direction is upper, although local space is there are liquid material downward in reactor Interior circulation, Flow Field Distribution that center is upper, surrounding flows down；Reactor head is discharged gas-liquid mixed phase product and enters corresponding gas-liquid separation In device.The top of the reactor does not have apparent gas-liquid separating function, therefore, it is difficult to carry out air lift operation in reactor, Therefore it is not provided with gas stripping gas point.
Shown in Figure 28, recycle hydrocarbons MR-KRDS can enter starting response location or the intermediate reaction position of the first conversion zone, Such as enter among first reactor entrance or first reactor.
Shown in Figure 28, when the first conversion zone uses the reactor of 2 or more serial operations, recycle hydrocarbons MR-KRDS can To enter in any reactor of front reaction zone RUA.
Since the top gas phase space of the top gas phase space of pure counter-current reactor, high pressure hot separator has gas-liquid clear Therefore separated space can arrange the washing dedirt step using washing oil, to guarantee the subsequent operation of top gas phase product Stability.
Using the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones, realize that several typical process flows of the invention are shown in Figure 29~Figure 37.
Figure 29 is the 1st kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 29, the 1st kind of typical work of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Skill flow chart, belongs to 2 sections of reaction process of gas-liquid fair current, and the first conversion zone gas-liquid mixed phase product passes through the whole of the second conversion zone Reaction process, the gas-liquid mixed phase product USR2-MP at the top of second reactor USR2 enter in tail end gas-liquid separator KD.
As shown in figure 29, first reactor USR1 form is that the inside of product liquid forced cyclic type is arranged liquid collecting cup and leads The suspended-bed reactor of flow tube, liquid material USR1-L-TOR1 derived from least part liquid collecting cup are returned by forced circulation pump Return first reactor USR1 cyclic process.
As shown in figure 29, in reaction step USR1, coal slurry material USR1-NMJ, recycle hydrocarbons MKDS, the hydrogen that may be used Logistics USR1-VF, that is, new hydrogen USR1H enters reactor USR1 from bottom, and uplink flows through reaction zone, is converted into product USR1-P；Top in reactor USR1, product USR1-P are separated into liquid material USR1-L-TOR1 and gas-liquid mixed phase material USR1-MP。
As shown in figure 29, second reactor USR2 form is that the inside of product liquid forced cyclic type is arranged liquid collecting cup and leads The suspended-bed reactor of flow tube, liquid material USR2-L-TOR2 derived from least part liquid collecting cup are returned by forced circulation pump Return second reactor USR2 cyclic process.
As shown in figure 29, in reaction step USR2, gas-liquid mixed phase product USR1-MP, that is, USR2- from first reactor The i.e. new hydrogen USR2H of MF, the hydrogen gas stream USR2-VF that may be used, enters reactor USR2 from bottom, uplink flows through reaction Area is converted into product USR2-P；Top in reactor USR2, product USR2-P are separated into liquid material USR2-L-TOR2 With gas-liquid mixed phase material USR2-MP.
As shown in figure 29, the gas KD-V from gas-liquid separator KD is used as reaction gas product RU-X-PV, goes to condense Journey S100 obtains lime set, flows back into first reactor.
Figure 30 is the 2nd kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 30, the 2nd kind of typical work of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Skill flow chart belongs to slurry series connection, 2 section tandem reactor process of the hydrogen short circuit across stream, with use 2 of the invention shown in Figure 27 1st kind of typical process flow diagram of the direct hydrogenation liquefaction of coal reaction process of conversion zone the difference is that: first reactor The product of USR1 enters the mode of second reactor USR2, wherein the first conversion zone gas-phase product only passes through the tail of the second conversion zone Portion's reaction process still deviates from the main body reaction zone that part liquid material enters the second conversion zone；
As shown in figure 30, in reaction step USR1, top in reactor USR1, it is mixed that product USR1-P is separated into gas-liquid The mutually product liquid USR1-L of material USR1-MP and liquid collecting cup discharge；Gas-liquid mixed phase material USR1-MP is from the top of second reactor USR2 Portion enters, and after mixing with the material USR2-P in second reactor USR2, is separated into gas-liquid mixed product USR2-MP and liquid collecting cup The liquid material USR2-L-TOR2 of discharge, liquid material product USR2-L-TOR2 enter the after forced circulation pump USR2-PUMP pressurization The feed zone cyclic process of two bottoms reactor USR2；The product liquid USR1-L of reactor USR1 liquid collecting cup discharge, is divided into two Road, first via USR1-L-TOR1 enter the charging of the bottom first reactor USR1 after forced circulation pump USR1-PUMP pressurization Area's cyclic process, the second tunnel enter the bottom reaction zone of second reactor USR2 as product slurry USR1-LP.
Figure 31 is the 3rd kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 31, the 3rd kind of typical work of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Skill flow chart belongs to 2 sections of reaction process of liquid material serial operation, hydrogen parallel operation, any one conversion zone gas-phase product is not By the reaction zone of another conversion zone, reacted with the direct hydrogenation liquefaction of coal of 2 conversion zones of use of the invention shown in Figure 27 1st kind of typical process flow diagram of process the difference is that: increase the reaction product USR1-MP2 of the first conversion zone US1 Gas-liquid separator R1-THPS.
As shown in figure 31, in gas-liquid separation step R1-THPS, the air lift hydrogen R1-THPS-BH that may be used enters separation The slurry that the middle and lower part contact USR1-MP of tank is brought into, reactor USR1 top gas-liquid product USR1-MP enter gas-liquid separation step The middle part of R1-THPS knockout drum, is separated into the gas phase of the entrainment slurries of rising, the slurries of the entrained air bubbles of decline, and gas phase is passed through After the de- solid such as sedimentation separation and/or washing separation, de- heavy constituent process, arranged from top discharge gas R1-THPS-V, from bottom Slurries R1-THPS-L out.
As shown in figure 31, gas R1-THPS-V goes condensation process S100 to obtain recycle hydrocarbons MKDS, flows back into first reactor In；Slurries R1-THPS-L is used as slurries raw material as the product slurry USR1-LP reaction zone for entering second reactor USR2 USR2-LF。
Figure 32 is the 4th kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 32, the 4th kind of typical work of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Skill flow chart belongs to 2 sections of reaction process of liquid material serial operation, hydrogen parallel operation, any one conversion zone gas-phase product is not By the reaction zone of another conversion zone, reacted with the direct hydrogenation liquefaction of coal of 2 conversion zones of use of the invention shown in Figure 28 2nd kind of typical process flow diagram of process the difference is that: gas-liquid product USR1-MP goes to condense at the top of first reactor Journey S100 obtains recycle hydrocarbons MKDS, flows back into first reactor.
Figure 33 is the 5th kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 33, the 5th kind of typical work of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Skill flow chart belongs to 2 sections of reaction process of liquid material serial operation, hydrogen counter-current operation, with use 2 of the invention shown in Figure 30 4th kind of typical process flow diagram of the direct hydrogenation liquefaction of coal reaction process of conversion zone the difference is that: tail end gas-liquid point Gas KD-V from step KD discharge passes through the reaction zone of the first conversion zone as second conversion zone gas-phase product adverse current, from And realize the secondary use of hydrogen.
Figure 34 is the 6th kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 34, the 6th kind of typical work of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Skill flow chart belongs to 2 sections of reaction process of liquid material serial operation, hydrogen counter-current operation, with use 2 of the invention shown in Figure 31 5th kind of typical process flow diagram of the direct hydrogenation liquefaction of coal reaction process of conversion zone the difference is that: second reaction The gas-liquid mixed phase product USR2-MP of section reactor head discharge, the product adverse current as second conversion zone containing gas phase pass through the The reactor USR1 of one conversion zone, to realize the secondary use of hydrogen, and reflux fraction product slurry circulate operation.
As shown in figure 34, second reactor USR2 form is the suspended-bed reactor of internal setting liquid collecting cup and diversion pipe, Product liquid USR2-LP derived from least part liquid collecting cup is sent into tail end gas-liquid separator KD, the gas-liquid of reactor head The reactor USR1 that mixed phase material product USR2-MP enters the first conversion zone is used in series.
As shown in figure 34, in tail end knockout drum KD system, the air lift hydrogen KD-BH that may be used enters knockout drum KD Middle and lower part contacts the slurry that USR2-MP is brought into, and product liquid USR2-LP derived from second reactor USR2 liquid collecting cup enters separation In the middle part of tank KD, be separated into the gas phase of the entrainment slurries of rising, the slurries of the entrained air bubbles of decline, gas phase by sedimentation separation and/or After the de- solids such as washing separation, de- heavy constituent process, the gas KD-V being discharged from top enters later separation recovery system；The bottom of from The liquid KD-L of portion's discharge, removes separation and recovery system as direct hydrogenation liquefaction of coal liquid material product.
Figure 35 is the 7th kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 35, with the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention shown in Figure 32 6th kind of typical process flow diagram the difference is that: do not use tail end knockout drum KD system, by second reactor USR2 Partial liquid product USR2-LP derived from liquid collecting cup is sent into recovery system directly as final product slurry.
Figure 36 is the 8th kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 36, with the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention shown in Figure 33 7th kind of typical process flow diagram the difference is that: by partial liquid product derived from second reactor USR2 liquid collecting cup USR2-L is used as final product slurry USR2-LP-DV to be sent into recovery system after deviating from least partly bubble.
As shown in figure 36, product liquid USR2-L derived from second reactor USR2 liquid collecting cup, by cyclone separator USR2-PS separates the liquid stream USR2-PS-VL rich in bubble, the liquid stream USR2-PS-L that lean gas steeps all the way all the way；Liquid stream USR2- PS-L points are 2 tunnels, and first via liquid USR2-PS-L-TOR2 flows through instead as the bottom upstream that the circulation fluid of USR2 enters USR2 Answer area's circulate operation, circulation fluid is depleted gas richness solid-liquid, institute in favor of raising reaction compartment liquid phase volume point rate, be conducive to Increase catalyst liquid concentration.
As shown in figure 36, liquid stream USR2-PS-L points are 2 tunnels, and the second road liquid is sent as product slurry USR2-PS-L-DV Enter recovery system.
Figure 37 is the 9th kind of typical process stream of the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention Cheng Tu.
As shown in figure 37, with the direct hydrogenation liquefaction of coal reaction process of 2 conversion zones of use of the invention shown in Figure 34 8th kind of typical process flow diagram the difference is that: by derived from first reactor USR1 liquid collecting cup at least partly liquid produce Object USR1-L is sent into second reactor USR2 after deviating from least partly bubble as material USR1-PS-L-DV.
As shown in figure 37, partial liquid product USR1-L derived from first reactor USR1 liquid collecting cup, by cyclonic separation Device USR1-PS separates the thing liquid stream USR1-PS-VL rich in bubble, the liquid stream USR1-PS-L that lean gas steeps all the way all the way；Liquid stream USR1-PS-L points are 2 tunnels, and first via liquid USR1-PS-L-TOR1 enters the bottom upstream stream of USR1 as the circulation fluid of USR1 Cross reaction zone circulate operation, circulation fluid is depleted gas richness solid-liquid, institute in favor of the liquid phase volume of raising reaction compartment divide rate, Conducive to increase catalyst liquid concentration.
As shown in figure 37, liquid stream USR1-PS-L point is 2 tunnels, the second road liquid as product slurry USR1-PS-L-DV into Enter in second reactor USR2.
On the basis of 29~Figure 37 of earlier figures, increases the conversion zone of 1 or more liquid material serial operation, may be constructed Using the direct hydrogenation liquefaction of coal reaction process of multiple conversion zones, reaction gas-phase product lime set therein flows back, contains product slurry The working principle of air lift is identical, and working method is similar.
Among concrete application process of the invention, among the process as shown in FIG. 1 to FIG. 37, not according to operating pressure Together, the conveying of certain slurries may be needed using force (forcing) pump, 2 tunnels or multichannel source is identical and the pressurization for the slurries that whereabouts is different Journey can combine pressurization, to reduce high-pressure pump number of units, reduce investment.
Hereinafter, describing the typical process flow of 3 sections of reaction process of the invention.
3 sections of reaction process of the slurries serial operation increase 1 compared with 2 sections of reaction process of slurries serial operation A conversion zone, process complexity is high, and the number of devices used is more, invest it is larger, but can be achieved on be more nearly it is pure inverse The technological operation of stream, in general, technological operation improvement is huge.
Figure 38 is the overall principle technique stream for 3 sections of reaction process that each section of piecewise counter flow series of gassiness product of the invention use Cheng Tu.
As shown in figure 38,3 sections of reaction process use 3 conversion zones US1, US2, US3；Each conversion zone includes hydrocarbon material The gas-liquid separation step of hydrogenation reaction step and the step gas-liquid product, that is to say, that any conversion zone includes at least 1 band gas The reactor of liquid separation function, or including at least 1 reactor without gas-liquid separating function and matched 1 gas-liquid separation Device；Certainly, more reactors and/or more gas-liquid separators can be used in any conversion zone.
As shown in figure 38,3 sections of reaction process use 3 conversion zones US1, US2, US3；The liquid material of each upstream reaction section produces Object can be gone in any 1 reactor of any 1 downstream reaction section；Figure 38 shows that upstream liquid material goes adjacent downstream anti- The situation in the reactor of section is answered, wherein starting material liquid material US1LF enters the first conversion zone US1, and the first conversion zone liquid material produces Object US1LP goes the second conversion zone US2, the second conversion zone liquid material product US2LP to go third conversion zone US3, third conversion zone liquid material Product US3LP removes its separation and recovery system.
As shown in figure 38,3 sections of reaction process use 3 conversion zones US1, US2, US3；The gassiness of each downstream reaction section produces Object can be gone in any 1 reactor of any 1 upstream reaction section；Figure 38 shows that gassiness material adverse current in downstream goes phase Situation in the reactor of adjacent upstream reaction section, wherein starting material hydrogen US3H, that is, US3VF enters third conversion zone US3, the The second conversion zone US2, the second conversion zone are removed after the three conversion zone gassiness product US3VP and hydrogen make-up US2H that may be used mixing The first conversion zone US1, the first conversion zone gassiness product are removed after the gassiness product US2VP and hydrogen make-up US1H that may be used mixing US1VP removes its separation and recovery system.
For operational needs, each section of piecewise counter flow series of gassiness product of the invention use shown in Figure 38 3 sections are anti- The overall principle process flow chart for answering process, can form mutation, and Figure 32, Figure 33, Figure 34 are 3 kinds of possible operation formats.
Figure 39 is that the first conversion zone hydrogen material of the invention independently uses, third conversion zone gassiness product adverse current enters the The overall principle process flow chart for 3 sections of reaction process that two conversion zones are used in series.
As shown in figure 39, it in order to reduce reaction process operating pressure as far as possible, needs to increase density of hydrogen as far as possible minimum Point (namely foreign gas concentration highest point) reaction process hydrogen partial pressure, so instead by third conversion zone gas-phase product, second It answers section gas-phase product is all accumulative to enter the first conversion zone, will lead to the hydrogen partial pressure mistake of the second half reaction zone of the first conversion zone It is low, that is, cause all gas product accumulative；The first conversion zone hydrogen material shown in Figure 39 independently uses, third conversion zone gassiness Product adverse current enters the mode that the second conversion zone is used in series, conducive to the non-hydrogen for the second half reaction zone for reducing by the first conversion zone Gas buildup amount is conducive to improve hydrogen partial pressure, may result in certainly and use more hydrogen.
Process as shown in figure 39, due to the first conversion zone hydrogen material be independently operated, therefore its operating pressure not by third The restriction of conversion zone operating pressure, the second conversion zone operating pressure, the first conversion zone operating pressure can be higher than third conversion zone The liquid material product US1LP of operating pressure, the second conversion zone operating pressure, such first conversion zone goes downstream reaction section that can rely on Pressure difference gravity flow is without pumping pressure-increasing unit；Even, process as shown in figure 39, the first conversion zone can be anti-using third is higher by Answer the operating pressure independent operation of 2.0~4.0Mpa of a section operating pressure, the second conversion zone operating pressure.
Figure 40 is that the second conversion zone hydrogen material of the invention independently uses, third conversion zone gassiness product adverse current enters the The overall principle process flow chart for 3 sections of reaction process that one conversion zone is used in series.
As shown in figure 40, the second conversion zone hydrogen material independently uses, third conversion zone gassiness product adverse current enters first The mode of operation of conversion zone, it is therefore prevented that third conversion zone gas-phase product, the second conversion zone gas-phase product are all accumulative to enter first The hydrogen partial pressure of the second half reaction zone of the first conversion zone can be improved in conversion zone, is conducive to reduce device stagnation pressure, certainly may Cause using more hydrogen.
Process as shown in figure 40, due to the second conversion zone hydrogen material be independently operated, therefore its operating pressure not by third The restriction of conversion zone operating pressure, the first conversion zone operating pressure, the second conversion zone operating pressure can be higher than third conversion zone Operating pressure, such second conversion zone liquid material product US2LP go downstream reaction section can by pressure difference gravity flow without pump Pressure-increasing unit.
Figure 41 is that third conversion zone hydrogen material of the invention independently uses, the second conversion zone gassiness product adverse current enters the The overall principle process flow chart for 3 sections of reaction process that one conversion zone is used in series.
As shown in figure 41, third conversion zone hydrogen material independently uses, the second conversion zone gassiness product adverse current enters first The mode of operation of conversion zone, still by the maximum second conversion zone gas-phase product of impurity gas yield, the first conversion zone gas-phase product All accumulative the second half reaction zones for being present in the first conversion zone, cannot achieve the second half reaction zone for improving the first conversion zone The target of hydrogen partial pressure is unfavorable for reducing device stagnation pressure, also results in using more hydrogen, third conversion zone hydrogen purity is high Gas-phase product do not obtain secondary use.Therefore, it for hydrogen reuse, is said on ordinary meaning, the process is seldom With.
Process as shown in figure 41, due to third conversion zone hydrogen material be independently operated, therefore its operating pressure not by first The restriction of conversion zone operating pressure, the second conversion zone operating pressure, third conversion zone operating pressure can be lower than the second conversion zone Operating pressure, such second conversion zone liquid material product US2LP go downstream reaction section can by pressure difference gravity flow without pump Pressure-increasing unit.
Figure 42 is the partial process flow signal of the 2 segmentation direct hydrogenation liquefaction of coal reaction process of the embodiment of the present invention one Figure.
As shown in figure 42, the local process of the 2 segmentation direct hydrogenation liquefaction of coal reaction process of the embodiment of the present invention one Flow diagram illustrates that being recycled back to for the stabilized hydrogenation object of middle matter hydrocarbon in the flash steam of first reactor R1 reaction product is used The allied processes of journey.
Specific embodiment
The present invention described in detail below.
Pressure of the present invention, refers to absolute pressure.
Normal boiling point of the present invention refers to vapour of the substance under an atmospheric pressure, liquid equilibrium temperature.
Routine boiling range of the present invention refers to the normal boiling point range of fraction.
Specific gravity of the present invention, unless stated otherwise, refer to normal pressure, fluid density and normal pressure under the conditions of 15.6 DEG C, The ratio of water density under the conditions of 15.6 DEG C.
The composition or concentration or content or yield value of component of the present invention are unless stated otherwise weight basis Value.
Conventional gas hydrocarbon of the present invention refers under normal condition in gaseous hydro carbons, including methane, ethane, third Alkane, butane.
Conventional liq hydrocarbon of the present invention refers to the hydro carbons being in a liquid state under normal condition, including pentane and its boiling point Higher hydro carbons.
Impurity element of the present invention, refer to non-hydrogen in feedstock oil, non-carbon, nonmetallic ingredient for example oxygen, sulphur, nitrogen, Chlorine etc..
Impurity composition of the present invention refers to hydro-conversion object such as water, ammonia, the vulcanization of non-hydrocarbon component in feedstock oil Hydrogen, hydrogen chloride etc..
Light hydrocarbon of the present invention is naphtha component, refers to that normal boiling point is lower than 200 DEG C of conventional liq hydrocarbon.
Diesel component of the present invention refers to that normal boiling point is 200~350 DEG C of hydro carbons.
Wax oil component of the present invention refers to that normal boiling point is 350~530 DEG C of hydro carbons.
Middle matter hydrocarbon of the present invention refers to that normal boiling point is 230~400 DEG C of hydro carbons.
Heavy hydrocarbon of the present invention refers to that normal boiling point is higher than 350 DEG C of hydro carbons.
Hydrogen to oil volume ratio of the present invention refers to the normal of the standard state volume flow of hydrogen and specified oily logistics The ratio of pressure, 20 DEG C of volume flow.
Hydrogenation reaction space refers to the fluid circulation space that the hydrogenation reaction occurs, and can be the interior space of reaction such as Empty barrel reactor area, air lift hydrogen mixed zone, liquid collection cups upper space region etc., can be the reactor external space such as pipeline Space in interior space, valve, space in mixer, space etc. in pump.
Polycyclic aromatic hydrocarbon mentioned herein, aromatic ring number >=3.
Up flow type hydrogenator of the present invention, reaction compartment or the processing medium in hydrogenation catalyst bed Macroscopic view flowing dominant direction is from top to bottom.
The present invention described in detail below.
DCL/Direct coal liquefaction process is described below.
DCL/Direct coal liquefaction process of the present invention refers under solvent naphtha existence condition by adding hydrogen to keep coal hydrogenation direct Liquefied method, according to the difference of solvent naphtha and catalyst, pyrolysis way and add hydrogen mode difference and process conditions not Together, following several techniques can be divided into:
1. dissolution pyrolysis liquefaction process: low-ash extract can be made to pyrolysis of coal extracting using heavy solvent, and (Japan claims Swelling charcoal)；Extract the available oils based on mink cell focus at supercritical conditions using light solvent.This method does not have to hydrogen, Though former process yield is high but product is still solid, latter technique such as supercritical extraction (extraction) method (SCE) extract content is not It is too high；
2. solvent adds hydrogen to extract liquefaction process: if any solvent refined coal process 1 and II (SRC-1 and SRC-II), Exxon donor solvent process EDS, Japanese New Energy Development Organization liquefaction process (NEDOL) etc., using hydrogen, but pressure is less high, and solvent naphtha has apparent work With；
3. Hydrogenation method: such as the H coal process (H- of the old and new's liquefaction process (IG and the NewlG) and the U.S. of Germany ) etc. Coal this kind is belonged to；
4. coal and residual oil joint processing method (COprocessing): once passing through together with coal using residual oil as solvent naphtha anti- Device is answered, recycle oil is not had to.Hydrocracking occurs is converted into light oil to residual oil simultaneously.The U.S., Canada, Germany and former Soviet Union etc. are each There is different technique；
5. destructive distillation liquefaction process: coal is first pyrolyzed and obtains tar, then carries out hydrocracking and upgrading to tar；
6. underground liquefaction process: solvent being injected subterranean coal, makes coal depolymerization and dissolution, in addition the impact force of fluid collapses coal It dissipates, the coal not being completely dissolved is then suspended in solvent, is extracted solution out with pump and is separated processing.
In coal direct liquefaction method, majority belongs to direct hydrogenation liquefaction of coal liquefaction process, and no matter which kind of coal faces the direct liquid of hydrogen Change process, target are to obtain oil product, and the function of pursuit is " coal turns oil ", it is necessary to which existing chemical change is that " coal adds The common trait of hydrogen ", current such technology is using solvent naphtha and catalyst, and the conventional boiling range of solvent naphtha is generally 200~450 DEG C, it is most be 200~400 DEG C, solvent naphtha majority is distilled oil, and contained aromatic hydrocarbons majority is the aromatic hydrocarbons of 2~4 ring structures.Therefore, Either which kind of coal faces hydrogen direct liquefaction process, and the outer oil extraction or direct hydrogenation liquefaction of coal that it is generated are oily, and (usually coal hydrogenation is straight Connect liquefaction light oil) or direct hydrogenation liquefaction of coal oil modified oil, as long as its composition has raw material compositing characteristic of the present invention, To use the method for the present invention to be processed.
What patent CN100547055C stated clearly a kind of is pressed in lignite with the thermally dissolving and catalytic of lignite preparing liquid fuel is owned by France Add hydrogen direct liquefaction process, including direct hydrogenation liquefaction of coal reaction process and direct hydrogenation liquefaction of coal oil hydrogenation modification process totally two A process.In order to improve the conversion ratio of coal direct liquefaction and realize that coal feedstock enters direct hydrogenation liquefaction of coal reactor, coal Charcoal is usually made coal dust before entering direct hydrogenation liquefaction of coal reactor, is made into oily coal with the solvent naphtha for having good hydrogen supply capacity Slurry, coal is pressurized, enters direct hydrogenation liquefaction of coal reactor after heating.
Direct hydrogenation liquefaction of coal reaction process of the present invention is referred to coal and molecule hydrogen that may be present as original Material is hydrogen supply dissolvent oil with specific oil product (the usually hydrogenation modification oil of direct hydrogenation liquefaction of coal oil), in certain operation Condition (such as operation temperature, operating pressure, solvent naphtha/coal weight ratio, hydrogen/solvent naphtha volume ratio and suitable hydrogenation catalyst) Under, the reaction process of carbon-carbon bond thermal cracking, hydrogenation liquefaction directly occurs for coal.
Direct hydrogenation liquefaction of coal oil of the present invention, refers to the oil that the direct hydrogenation liquefaction of coal reaction process generates Product, it is present in Coal Liquefaction reaction effluent, is based on hydrogen supply dissolvent oil, reaction consumption coal and reaction transfer hydrogen Combined reaction product.
After direct hydrogenation liquefaction of coal reaction process works well, it is anti-that hydrogen supply dissolvent oil generallys use direct hydrogenation liquefaction of coal The hydrogenation modification oil for the direct hydrogenation liquefaction of coal oil (usually conventional distillate of the boiling range higher than 165 DEG C) for answering process self-produced, coal The main target for adding hydrogen direct liquefaction oil hydrogenation modification process is production direct hydrogenation liquefaction of coal reaction process solvent naphtha, specifically For be exactly improve in oil product " with good hydrogen supply function component " content, such as improve naphthenic base benzene class, bicyclic alkyl The content of benzene class component, the fact that a large amount of double ring arenes and a large amount of thrcylic aromatic hydrocarbons are contained based on direct hydrogenation liquefaction of coal oil, coal Adding hydrogen direct liquefaction oil hydrogenation modification process is the hydrogenation process of one " appropriate aromatic hydrocarbons saturation ".
The final goal of direct hydrogenation liquefaction of coal reaction process is the outer oil product supplied of production, usual direct hydrogenation liquefaction of coal oil The hydrogenation modification oil that hydrogenation modification process generates is two parts: a part is used as direct hydrogenation liquefaction of coal reaction process hydrogen supply Solvent naphtha, a part are used as the outer oil extraction of direct hydrogenation liquefaction of coal liquefaction process.In general, direct hydrogenation liquefaction of coal reaction process generates At least part direct hydrogenation liquefaction of coal light oil be used as the outer oil extraction A of coal oil process, remaining direct hydrogenation liquefaction of coal oil is used Make direct hydrogenation liquefaction of coal oil hydrogenation modification process feedstock oil production direct hydrogenation liquefaction of coal reaction process hydrogen supply dissolvent oil and There is the outer oil extraction of A and B two-way in outer oil extraction B, the final whereabouts of the outer oil extraction of A and B two-way is mentioned by deep hydrogenation at this time Matter process produces high-quality oil product such as diesel oil distillate, naphtha cut.
Up flow type expanded bed hydrogenator of the present invention, the basic element of character usually have:
1. reactor shell；
2. the opening (or being adapter tube) in reactor shell；
3. the up flow type being arranged in reactor enclosure body adds hydrogen main reaction space, usually using catalyst when working condition, Usually using charging distributed component for being uniformly distributed charging；
4. being arranged in the feed distributor of bottom in reactor enclosure body；
5. being arranged in the liquid collection cups LD and liquid conduits LK of upper section or middle upper section in reactor enclosure body；
6. reactor intermediate feed distributor (or distributor), the mixer of catalyst bed interlayer, such as cold hydrogen box；
7. rectification part is exported, such as collector, liquid phase discharge vortex-proof device, mixed phase product fairlead.
8. the measuring instrumentss that may be installed: testing the temperature-measuring part such as thermocouple of reaction bed temperature, measure reactor The pressure gauge of system specific location pressure measures liquid level instrument such as glass plate, floating drum, the double flange difference gauges, guided wave of liquid level Radar, ray level-sensing device etc.；
Up-flow reactor of the present invention, accessory are external insulation material, supporting element (skirt or trunnion), base Plinth, ladder, operating platform and fire-fighting accessory that may be present such as steam smothering ring.According to the conditions such as construction ground geology, meteorology, knot The conditions such as weight of equipment, height are closed, up-flow reactor of the present invention needs to drive piles to control under its basis as needed The sinking speed on its basis.
Up-flow reactor of the present invention, working method can choose:
1. floating bed hydrogenation reactor；
2. boiling bed hydrogenation reactor usually draws off the decreased catalysis of activity from bed bottom in an intermittent fashion Agent fills into fresh catalyst from bed top in an intermittent fashion and maintains bed catalyst reserve；
3. slight expanded-bed.
About hydrocarbon material hydrogen addition technology, use can be reasonably selected to prior art or is used cooperatively.
For direct hydrogenation liquefaction of coal reaction process, in order to reduce liquefying reactor rear portion system corrosion, Ke Nengxu Sodium carbonate is injected, into final reacting product to neutralize corrosive component such as hydrogen chloride, hydrogen fluoride, hydrogen sulfide etc., Jiang Qiyin Ion is fixed.
The present invention, the gas phase of the initial reaction product of the heavy-oil hydrogenation heat cracking reaction process high particularly suitable for fragrant charcoal rate The utilization of interior middle matter hydrocarbon, because matter hydrocarbon is usually enriched the virtue of the high the hydrocarbon component of arene content and/or partial hydrogenation saturation in these The hydrocarbon component, these components have the following characteristics that
1. the liquid phase of aromatic hydrocarbons component can dissolve colloid, the asphalitine of the generation of heat from hydrogenation cracking process, prevent them poly- Collection condensation green coke；
2. the liquid phase of aromatic hydrocarbons component, higher to the solubility of hydrogen, conducive to hydrogen to goal response object heavy hydrocarbon component Transmitting；
3. the aromatic component of partial hydrogenation saturation, belongs to hydrogen supply hydrocarbon.
The present invention, the gas phase of the initial reaction product of the high heavy-oil hydrogenation heat cracking reaction process of particularly suitable virtue charcoal rate The utilization of interior middle matter hydrocarbon, can constitute online circulation hydrogen supply dissolvent low cost production, and major part or even whole hydrogen supply dissolvents The hydro carbons of reaction product of the preceding biology from heat from hydrogenation cracking reaction process RU.
Hydrogen supply hydrocarbon described herein refers to that direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation reaction process, kerosene refine altogether In hydrogenation process with hydrogen supply function the hydrocarbon component, hydrogen supply hydrocarbon include the double ring arene of fractional saturation, fractional saturation it is more Cycloaromatics.In hydrogen supply hydrocarbon, the hydrogen supply speed of dihydro body is all larger than tetrahydro body, the dihydro body of thrcylic aromatic hydrocarbon and the dihydro of double ring arene Body is compared, and it is low that hydrogen supply speed has height to have；Although test is it has been proved that polycyclic aromatic hydrocarbon has the energy of transmitting hydrogen without hydrogen supply capacity Power.At 400 DEG C, the opposite hydrogen supply speed of following component is as follows:
Characteristic of the invention is described below.
The stabilized hydrogenation object reuse method of middle matter hydrocarbon, feature in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention It is to comprise the steps of:
(1) in hydrocarbon material hydrogenation process RU, there are hydrogen, conventional liq hydrocarbon, there may be solid particles simultaneously Under the conditions of mixed phase material, hydrogenation reaction RU-R at least is carried out containing the first raw material RU-F1 of carbon and protium and is converted into most Whole hydrogenation reaction product RU-P；Recycle final hydrogenation reaction product RU-P；
First raw material RU-F1 includes liquid material RU-F1L and solid particulate materials RU-F1S that may be present；
Hydrogenation reaction RU-R, the hydrofining reaction comprising at least part liquid material RU-F1L include at least one The hydrocracking reaction for dividing liquid material RU-F1L, the stabilized hydrogenation comprising the free radical that at least part heat cracking reaction generates Reaction may include the hydrogenation liquefaction reaction of at least part solid particulate materials RU-F1S that may be present；
Hydrogenation reaction RU-R may use catalyst RU-CAT；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon for the hydrocarbon component for being 230~400 DEG C containing normal boiling point is used；
In hydrocarbon material hydrogenation process RU, the external of the hydrogen supply hydrocarbon SH for being 230~400 DEG C containing normal boiling point may be used Hydrogen supply hydrocarbon OUT-TO-RU-DS；
In hydrocarbon material hydrogenation process RU, it is possible to create the hydrogen supply the hydrocarbon component RU- that normal boiling point is 230~400 DEG C PRO-DSC；
Hydrocarbon material hydrogenation process RU uses hydrogenator RU-XE, final hydrogenation reaction product RU-P, to contain hydrogen Gas, conventional liq hydrocarbon simultaneously may the mixed phase material containing solid particle, with 1 tunnel or 2 tunnels or multichannel when leaving reactor RU-XE The form of material RU-P-X occurs, and material RU-P-X is gas phase or liquid phase or gas-liquid mixed phase or gas-liquid-solid three-phase logistics；
In hydrocarbon material hydrogenation process RU, setting may include at least two reaction of the serial operation of the liquid material of solid Section；
One conversion zone refers to that the gas-liquid separation comprising liquid material hydrogenation reaction step and the step gas-liquid product walks Rapid technical process；
The front conversion zone RUA of the hydrocarbon material hydrogenation process RU, refers to hydrocarbon material hydrogenation process RU's Any upstream reaction section of the last one conversion zone RUJ or whole upstream reaction sections；
In hydrocarbon material hydrogenation process RU, at least 2 hydrogenator RU-XE are used；
Separating liquid RUAP-HS-L is separated into separation process RUAP-HS, at least part leading portion hydrogenation reaction product RUAP With the separation gas RUAP-HS-V for the hydrocarbon component for being 230~400 DEG C containing normal boiling point；
Separating liquid RUAP-HS-L is converted into rear portion reaction product RUBP into rear portion conversion zone RUB；
The logistics of the hydrocarbon component that containing normal boiling point is 230~400 DEG C of at least part based on separation gas RUAP-HS-V Used as material MR-F, it is understood that there may be residual gas RUAP-HS-V used as material RUAP-HS-V-BYPASS；
(2) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR- F is converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, and the hydro carbons in material MR-F carries out the portion of aromatic hydrocarbons Divide plus hydrogen saturated reaction MRR is converted into hydrogen supply the hydrocarbon component MR-DS；
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Recycle hydrocarbons MR-KRDS enters hydrocarbon material hydrogenation process RU；
At least part recycle hydrocarbons MR-KRDS returns to hydrocarbon material hydrogenation process RU's as MR-KRDS-TO-RUA Front reaction zone RUA participates in hydrocarbon material hydrogenation reaction RUA-R.
The present invention, in general, using at least 2 hydrogenator RU-XE, at least 1 in hydrocarbon material hydrogenation process RU Hydrogenator is up flow type expanded bed hydrogenator.
The present invention, common operation target is: the hydro carbons in return course TLOOP, recycle hydrocarbons MR-KRDS is in weight Mainly it is made of the hydrocarbon component that normal boiling point is 230~400 DEG C.
The present invention can be with simultaneous processing hydrogen supply hydrocarbon precursor MR-FK in stabilized hydrogenation reaction process MR；
In stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, hydrogen supply hydrocarbon predecessor Object MR-FK, material MR-F are converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, in material MR-F The partial hydrogenation saturated reaction MRR that hydro carbons carries out aromatic hydrocarbons is converted into hydrogen supply the hydrocarbon component MR-DS.
The present invention, in hydrocarbon material hydrogenation process RU, the hydrogenator of front conversion zone RUA and separation process The equipment that RUAP-HS is used, can be mutually indepedent.
The present invention, in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA, which has, to be produced Object part takes off liquid separation function, obtains separating liquid and gas-liquid mixed phase material, and separation process RUAP-HS can be in front conversion zone It is carried out in last hydrogenator of RUA.
The present invention, in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA, which has, to be produced The clear separation function of object gas-liquid, obtain separating liquid and separation gas, separation process RUAP-HS can front conversion zone RUA most It is carried out in latter hydrogenator.
The present invention, in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA, which has, to be produced The clear separation function of object gas-liquid, obtain separating liquid and separation gas, separation process RUAP-HS front conversion zone RUA last It is carried out in platform hydrogenator, last hydrogenator mode of operation can be gas-liquid counter current operation mode.
The present invention can be used as object based on separation gas RUAP-HS-V at least partially in hydrocarbon material hydrogenation process RU Expect that MR-F is used.
The present invention, the operation mode for obtaining material MR-F may is that
(1) in hydrocarbon material hydrogenation process RU, thermal high separation is entered based on separation gas RUAP-HS-V at least partially Process AP-HS is separated into hot high score gas AP-HS-V and hot high score oil AP-HS-L；
The logistics of the hydrocarbon component that containing normal boiling point is 230~400 DEG C of at least part based on hot high score oil AP-HS-L It is used as material MR-F.
The present invention, the operation mode for obtaining material MR-F may is that
(1) in hydrocarbon material hydrogenation process RU, thermal high separation is entered based on separation gas RUAP-HS-V at least partially Process AP-HS is separated into hot high score gas AP-HS-V and hot high score oil AP-HS-L；
The logistics of the hydrocarbon component that containing normal boiling point is 230~400 DEG C of at least part based on hot high score gas AP-HS-V It is used as material MR-F.
The present invention, the operation mode for obtaining recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
At least part stabilized hydrogenation reaction product MRP is used as recycle hydrocarbons MR-KRDS.
The present invention, the operation mode for obtaining recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Stabilized hydrogenation reaction product MRP is separated, the liquid for the hydrogen supply the hydrocarbon component for being 230~400 DEG C containing normal boiling point is obtained State logistics XXK, the logistics at least partially based on liquid stream XXK are used as recycle hydrocarbons MR-KRDS.
The present invention, the operation mode for obtaining recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Stabilized hydrogenation reaction product MRP is separated, the gas for the hydrogen supply the hydrocarbon component for being 230~400 DEG C containing normal boiling point is obtained State logistics YYK, the logistics at least partially based on gaseous stream YYK are used as recycle hydrocarbons MR-KRDS.
The circulate operation mode of the present invention, recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
At least part recycle hydrocarbons MR-KRDS enters hydrocarbon material hydrogenation process RU after mixing with the first raw material RU-F1.
The circulate operation mode of the present invention, recycle hydrocarbons MR-KRDS may is that
(3) in return course TLOOP, it is containing normal boiling point based on stabilized hydrogenation reaction product MRP at least partially The logistics of 230~400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
First raw material RU-F1 of at least part recycle hydrocarbons MR-KRDS and at least part solid powder shape is mixed into slurry After material, into hydrocarbon material hydrogenation process RU.
The present invention, operation target may is that
(1) hydrogen supply hydrocarbon RUA-DS is used in front conversion zone RUA in hydrocarbon material hydrogenation process RU；
Leading portion hydrogenation reaction RUA-R, uses catalyst RUA-CAT；
(3) hydro carbons in return course TLOOP, recycle hydrocarbons MR-KRDS.In weight mainly by normal boiling point be 230 ~400 DEG C of the hydrocarbon component composition.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU.
The present invention, operation target may is that
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is lower than hydrogenation reaction product RUAP 0~1.0MPa of operating pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is 350~480 DEG C.
The present invention, operation target may is that
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is lower than hydrogenation reaction product RUAP 0~0.5MPa of operating pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is 400~450 DEG C.
The present invention, operation target may is that
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is lower than hydrogenation reaction product RUAP 0~1.0MPa of operating pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, than hydrogenation reaction product RUAP's 5~80 DEG C of low operation temperature.
The present invention, operation target may is that
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is lower than hydrogenation reaction product RUAP 0~1.0MPa of operating pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, in the item for guaranteeing material noncoking Under part, the difference DT of operation temperature and the operation temperature of hydrogenation reaction product RUAP is small as far as possible.
The present invention, operation target may is that
(1) in hydrocarbon material hydrogenation process RU, setting may include 2 or multiple of the serial operation of the liquid material of solid Conversion zone wherein be existed between conversion zone in the presence of the series flow for the liquid material that may include solid with the liquid material that may include solid Flowing between conversion zone is forward direction, the type of flow classification of hydrogen material between conversion zone, a kind or several selected from following manner Kind:
1. hydrogen material flows to cocurrent in the same direction with the main body of serum materials, belong to liquid, gas cocurrent tandem reactor process；
2. slurry series connection, tandem reactor process of the hydrogen short circuit across stream；
3. gas-phase product does not enter the reaction process of other any conversion zones there are at least one conversion zone, gas is former Material do not use the hydrogen from other any conversion zones, belong to there are hydrogen material parallel operation reaction process；
4. reaction process receives the hydrogen product of downstream reaction section there are at least one conversion zone, belong in conversion zone Between there are the reaction process of hydrogen gas product counter-current operation.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, using by normal boiling point being mainly 230~400 DEG C The hydrogen supply hydrocarbon TO-RUA-DS of hydro carbons composition.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen supply hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V is used as material MR-F.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen supply hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
Warm high pressure separate section RUAP-HS-V-MS is set, separation gas RUAP-HS-V is separated into gas RUAP-HS-V- MS-V and separating liquid RUAP-HS-V-MS-L；The hydrocarbon for being 230~400 DEG C containing normal boiling point in separating liquid RUAP-HS-V-MS-L Component；
At least part separating liquid RUAP-HS-V-MS-L is used as material MR-F.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen supply hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
It is set using the warm high pressure separate section RUAP-HS-V-MS of gas stripping gas RUAP-HS-V-MS-BH, gas will be separated RUAP-HS-V is separated into gas RUAP-HS-V-MS-V and separating liquid RUAP-HS-V-MS-L；
Separating liquid RUAP-HS-V-MS-L and gas stripping gas RUAP-HS-V-MS-BH completes to separate, and is separated into air lift row The gentle extract RUAP-HS-V-MS-L-BL of deflation RUAP-HS-V-MS-L-BV；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid RUAP-HS-V-MS-L-BL；
At least part air lift liquid RUAP-HS-V-MS-L-BL is used as material MR-F.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen supply hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
It is set using the warm high pressure separate section RUAP-HS-V-MS of gas stripping gas RUAP-HS-V-MS-BH, gas will be separated RUAP-HS-V is separated into gas RUAP-HS-V-MS-V and separating liquid RUAP-HS-V-MS-L；
Separating liquid RUAP-HS-V-MS-L and gas stripping gas RUAP-HS-V-MS-BH completes to separate, and is separated into air lift row The gentle extract RUAP-HS-V-MS-L-BL of deflation RUAP-HS-V-MS-L-BV；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid RUAP-HS-V-MS-L-BL；
At least part air lift liquid RUAP-HS-V-MS-L-BL is used as material MR-F；
(3) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR- F is converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, and the hydro carbons in material MR-F carries out the portion of aromatic hydrocarbons Divide plus hydrogen saturated reaction MRR is converted into hydrogen supply the hydrocarbon component MR-DS；
(4) separation is separated into the separation process MRP-S using gas stripping gas MRP-S-BH, stabilized hydrogenation reaction product MRP The separating liquid MRP-L of gas MRP-V and the hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point；
Separating liquid MRP-L and gas stripping gas MRP-S-BH completes to separate, and it is gentle to be separated into air lift discharge gas MRP-L-BV Extract MRP-L-BL；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid MRP-L-BL；
Material of at least part based on air lift liquid MRP-L-BL is used as recycle hydrocarbons MR-KRDS.
The present invention, operation target may is that
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation reaction States of matter is the hydrocarbon powder of solid particle when the reactor of process RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, using by normal boiling point being mainly 230~400 DEG C The hydrogen supply hydrocarbon TO-RUA-DS of hydro carbons composition；
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V is used as material MR-F, existing residual gas RUAP-HS-V conduct Material RUAP-HS-V-BYPASS is used；
Material RUAP-HS-V-BYPASS enters separation process, is separated into gas RUAP-HS-V-BYPASS-V and containing normal Advise the lime set RUAP-HS-V-BYPASS-L for the hydrocarbon component that boiling point is 230~400 DEG C；
At least part lime set RUAP-HS-V-BYPASS-L, into hydrocarbon material hydrogenation process RU；
At least part lime set RUAP-HS-V-BYPASS-L returns to the front reaction zone of hydrocarbon material hydrogenation process RU RUA participates in hydrocarbon material hydrogenation reaction RUA-R.
The present invention, operation target when processing hydrocarbon powder RU-F1S may is that
(1) hydrocarbon material hydrogenation process RU adds hydrogen direct liquefaction reaction process RU for the hydrocarbon powder RU-F1S of raw material, 2 or multiple conversion zones of slurries serial operation are set；
One conversion zone refers to that the gas-liquid separation comprising slurry hyd reaction step and the step gas-liquid product walks Rapid technical process；
The front conversion zone RUA refers to any conversion zone in the upstream of the last one conversion zone or whole upstream reactions Section；
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, there are hydrogen, include conventional liq hydrocarbon, the carbon of hydrogen supply hydrocarbon Hydrogen powder and there may be under conditions of catalyst, carry out at least part hydrocarbon powder RU-F1S's plus hydrogen direct liquefaction it is anti- It answers RU-R to be converted into hydrocarbon powder and adds hydrogen direct liquefaction final reacting product RU-P；Final hydrogenation reaction product RU-P, be 1 tunnel or 2 tunnels or multichannel material；Recycle final hydrogenation reaction product RU-P；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon TO-RU- for the hydro carbons for being 230~400 DEG C containing normal boiling point is used DS；
In front conversion zone RUA, the hydrogen supply hydrocarbon RUA-DS for the hydro carbons for being 230~400 DEG C containing normal boiling point is used；
Add the front conversion zone RUA of hydrogen direct liquefaction reaction process RU in hydrocarbon powder, there are hydrogen, include hydrogen supply hydrocarbon Conventional liq hydrocarbon, hydrocarbon powder and there may be under conditions of catalyst, hydrocarbon powder RU-F1S carries out at least part Hydrocarbon powder adds hydrogen direct liquefaction front reaction RUA-R to be converted into hydrocarbon powder and adds hydrogen direct liquefaction front reaction product RUAP； Front reaction product RUAP is 1 tunnel or 2 tunnels or multichannel material；
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU, in the same of recycle hydrocarbons MR-KRDS of the processing from step (5) When, other hydrogen supply dissolvent oil BDS and hydrocarbon powder KS can be capable of processing；
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V used as material MR-F, it is understood that there may be residual gas RUAP-HS-V It is used as material RUAP-HS-V-BYPASS；
(3) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR- F is converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, and the hydro carbons in material MR-F carries out the portion of aromatic hydrocarbons Divide plus hydrogen saturated reaction MRR is converted into hydrogen supply the hydrocarbon component MR-DS；
(4) separation gas MRP-V is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP and contain normal boiling point For the separating liquid MRP-L of 230~400 DEG C of hydrogen supply the hydrocarbon component MR-DS；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
(5) enter hydrocarbon material hydrogenation process RU in return course TLOOP, recycle hydrocarbons MR-KRDS；
At least part recycle hydrocarbons MR-KRDS returns to hydrocarbon material hydrogenation process RU's as MR-KRDS-TO-RUA Front reaction zone RUA participates in hydrocarbon material hydrogenation reaction RUA-R.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
Material of a part based on separating liquid MRP-L, the rear portion for going hydrocarbon powder to add hydrogen direct liquefaction reaction process RU are anti- Answering a section RUB contact slurry to carry out hydrocarbon powder adds hydrogen direct liquefaction to react.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, at least two conversion zone of slurries serial operation is set, wherein There are the series flows of slurry between conversion zone, are forward direction, hydrogen object between conversion zone with flowing of the slurry between conversion zone The type of flow of material is classified, and a kind or several of following manner can be selected from:
1. hydrogen material flows to cocurrent in the same direction with the main body of serum materials, belong to liquid, gas cocurrent tandem reactor process；
2. slurry series connection, tandem reactor process of the hydrogen short circuit across stream；
3. gas-phase product does not enter the reaction process of other any conversion zones there are at least one conversion zone, gas is former Material do not use the hydrogen from other any conversion zones, belong to there are hydrogen material parallel operation reaction process；
4. reaction process receives the hydrogen product of downstream reaction section there are at least one conversion zone, belong in conversion zone Between there are the reaction process of hydrogen gas product counter-current operation.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, slurries raw material is when the reaction of front conversion zone RUA stops Between account for slurries raw material and add the 30~65% of the general reaction residence time of hydrogen direct liquefaction reaction process RU in whole hydrocarbon powder.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Most of hydro carbons in separating liquid MRP-L, can be selected from a kind or several in following conventional boiling range:
1. the conventional liquid hydrocarbon that normal boiling point is 230~400 DEG C；
2. the conventional liquid hydrocarbon that normal boiling point is 230~350 DEG C；
3. the conventional liquid hydrocarbon that normal boiling point is 230~300 DEG C.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
The weight of recycle hydrocarbons MR-KRDS is the 5~95% of separating liquid MRP-L weight.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(5) add hydrogen direct liquefaction anti-by hydrocarbon powder in return course TLOOP, at least part recycle hydrocarbons MR-KRDS Answering whole main body reaction compartments of the first reactor of the first conversion zone of process RU to carry out hydrocarbon powder adds hydrogen direct liquefaction anti- It answers.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(5) go hydrocarbon powder that hydrogen direct liquefaction is added to react in return course TLOOP, at least part recycle hydrocarbons MR-KRDS Process RU
Contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react, working method, can selected from one of the following or It is several:
1, at least part recycle hydrocarbons MR-KRDS are selected, the front that gravity flow returns to direct hydrogenation liquefaction of coal reaction process is anti- Section is answered, contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
2, at least part recycle hydrocarbons MR-KRDS are selected, the front conversion zone of direct hydrogenation liquefaction of coal reaction process is returned Contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
3, at least part recycle hydrocarbons MR-KRDS is selected to return to direct hydrogenation liquefaction of coal reaction process after heat exchange heating Front conversion zone, contact slurry carry out hydrocarbon powder and hydrogen direct liquefaction are added to react；
Selection 4, at least part recycle hydrocarbons MR-KRDS are used as coal slurry and prepare solvent naphtha configuration coal slurry MKDS-MJ, then coal Slurry MKDS-MJ enters direct hydrogenation liquefaction of coal reaction process, carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
Selection 5, at least part recycle hydrocarbons MR-KRDS are used as coal slurry and prepare solvent naphtha configuration coal slurry MKDS-MJ, then coal Slurry MKDS-MJ enters the front conversion zone of direct hydrogenation liquefaction of coal reaction process, carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
6, at least part recycle hydrocarbons MR-KRDS are selected, the washing oil in washing step DW, as gas RUAP-HS-V Using to wash the dust in abjection gas RUAP-HS-V；It, will be in gas RUAP-HS-V while completing to wash dedirt Some hydrocarbon is condensed into liquid phase DWL；
At least part liquid phase DWL returns to direct hydrogenation liquefaction of coal reaction process, and contact slurry carries out hydrocarbon powder and adds hydrogen Direct liquefaction reaction；
7, at least part recycle hydrocarbons MR-KRDS are selected, the washing oil in washing step DW, as gas RUAP-HS-V Using to wash the dust in abjection gas RUAP-HS-V；It, will be in gas RUAP-HS-V while completing to wash dedirt Some hydrocarbon is condensed into liquid phase DWL；
At least part liquid phase DWL returns to the front conversion zone of direct hydrogenation liquefaction of coal reaction process, and contact slurry carries out Hydrocarbon powder adds hydrogen direct liquefaction to react；
8, at least part liquid phase DWL are selected, direct hydrogenation liquefaction of coal reaction process contact slurry is returned and carries out hydrocarbon powder Before material plus the reaction of hydrogen direct liquefaction, it is used as Conduit rinse oil or pump flushing oil or instrument flushing oil.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
At least part recycle hydrocarbons MR-KRDS is used as hydrocarbon powder slurry preparation solvent naphtha and configures hydrocarbon powder slurry MR- KRDS-MJ, then hydrocarbon powder slurry MR-KRDS-MJ enters hydrocarbon powder and adds hydrogen direct liquefaction reaction process RU-RU, carries out carbon Hydrogen powder adds hydrogen direct liquefaction to react, and working method can be selected from one of the following or several:
1, recycle hydrocarbons MR-KRDS are selected, hydrocarbon powder slurry MR-KRDS- is prepared after mixing with other hydrogen supply dissolvent oil BDS BDS-MJ, hydrocarbon powder slurry MR-KRDS-BDS-MJ are used as hydrocarbon powder and starch MR-KRDS-MJ；
2, recycle hydrocarbons MR-KRDS are selected, hydrocarbon powder slurry preparation solvent naphtha is used alone as and configures hydrocarbon powder slurry MR- KRDS-MJ；
Other hydrogen supply dissolvent oil BDS prepare hydrocarbon powder and starch BDS-MJ.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
At least part recycle hydrocarbons MR-KRDS is used alone as hydrocarbon powder slurry preparation solvent naphtha and configures hydrocarbon powder slurry MR- KRDS-MJ；
Other hydrogen supply dissolvent oil BDS prepare hydrocarbon powder and starch BDS-MJ；
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the reaction time of hydrocarbon powder slurry MR-KRDS-MJ with The reaction time of hydrocarbon powder slurry BDS-MJ is not identical.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In washing process BW10, separates gas RUAP-HS-V and at least contacted 1 time with wash cooling liquid CWL, separate gas RUAP- At least part hydrocarbon gas in HS-V is changed into hydrocarbon liquid and enters in rich cleaning solution BW10-L, leaves washing process BW10 discharge gas BW10-V；The weight flow of rich cleaning solution BW10-L is greater than the weight flow of wash cooling liquid CWL；
At least part gas BW10-V is used as material MR-F.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In washing process BW10, separates gas RUAP-HS-V and at least contacted 1 time with wash cooling liquid CWL, separate gas RUAP- At least part hydrocarbon gas in HS-V is changed into hydrocarbon liquid and enters in rich cleaning solution BW10-L, leaves washing process BW10 discharge gas BW10-V；The weight flow of rich cleaning solution BW10-L is greater than the weight flow of wash cooling liquid CWL；
Rich cleaning solution BW10-L, whereabouts can be selected from one of the following or several:
1. being mixed into separating liquid RUAP-HS-L；
2. conversion zone RUA before going；
3. removing rear conversion zone RUB；
4. hydrocarbon powder process with slurry is gone to make to use with slurry solvent.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) in washing process BW10, the contact separation mode of operation of gas RUAP-HS-V and wash cooling liquid CWL are separated, it can Selected from one of the following or several:
1. separating after mixing, 1 contact, 1 separation is carried out；
2. counter current contacting carries out 2 contacts and 2 separation；
3. counter current contacting carries out multiple-contact and separating for several times.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) separation process RUAP-HS is carried out, most in last hydrogenator of leading portion hydrogenation process RUA Latter hydrogenator is unit equipment.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, hydrocarbon powder RU-F1S can a kind in following or It is several:
1. coal dust；
2. molding powder；
3. rubber powder；
4. direct hydrogenation liquefaction of coal reaction process RU mixes other hydrocarbon powders of refining.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, it is understood that there may be a kind or several in following of solid:
1. coal dust；
2. catalyst solid particle；
3. sulphur powder；
4. hydrocarbon ils coking material carrier semicoke particle；
5. molding powder；
6. rubber powder；
7. other solid powders that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to need to input.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process, can be selected from following work 1 kind or several during skill:
1. using the direct hydrogenation liquefaction of coal liquefaction process of hydrogen supply dissolvent oil；
2. not using the direct hydrogenation liquefaction of coal liquefaction process of hydrogen supply dissolvent oil；
3. kerosene refines process altogether；
4. coal faces hydrogen thermosol liquefaction process.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the hydrocarbon powder used adds hydrogen direct liquefaction reactor XRUE Working method can a kind or several in following:
1. suspended-bed reactor, that is, paste state bed reactor；
2. fluidized bed reactor；
3. suspension bed and ebullated bed combination type reactor.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the hydrocarbon powder used adds hydrogen direct liquefaction reactor XRUE Working method, can a kind or several in following:
Option 1, liquid material and gas material use the counter-current reactor of pure adverse current working method；
Option 2, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump Answer the fluidized bed reactor of device XRUE material inlet；
Option 3, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump Answer the suspended-bed reactor of device XRUE material inlet；
Option 4, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of device XRUE material inlet is answered, while circulating pump conveys circulation fluid, downstream transport liquid material product；
Option 5, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of device XRUE material inlet is answered, while circulating pump conveys circulation fluid, downstream transport liquid material product；
Option 6, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor for answering device XRUE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；
Option 7, reactor XRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor for answering device XRUE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；
Option 8, reactor XRUE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport liquid Expect product, is not provided with the fluidized bed reactor system of liquid material product forced circulation；
Option 9, reactor XRUE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport liquid Expect product, is not provided with the suspended-bed reactor system of liquid material product forced circulation；
Option 10, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor XRUE material inlet and the combination type reactor of ebullated bed；
Option 11, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor XRUE material inlet and the combination type reactor of ebullated bed, while circulating pump conveys circulation fluid, downwards Trip conveying liquid material product；
Option 12, reactor XRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor XRUE material inlet and the combination type reactor of ebullated bed are collected simultaneously other collection liquids warp of cup discharge Cross other dedicated feeding engine downstream transport liquid material products；
The suspended-bed reactor system of flow pattern under the center upstream surrounding of internal guide cylinder is arranged in option 13；
The suspended-bed reactor system of flow pattern in the dirty surrounding in center of internal guide cylinder is arranged in option 14；
Option 15, empty cylinder bubbling bed suspended-bed reactor system；
Option 16 is formed reactor top reaction zone liquid phase and is flowed down under Returning reactor using the external circulation pipe of reactor The device outside circulation of portion's reaction zone.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, conversion zone obtains the mode of product slurry, can be selected from down State a kind or several in mode:
1. the slurries that the gas-liquid separation process of autoreaction section reaction product is discharged, as final reaction section product slurry；
2. the final reactor of conversion zone uses pure counter-current reactor, the bottom liquid phase region of the final reactor of autoreaction section The slurries of discharge, as conversion zone product slurry；
3. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup warp in the final reactor of autoreaction section The slurries of diversion pipe discharge, as conversion zone product slurry；
4. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup warp in the final reactor of autoreaction section The slurries of diversion pipe discharge, as slurry to be de-gassed；
Slurry to be de-gassed is separated into the liquid stream rich in bubble, the liquid stream that lean gas steeps all the way all the way by cyclonic separation step；
The liquid stream of lean gas bubble, is used as conversion zone product slurry.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Add hydrogen direct liquefaction reaction process RU, last hydrogenator RU19 of the first conversion zone in hydrocarbon powder, The reactor that there is part to take off liquid function of liquid collecting cup is set for top, and collection liquid RU19-DL-L derived from liquid collecting cup is as the One conversion zone product slurry, whereabouts can be selected from one of the following or several:
1. going the reaction step of the second conversion zone；
2. removing the gas-liquid separator of the first conversion zone product slurry, it is separated into degassing slurries and gas；
3. going the first conversion zone cyclic process；
4. portion collection liquid RU19-DL-L removes separation and recovery system after dropping valve is depressured.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
In separation and recovery process SYS300, recycles final hydrogenation reaction product RU-P and obtain hydrogen rich gas gas RH, at least one Part hydrogen rich gas gas RH returns to hydrocarbon powder and hydrogen direct liquefaction reaction process RU is added to be used as circulating hydrogen.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
The working method of separation and recovery process SYS300, hydrogen upgrading process H2UPU, H2UPU comprising hydrogen material can Selected from one of the following or several:
1. using membrane separation process concentrate hydrogen；
2. using PSA pressure swing adsorption technique concentrate hydrogen；
3. using deep cooling process for separating concentrate hydrogen.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
In separation and recovery process SYS300, recycles final hydrogenation reaction product RU-P and obtain hydrogen rich gas gas RH, work Mode can be selected from one of the following or several:
1. thermal high separation process RU-P-THPS, cold anticyclone separation process is arranged in separation and recovery process SYS300 CHPS；
Hot high score gas RU-P- is separated into thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P THPS-V and hot high score liquid material RU-P-THPS-L；
Cold high score gas CHPS-V and cold high score are separated into cold anticyclone separation process CHPS, hot high score gas RU-P-THPS-V Liquid material CHPS-L；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH；
2. in separation and recovery process SYS300, setting thermal high separation process RU-P-THPS, warm high pressure separation process MHPS, cold anticyclone separation process CHPS；
Hot high score gas RU-P- is separated into thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P THPS-V and hot high score liquid material RU-P-THPS-L；
Warm high score gas MHPS-V and Wen Gaofen are separated into warm high pressure separation process MHPS, hot high score gas RU-P-THPS-V Liquid material MHPS-L；
Cold high score gas CHPS-V and cold high score liquid material are separated into cold anticyclone separation process CHPS, warm high score gas MHPS-V CHPS-L；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH；
3. the thermal high separation process RU-P- with gas condensation collection step LCD is arranged in separation and recovery process SYS300 THPS, cold anticyclone separation process CHPS；
Hot high score gas RU-P- is first separated into thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P THPS-V and hot high score liquid material RU-P-THPS-L；Hot high score gas RU-P-THPS-V, in gas condensation collection step LCD cooling point From for condensate liquid LCD-L and de- liquid gas LCD-V；
Cold high score gas CHPS-V and cold high score liquid material CHPS- are separated into cold anticyclone separation process CHPS, de- liquid gas LCD-V L；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(2) separation gas RUAP-HS-V and separation are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP Liquid RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In separation process RUAP-HS, stripping step BH-S, which is arranged, using gas stripping gas BH makes leading portion hydrogenation reaction product The hydrocarbon component vapour based on hydrogen supply dissolvent oil that at least part normal boiling point in the liquid phase RUAP-L of RUAP is 230~400 DEG C Change and enter in separation gas RUAP-HS-V, increases the weight for the hydro carbons that normal boiling point is 230~400 DEG C in separation gas RUAP-HS-V Flow.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(1) add the working method of hydrogen direct liquefaction reaction process RU, stripping step BH-S in following in hydrocarbon powder One or more:
1. being mixed with gas stripping gas BH with the gas-liquid mixed phase product RUAP of front reaction zone, the hydro carbons in air lift slurries；
2. being contacted with gas stripping gas BH with the pure product slurry RUAP-LP of front reaction zone；
3. dividing front reaction process RUA to 2 grades of formula front reaction process RUA1, RUA2 for slurries serial operation, front The gas RUA1-P- for the hydrocarbon component based on hydrogen supply dissolvent oil that reaction process RUA1 discharge is 230~400 DEG C containing normal boiling point The gas for the hydrocarbon component based on hydrogen supply dissolvent oil that XV, front reaction process RUA2 discharge are 230~400 DEG C containing normal boiling point RUA2-P-XV, gas RUA1-P-XV and/or gas RUA2-P-XV are used as separation gas RUAP-HS-V.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(1) the gas stripping gas BH, Ke Yixuan for adding hydrogen direct liquefaction reaction process RU, stripping step BH-S to use in hydrocarbon powder From one or more of following materials:
1. the new hydrogen that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
2. the circulating hydrogen that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
3. the circulating hydrogen after the hydrogen upgrading that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
4. adding in hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the front reaction zone of product slurry RUA-LP is discharged The hydrogen rich gas material of the reaction zone discharge in downstream or its derivative gas；
5. hydrocarbon powder adds the matched hydrogen supply dissolvent in addition to MR reaction process of hydrogen direct liquefaction reaction process RU to add hydrogen Stablize hydrogen rich gas gas or its derivative gas that the reaction product of reaction process is isolated；
6. hydrocarbon powder adds the matched hydrocarbon powder liquefaction oil of hydrogen direct liquefaction reaction process RU to add hydrogen upgrading reaction process The hydrogen rich gas gas isolated of reaction product or its derive gas.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
(4) in separation and recovery process SYS700, separation process MRP-S is set, stabilized hydrogenation reaction product MRP is separated into point From gas MRP-V and separating liquid MRP-L；
Separation and recovery process SYS700, working method are selected from one of the following or several:
1. thermal high separation process MRP-THPS is arranged in separation and recovery process SYS700；
Hot high score gas MRP-THPS-V is separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP With hot high score liquid material MRP-THPS-L；
Based on hot high score liquid material MRP-THPS-L, separating liquid MRP-L is obtained；
2. thermal high separation process MRP-THPS, cold anticyclone separation process MRP- is arranged in separation and recovery process SYS700 CHPS；
Hot high score gas MRP-THPS-V is separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP With hot high score liquid material MRP-THPS-L；
Cold anticyclone separation process MRP-CHPS, hot high score gas MRP-THPS-V be separated into cold high score gas MRP-CHPS-V and Cold high score liquid material MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or cold high score liquid material MRP-CHPS-L, separating liquid MRP-L is obtained；
3. in separation and recovery process SYS700, setting thermal high separation process MRP-THPS, warm high pressure separation process MRP- MHPS, cold anticyclone separation process MRP-CHPS；
Hot high score gas MRP-THPS-V is separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP With hot high score liquid material MRP-THPS-L；
Warm high pressure separation process MRP-MHPS, hot high score gas MRP-THPS-V be separated into warm high score gas MRP-MHPS-V and Warm high score liquid material MRP-MHPS-L；
Cold anticyclone separation process MRP-CHPS, warm high score gas MRP-MHPS-V be separated into cold high score gas MRP-CHPS-V and Cold high score liquid material MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or warm high score liquid material MRP-MHPS-L, separating liquid MRP-L is obtained；
4. the thermal high separation process with gas condensation collection step MRP-LCD is arranged in separation and recovery process SYS700 MRP-THPS, cold anticyclone separation process MRP-CHPS；
Hot high score gas MRP-THPS- is first separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP V and hot high score liquid material MRP-THPS-L；Hot high score gas MRP-THPS-V, in gas condensation collection step MRP-LCD cooling separation For condensate liquid MRP-LCD-L and de- liquid gas MRP-LCD-V；
Cold high score gas MRP-CHPS-V and cold high score are separated into cold anticyclone separation process CHPS, de- liquid gas MRP-LCD-V Liquid material MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or condensate liquid MRP-LCD-L, separating liquid MRP-L is obtained.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU, in the slurries MR-KRDS- that fabrication cycles hydrocarbon MR-KRDS is prepared While MJ, process the slurries BDS-MJ that other hydrogen supply dissolvent oil BDS are prepared, working method can in following one Kind:
1. slurries MR-KRDS-MJ, slurries BDS-MJ enter hydrocarbon powder and add hydrogen direct liquefaction reaction process RU after mixing Reactor in；
2. slurries MR-KRDS-MJ, slurries BDS-MJ, add that hydrogen direct liquefaction reaction process RU's is same into hydrocarbon powder In the same reaction space of a reactor；
3. positive on the basis of flowing through the main body flow direction in hydrogenation reaction space by slurries, the hydrocarbon material of slurries MR-KRDS-MJ adds The intermediate reaction product of hydrogen direct liquefaction enters subsequent hydrocarbon material and adds hydrogen direct liquefaction reaction process after mixing with slurries BDS-MJ In；
4. positive, the hydrocarbon material of slurries BDS-MJ on the basis of crossing the main body flow direction in hydrogenation reaction space by oil powder slurries stream The intermediate reaction product for adding hydrogen direct liquefaction enters subsequent hydrocarbon material and adds hydrogen direct liquefaction anti-after mixing with slurries MR-KRDS-MJ During answering.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrogen direct liquefaction reaction process RU, slurries MR-KRDS-MJ is added to enter hydrocarbon powder and add the direct liquid of hydrogen in hydrocarbon powder Changing the hydrocarbon powder of reaction process RU participation adds hydrogen direct liquefaction to react, and what is contacted first is other containing serum materials, can be selected from down One or more of column:
1. adding the hydrocarbon powder of participation of hydrogen direct liquefaction reaction process RU that hydrogen direct liquefaction is added to react into hydrocarbon powder Other slurries BDS-MJ；
2. hydrocarbon powder adds the hydrocarbon powder of participation of hydrogen direct liquefaction reaction process RU to add starch containing for hydrogen direct liquefaction reaction The recycle stock of liquid；
3. hydrocarbon powder add that hydrogen direct liquefaction reaction process RU generates containing serum materials, add hydrogen direct from hydrocarbon powder The intermediate product of liquefaction reaction process RU；
4. hydrocarbon powder add that hydrogen direct liquefaction reaction process RU generates containing serum materials, add hydrogen direct from hydrocarbon powder The final product of liquefaction reaction process RU.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, and setting slurries are connected At least two conversion zone of operation, whole oil powders slurry raw materials, which enter, to be participated in hydrocarbon powder in the reaction process of the first conversion zone and adds hydrogen Direct liquefaction reaction.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, the liquefied fraction of coal dust Greater than 85%.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, the liquefied fraction of coal dust It is 85~98%.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, while mixing the non-coal of refining Base weight oil FD.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, while mixing the non-coal of refining Base weight oil FD；The cracking conversion rate of heavy oil FD is greater than 90%.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, operating condition are as follows: Reaction temperature is 400~485 DEG C, and reactor pressure is 6~30MPa, vapor phase hydrogen volumetric concentration 50~95%, gas-liquid volume ratio For 300~1500NL/kg, deliquescence accelerant additive amount is 0.1~3 mass % of dry pulverized coal weight, and co-catalyst additive amount is Sulphur/catalyst activity metal molar ratio is 1.0~2.0 in co-catalyst, and coal slurry solid concentration is 40~60 mass %, reaction Residence time TRU is 0.5~4 hour.
In preceding conversion zone RUA, ratio, that is, agent coal ratio JK10 of hydrogen supply agent weight and coal dust weight is 0.5~2.0；
In rear conversion zone RUB, ratio, that is, agent coal ratio JK20 of hydrogen supply agent weight and coal dust weight is 0.5~2.0.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.30~0.95 of the agent coal ratio JK10 of preceding conversion zone RUA.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.45~0.80 of the agent coal ratio JK10 of preceding conversion zone RUA.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.50~0.70 of the agent coal ratio JK10 of preceding conversion zone RUA.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, into hydrocarbon powder Adding hydrogen direct liquefaction reaction process RU to participate in hydrocarbon ils at least part of direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply At least part of solvent DS is used as the solvent for preparing coal slurry；
The ratio of the weight flow rate KS-W of the weight flow rate DS-W and coal dust KS of hydrogen supply dissolvent DS are agent coal ratio K100= (DS-W)/(KS-W), K100 are 0.5~2.0.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, into hydrocarbon powder Adding hydrogen direct liquefaction reaction process RU to participate in hydrocarbon ils at least part of direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply At least part of solvent DS is used as the solvent for preparing coal slurry；
Hydrogen supply dissolvent DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, and the weight of part saturation aromatic hydrocarbons contains It is 0.35~0.70 that amount, which is greater than 15%, aromatic carbon rate,.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, into hydrocarbon powder Adding hydrogen direct liquefaction reaction process RU to participate in hydrocarbon ils at least part of direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply At least part of solvent DS is used as the solvent for preparing coal slurry；
Hydrogen supply dissolvent DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, and the weight of part saturation aromatic hydrocarbons contains It is 0.45~0.60 that amount, which is greater than 25%, aromatic carbon rate,.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, the coal hydrogenation used Direct liquefaction catalyst is a kind of composite hydrogenation catalyst, includes high-activity component and low activity component；The high activity group It is 1: 10 to 10: 1 that parting, which belongs to the weight ratio of low activity component metals,；The high-activity component is the water soluble salt chemical combination of molybdenum Or mixtures thereof object；The low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, direct hydrogenation liquefaction of coal catalyst water content are lower than 2wt%；Direct hydrogenation liquefaction of coal catalyst particle diameter be 1~ 100 μm of powdered granule.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, the coal hydrogenation used Direct liquefaction catalyst be nanometer ultra-fine grain aqua oxidation iron catalyst and/or iron oxide and/or pyrite and/or bloodstone and Or molybdenum oxide and/or molybdenum sulfide and/or ammonium molybdate and/or nickel sulfide.
The present invention, mode of operation when processing hydrocarbon powder RU-F1S may is that
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, into hydrocarbon powder Adding hydrogen direct liquefaction reaction process RU to participate in hydrocarbon ils at least part of direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS.
Mode of operation of the invention may is that
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C is used Hydrocarbon TO-RU-DS；
Hydrogen supply hydrocarbon TO-RU-DS, the external hydrogen supply including the hydrogen supply hydrocarbon SH for being 230~400 DEG C containing normal boiling point may be used Hydrocarbon OUT-TO-RU-DS, including recycle hydrocarbons MR-KRDS；
The weight flow rate heavy oil RU-F1L-W of the weight flow rate TO-RU-DS-W and heavy oil RU-F1L of hydrogen supply hydrocarbon TO-RU-DS Ratio be oil ratio KP80, KP80=(TO-RU-DS-W)/(RU-F1L-W), KP70 be 0.05~1.0.
Mode of operation of the invention may is that
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
It is converted in the heavy hydrocarbon HNBPC heat from hydrogenation cracking reaction of hydrocarbon material hydrogenation process RU, front reaction zone RUA Rate is selected from one of the following or several:
1. heat from hydrogenation cracking reaction conversion ratio is lower than 20% stage of reaction；
2. heat from hydrogenation cracking reaction conversion ratio is lower than 35% stage of reaction；
3. heat from hydrogenation cracking reaction conversion ratio is lower than 50% stage of reaction.
Mode of operation of the invention may is that
(4) in separation and recovery process SYS700, separation process MRP-S is set, stabilized hydrogenation reaction product MRP is separated into point From gas MRP-V and separating liquid MRP-L；
The whereabouts of gas MRP-V is separated, one of the following or several is selected from:
1. at least part hydrogen rich gas gas MRP-V becomes cold anticyclone and separates gas MRP-V- after cooling and dewatering, de-oiling CHPS-V, at least part MRP-V-CHPS-V use return direct hydrogenation liquefaction of coal reaction process RU to use as recycle hydrogen；
2. at least part hydrogen rich gas gas MRP-V becomes cold anticyclone and separates gas MRP-V- after cooling and dewatering, de-oiling CHPS-V, at least part MRP-V-CHPS-V deviate from least part non-hydrogen gas by hydrogen purification process HUPSYS, Obtain high-purity hydrogen MRP-V-CHPS-V-PH；At least part high-purity hydrogen MRP-V-CHPS-V-PH makes as recycle hydrogen It is used with direct hydrogenation liquefaction of coal reaction process RU is returned；
3. at least part hydrogen rich gas gas MRP-V becomes warm high pressure and separates gas MRP-V- after cooling and dewatering, de-oiling KMHPS-V, the warm high pressure separation gas MRP-V-KMHPS-V gravity flow of at least part is into direct hydrogenation liquefaction of coal reaction process RU's The secondary use of the lower reaction zone of operating pressure；
4. at least part hydrogen rich gas gas MRP-V, gravity flow enters the operation pressure of direct hydrogenation liquefaction of coal reaction process RU The secondary use of the lower reaction zone of power；
5. at least part hydrogen rich gas gas MRP-V, into the removal process of rear portion reaction zone RUB product.
Mode of operation of the invention may is that
(1) in hydrocarbon material hydrogenation process RU, the removal process of front reaction zone RUA product, with rear portion reaction zone RUB The removal process of product partly or entirely shares.
Mode of operation of the invention may is that
(1) in hydrocarbon material hydrogenation process RU, the removal process of the gaseous product of front reaction zone RUA is anti-with rear portion The removal process of the gaseous product of area RUB is answered, is partly or entirely shared.
Mode of operation of the invention may is that
(1) in hydrocarbon material hydrogenation process RU, the removal process of the liquid material product of front reaction zone RUA is anti-with rear portion The removal process of the liquid material product of area RUB is answered, is partly or entirely shared.
Mode of operation of the invention may is that
(1) in hydrocarbon material hydrogenation process RU, the removal process of the product slurry of front reaction zone RUA is anti-with rear portion The removal process of the product slurry of area RUB is answered, is partly or entirely shared.
Mode of operation of the invention may is that
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply being mainly made of the hydro carbons that normal boiling point is 230~530 DEG C is used Hydrocarbon TO-RU-DS；
The hydrogen supply hydrocarbon TO-RU-DS of 50 weight % or more, is provided by recycle hydrocarbons MR-KRDS；
In hydrocarbon material front hydrogenation process RUA, using being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C Hydrogen supply hydrocarbon TO-RUA-DS；
The hydrogen supply hydrocarbon TO-RUA-DS of 50 weight % or more, is provided by recycle hydrocarbons MR-KRDS.
Mode of operation of the invention may is that
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply being mainly made of the hydro carbons that normal boiling point is 230~530 DEG C is used Hydrocarbon TO-RU-DS；
In hydrocarbon material front hydrogenation process RUA, using being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C Hydrogen supply hydrocarbon TO-RUA-DS；
The hydrogen supply hydrocarbon TO-RUA-DS of 100 weight %, is provided by recycle hydrocarbons MR-KRDS.
The general control principle of the gas-phase presulfiding hydrogen concentration of hydrogenation process of the invention described in detail below.
As needed, any hydrogenation process can be added in any supplement sulphur, but be typically incorporated into most upstream Hydrogenation process entrance, to guarantee reaction process necessary minimum concentration of hydrogen sulfide such as 500PPm (v) or 1000PPm (v) or the expected specified value such as 3000PPm (v), with guarantee the necessary hydrogen sulfide sectional pressure of catalyst not less than minimum specified value, with Guarantee the necessary vulcanization kenel of catalyst.The supplement sulphur can be sulfide hydrogen or can be converted into hydrogen sulfide to adding hydrogen Material of the conversion process without ill-effect, such as hydrogen sulfide containing gas or oil product, or vulcanization is generated after contacting with high-temperature hydrogen The molten sulfur or carbon disulfide of hydrogen or dimethyl disulfide etc..
The rule of the high pressure separation process of hydrogenation reaction effluent of the invention described in detail below.
The high pressure separation process of hydrogenation reaction effluent generally comprises cold high pressure separator, when hydrocarbon in hydrogenation reaction effluent When oil density big (such as close with water density) or viscosity are difficult to separate or contain solid particle greatly or with water emulsification, it is also necessary to set The high pressure hot separator that operation temperature is usually 150~450 DEG C is set, hydrogenation reaction effluent enters high pressure hot separator point at this time It by conventional liq hydrocarbon and may mainly be deposited from the hot high score gas gas being mainly made of hydrogen in volume for one and one Solid composition hot high score oil liquid body, hot high score gas enters the cold high pressure separator point that operation temperature is usually 20~80 DEG C Following target is realized: cold since a large amount of high boiling components enter in hot high score oil liquid body from for cold high score oil and cold high score gas High score oil density becomes smaller or viscosity becomes smaller or is easily isolated with water.Thermal high is arranged in the high pressure separation process of hydrogenation reaction effluent Separator is also equipped with the advantages of reducing thermal loss, because hot high score oil liquid body can be to avoid hot high score gas experience using empty The process that cools of cooler or water cooler.Meanwhile the hot high score oil liquid body in part can be returned to the hydrogenation process of upstream Be recycled, with improve receive the recycle oil hydrogenation process overall raw material property, or to the cycling hot high score oil into Row circulation plus hydrogen.
Between thermal high separate section and cold anticyclone separate section, as needed, warm high pressure separate section can be set, Become gas-liquid two-phase material after hot high score air cooling at this time, one is separated into warm high-pressure separator in volume mainly by hydrogen The warm high score gas gas and the warm high score oil liquid being mainly made of conventional liq hydrocarbon and solid that may be present of gas composition Body, warm high score gas gas enter cold anticyclone separate section and carry out cooling and gas-liquid separation.
Hydrogenation reaction effluent or hot high score gas or warm high score gas enter before cold anticyclone separate section, usually first reduce temperature (temperature should be higher than that in the hydrogenation reaction effluent gas phase degree (usually with reactive moieties feed exchange heat) to about 220~100 DEG C Crystallization temperature, the crystallization temperature of sal-ammoniac of sulphur hydrogenation ammonia), then usually injection washing water formation water filling back end hydrogenation is anti-thereto Answer effluent, it may be necessary to which 2 or multiple injection points are set, and washing water is used for absorbing ammonia and issuable other impurity such as chlorine Change hydrogen etc., and the aqueous solution after absorbing ammonia necessarily absorbs hydrogen sulfide.In cold anticyclone separate section, the water filling back end hydrogenation reaction stream Object separates out are as follows: the cold high score gas being mainly made of hydrogen in volume, one mainly by conventional liq hydrocarbon and dissolved hydrogen The cold high score oil of composition, a cold high score water be mainly made of water and dissolved with ammonia, hydrogen sulfide.The cold high score water, The content of middle ammonia is generally 0.5~15% (w), preferably 1~8% (w).One purpose of note washing water is to absorb hydrogenation reaction Ammonia and hydrogen sulfide in effluent prevent from forming sulphur hydrogenation ammonia or more sulphur ammonia Crystallization Plugging heat exchanger channels, increase system pressure Drop.The injection rate of the washing water should be determined according to following principles: on the one hand, washing water divides after injecting hydrogenation reaction effluent For vapour phase water and liquid phase water, liquid phase water has to be larger than zero, preferably washs 30% or more of water inventory；In another aspect, washing Water is washed for absorbing the ammonia in hydrogenation reaction effluent, prevents the ammonia density of high score gas too high, reduces catalyst activity, usually height Divide the ammonia volumetric concentration of gas more lower better, generally no greater than 200PPm (v), desirably no more than 50PPm (v).The cold anticyclone Separator operation pressure be hydrogenation reaction partial pressure subtract actual pressure drop, cold anticyclone separate section operating pressure with add hydrogen it is anti- The difference of pressure is answered, it is unsuitable too low or excessively high, it is usually generally 0.35~3.2MPa, 0.5~1.5MPa.The cold high score The hydrogen volume concentration value of gas, should not too low (cause device operating pressure rise), generally should not less than 70% (v), it is preferably not low In 80% (v), preferably not below 85% (v).As previously described at least part, be usually 85~100% cold high score gas return It is recycled in hydrogenation reaction part, to provide the necessary amounts of hydrogen in hydrogenation reaction part and hydrogen concentration；It is thrown to improve device Provide efficiency, it is necessary to assure circulation hydrogen concentration be not less than lower limit value above-mentioned, for this purpose, according to specific feedstock property, reaction condition, Product distribution can exclude a part of cold high score gas to exclude methane, the ethane that reaction generates.For the cold high score of discharge Gas can realize hydrogen and non-hydrogen gas component point using conventional membrane separation process or pressure swing adsorption technique or oil wash technique From, and the hydrogen of recycling is used as new hydrogen.
For direct hydrogenation liquefaction of coal reaction process RU, because of conventional gas hydrocarbon, CO, CO2Yield is huge, usually most of Cold high score gas of the cold high score gas than such as from about 70~100%, after being purified as membrane separation process obtained by permeated hydrogen pressurization after return Hydrogenation process does not permeate gas by PSA and mentions hydrogen or pressurization return plus hydrogen after " steam reforming hydrogen manufacturing+PSA mentions hydrogen " Reaction process is recycled.
New hydrogen enters plus hydrogen partial is to supplement the hydrogen that hydrogenation process consumes, and the higher the better for new hydrogen hydrogen concentration, generally Not preferably less than 95% (v), preferably not below 99% (v).All new hydrogen can be introduced any hydrogenation reaction part, be preferably introduced the One hydrogenator.
The present invention, in any reaction process, it can be entirely recycle hydrogen that the hydrogen gas stream used, which can be entirely new hydrogen, It can be the gaseous mixture of new hydrogen and recycle hydrogen.
Reference examples
Butt coal processing capacity be 250 tons/when direct hydrogenation liquefaction of coal device direct hydrogenation liquefaction of coal reaction process RU, Operated using conventional gas-liquid cocurrent reactive mode, coal slurry is mixed into after hydrogen partial after being overpressurized through heating stove heating, then with After high-temperature hydrogen mixing from hydrogen heating furnace, into the bottom of up flow type suspension bed the first direct hydrogenation liquefaction of coal reactor Portion；The circulation liquid material of liquid collecting cup outflow at the top of first direct hydrogenation liquefaction of coal reactor USR1 is followed after circulating pump pressurizes Ring enters the bottom of up flow type suspension bed the first direct hydrogenation liquefaction of coal reactor, after mixing with charging coal slurry, charging hot hydrogen Coal is carried out by the main reaction space that the distributor of lower disposed in reactor USR1 shell ring flows up into reactor USR1 Hydrogen direct liquefaction is added to react.
The hydrogen feed of each reactor, the primary mixed zone that reactor bottom is all injected by bottom feed inlet, with After the mixing of loop slurry product, main reaction region is passed through by upstream after distribution plate.
Direct hydrogenation liquefaction of coal reaction process RU, the internal diameter using 2 serial operations is 4.812 meters, length of cylindrical shell sections 35 The suspension bed direct hydrogenation liquefaction of coal hot wall reactor of the liquid product forced circulation of rice, the first direct hydrogenation liquefaction of coal reactor USR1 product USR1P enters the second direct hydrogenation liquefaction of coal reactor USR2, the second direct hydrogenation liquefaction of coal reactor USR2 production Object USR2P reacts final product RU-P as direct hydrogenation liquefaction of coal, carries out Oil-gas Separation, heat into rear end high pressure hot separator Oil product fractionation is carried out after the pressurization degassing of high score oil.
The operating process of direct hydrogenation liquefaction of coal process RU is described below:
1. direct hydrogenation liquefaction of coal catalyst, hydrogen supply dissolvent RUDS, coal dust are made into coal dust in coal process for preparation AM The coal RUF that mass concentration is 45% is pressurizeed with coal force (forcing) pump and inputs coal heating furnace；The pressurization of co-catalyst molten sulfur It is mixed afterwards with the coal RUF of coal pressurization pump discharge；
Table 2 is the property of direct hydrogenation liquefaction of coal reaction process RU feed coal；
Table 3 is the property of direct hydrogenation liquefaction of coal reaction process RU solvent naphtha；
Table 4 is the catalyst property of direct hydrogenation liquefaction of coal reaction process RU；
Table 5 is the co-catalyst property of direct hydrogenation liquefaction of coal reaction process RU；
2. obtaining direct hydrogenation liquefaction of coal reaction product is RU-P in direct hydrogenation liquefaction of coal reaction process；
Direct hydrogenation liquefaction of coal reaction process or its feed system make flushing oil, cooling down oil using hydrogen supply dissolvent oil；
Table 6 is direct hydrogenation liquefaction of coal reaction condition summary sheet；
Table 7 is direct hydrogenation liquefaction of coal reaction process material balance table；
Table 8 is the new hydrogen logistics table that reference examples enter first reactor
Table 9 is reference examples the second hydrogen gas stream table；
Table 10 is reference examples reaction process and material distribution table；
Table 11 is the fraction property that reference examples direct hydrogenation liquefaction of coal reaction process RU liquefaction generates oil；
Table 12 is reference examples, the operating parameter of the separation process of the net product of the first reactor of embodiment, logistics composition table.
Using forced circulation suspension bed hot wall reactor USR1, USR2 of 2 serial operations, USR1 reaction temperature is 448 ~465 DEG C, USR2 reaction temperature is 455~465 DEG C, and the upper space in every reactor arranges built-in gas liquid-liquid separation Component, that is, liquid collection cups, Partial Liquid Phase product enter liquid collection cups, along catheter outflow reactor bottom, by circulating pump Respective reactor inlet is returned after pressurization and forms liquid circulation, and liquid circulation amount is 2.0~2.2 times of coal slurry total amount；It is other mixed Reactor head is discharged along diversion pipe in phase gas-liquid product；
Direct hydrogenation liquefaction of coal process RU final reacting product RU-P temperature is 465 DEG C, and injecting cooling oil and cold hydrogen reduces Temperature is to entering high pressure hot separator ATHPS after 410~420 DEG C；
3., using high pressure hot separator ATHPS, being in temperature in the separate section of Coal Liquefaction reaction product RU-P 410~420 DEG C, under conditions of pressure is 18.8~19.0MPa, separation Coal Liquefaction reaction product RU-P obtains hot high score oil ATHPS-L and hot high score gas ATHPS-V；
The hydro carbons in hot high score oil ATHPS-L and hot high score gas ATHPS-V is collected, uses fractionation in fractionating section AFRAC Tower obtains narrow fraction oil product, is that 220~530 DEG C of fractions are sent into solvent oil hydrogenation stabilization process A-CRU by normal boiling point, is supplied Hydrogen solvent naphtha RUDS removes coal process for preparation AM and other uses a little；Obtain about 600,000 tons/year of liquefied residue, go residue at Type.
In separation process AF, recycle direct hydrogenation liquefaction of coal reaction product RU-P, obtain hydrogen volume concentration be 94~ 96% hydrogen-rich stream RUH returns to direct hydrogenation liquefaction of coal reaction process and is recycled, and the concentrate mode of hydrogen is UF membrane Purification.
In separation process AF, recycle direct hydrogenation liquefaction of coal reaction product RU-P, obtain mainly by conventional boiling range be 250~ The direct hydrogenation liquefaction of coal of 530 DEG C of hydro carbons composition generates oil distillate oil AFD, obtains being higher than comprising normal boiling point 530 DEG C of hydrocarbon The AFK of the dregs of fat containing solid of class；
Part direct hydrogenation liquefaction of coal generates oil distillate oil AFD as material flow A FD1, is used as hydrogen supply dissolvent predecessor hydrocarbon MFB；
Stabilized hydrogenation reaction, which is carried out, in stabilized hydrogenation reaction process MR, hydrogen supply dissolvent predecessor hydrocarbon MFB completes aromatic hydrocarbon molecule Part aromatic ring saturated reaction MRR is converted into stabilized hydrogenation reaction product MRP；
Stabilized hydrogenation reaction product MRP is recycled, hydrogen supply dissolvent DS is obtained；
At least part hydrogen supply dissolvent DS enters direct hydrogenation liquefaction of coal reaction process as hydrogen supply dissolvent LCF-DS, hydrogen supply Solvent LCF-DS and coal dust are formulated as coal slurry LCF use；
Hydrogen supply dissolvent DS is the liquid phase stream containing hydrogen supply dissolvent, the hydro carbons group for being mainly 250~530 DEG C by conventional boiling range At.
In above-mentioned total system, hydrogen supply dissolvent amount is 1.22 times i.e. 244.0 ten thousand tons/year of coal dust, and solvent oil hydrogenation is stablized Process produces about 243.5 ten thousand tons/year of feed oil of hydrogen supply dissolvent, is the recycle oil being present in total system.
The coal of coal slurry: oily weight ratio is 45.05: 54.95, and the hydrogen supply dissolvent dosage of coal slurry thick in this way is coal blending 122.0%.
The operating pressure of second floating bed hydrogenation reactor product RUA2P is 18.86MPa, operation temperature is 455~465 ℃。
System hydrogen usage is shown in Table 7, table 8, table 9.
Using GS equation calculation phase equilibrium constant, flowsheeting calculated result is shown in Table 12.
Since the gas phase of upstream reactor product all passes through downstream reactor, so, the gas holdup of second reactor is high That is liquid Space low efficiency, while containing wide variety of conventional gaseous hydrocarbon, water, hydrogen sulfide, ammonia, carbon monoxide, carbon dioxide in gas phase, Therefore vapor phase hydrogen concentration is low, and in order to maintain hydrogen partial pressure to be higher than 12.7MPa, operating pressure is forced to be increased to 19MPa.
The property of 2 direct hydrogenation liquefaction of coal reaction process RU feed coal of table
The property of 3 direct hydrogenation liquefaction of coal reaction process RU solvent naphtha of table
The catalyst property of 4 direct hydrogenation liquefaction of coal reaction process RU of table
Serial number Project Data Remarks
1 Active component Nanometer section FeOOH
2 Carrier Part material coal
3 Additive amount, (Fe/ dry coal), wt% 1.00
4 The Fe content of fine coal supported catalyst, wt% 5.6±0.5 Permanganimetric method
5 The granularity of fine coal supported catalyst, wt% Laser particle size method
≤74μm ≥80
74 μm of > < 20
6 Catalyst is aqueous, wt% ≤4 Gravimetric method
The co-catalyst property of 5 direct hydrogenation liquefaction of coal reaction process RU of table
6 direct hydrogenation liquefaction of coal reaction condition summary sheet of table
Project Data
React stagnation pressure, MPa 18.8~19.0
React hydrogen partial pressure, MPa Minimum 12.7
Average reaction temperature, DEG C 430~455
USR1 hydrogen normal volume is to coal weight ratio, standard cubic meter hydrogen/ton coal Entrance 1130, outlet 690
USR2 hydrogen normal volume is to coal weight ratio, standard cubic meter hydrogen/ton coal Entrance 890, outlet 740
Chemistry consumption hydrogen, standard cubic meter hydrogen/ton coal 590~610
Chemistry consumption hydrogen distribution USR1: USR2 About (70~75): (25~30)
Direct hydrogenation liquefaction of coal catalyst Nanometer section hydrated ferric oxide
Direct hydrogenation liquefaction of coal catalyst loading, (Fe/ dry coal), wt% 1.00
Auxiliary agent Liquid stream
Auxiliary dosage, Atomic ratio >=2 S/Fe
Reaction compartment hydrogen sulphide in the vapor phase volumetric concentration Greater than 3000PPm
The coal of the liquefying reactor apparent residence time (to coal standard state volume) 140~145 minutes
Moisture-and-ash-free basis lique faction of coal rate, weight % Greater than 90
7 direct hydrogenation liquefaction of coal reaction process material balance table of table
Project Into/maf.wt% Into/maf.wt% Out/maf.wt% Out/maf.wt% Into-go out/maf.wt%
H2S 0.00 0.00 0.72 0.68 0.72
NH3 0.00 0.00 0.36 0.34 0.36
CO 0.00 0.00 0.99 0.94 0.99
CO2 0.00 0.00 1.46 1.39 1.46
C1 0.00 0.00 3.46 3.29 3.46
C2 0.00 0.00 2.79 2.66 2.79
C3 0.00 0.00 3.32 3.16 3.32
C4 0.00 0.00 1.83 1.74 1.83
Solvent 128.52 122.22 0.00 0.00 -128.52
Oily (220 DEG C of <) 0.00 0.00 25.33 24.09 25.33
Oily (220 DEG C of >) 0.00 0.00 30.01 28.54 30.01
Solvent materials 0.00 0.00 128.52 122.22 128.52
H2O 0.00 0.00 12.27 11.67 12.27
538 DEG C or more fractions 0.00 0.00 15.21 14.46 15.21
H2 5.65 5.37 0.00 0.00 -5.65
Moisture-and-ash-free basis coal 100.00 95.10 8.78 8.35 -91.22
Ash 5.15 4.90 5.15 4.90 0.00
Catalyst-Fe 1.05 1.00 1.05 1.00 0.00
Catalyst-other 0.61 0.58 0.23 0.22 -0.38
Sulphur 1.20 1.14 0.69 0.66 -0.51
DMKDS 0.00 0.00 0.00 0.00 0.00
It is total 242.18 230.32 242.18 230.32 0.00
Note: Maf is moisture and ash-free basis.
8 reference examples of table enter the new hydrogen logistics table of first reactor
9 reference examples the second hydrogen gas stream table of table
10 reference examples reaction process of table and material distribution table
11 reference examples direct hydrogenation liquefaction of coal reaction process RU of table liquefaction generates the fraction property of oil
As can be seen from Table 12, in the gas phase of the net product of first reactor >=230 DEG C of conventional liquid hydrocarbon (solvent naphtha) Weight is potential recycle hydrocarbons MKDS to be outer for hydrogen supply agent weight 33%, warm high-pressure separator KKD is right >=230 DEG C of conventional liquid hydrocarbon The condensation efficiency of (solvent naphtha) is 91%.
Embodiment
Embodiment one
Based on reference examples, using the stabilized hydrogenation object of middle matter hydrocarbon in the hydrocarbon material either shallow heat from hydrogenation cracked gas product of the present invention Reuse method, improved process flow chart are shown in attached drawing 42, are described as follows:
1. overall hydrogen THF, coal slurry BDS-MJ, recycle hydrocarbons MR-KRDS-TOR1 are mixed into overall raw material USR1F1, under Portion enters first reactor USR1；Net product USR1-MP is discharged from top in first reactor USR1；
2. making the net product USR1-MP of first reactor USR1 enter leading portion high pressure hot separator in separation process RUA-PS D1 is separated into hot high score oil D1L and the i.e. RUA-PS-V of hot high score gas D1V；
Hot high score oil D1L carries out the reaction of depth direct hydrogenation liquefaction of coal into second reactor USR2；
3. hot high score gas D1V, into warm high-pressure separator KKD, being separated into containing normal boiling point is 230~400 DEG C Most of foreign gas in the warm high score oil KKDL of hydrogen supply the hydrocarbon component and warm high score gas KKDV, hot high score gas D1V enters temperature In high score gas KKDV, hydrogen supply the hydrocarbon component of the normal boiling point higher than 230 DEG C of the 80 weight % or more in hot high score gas D1V is entered In warm high score oil KKDL；
Warm high score oil KKDL, into stabilized hydrogenation reaction process MR, there are the items of hydrogen and stabilized hydrogenation catalyst MRC Under part, it is converted into stabilized hydrogenation reaction product MRP by stabilized hydrogenation reaction process MR, the hydro carbons in hot high score gas D1V carries out The partial hydrogenation saturated reaction MRR of aromatic hydrocarbons is converted into hydrogen supply the hydrocarbon component MR-DS；
4. condensing and separating process MRP-S, stabilized hydrogenation reaction product MRP enters warm high-pressure separator D2 and is separated into warm height Divide warm high score oil D2L, that is, separating liquid MRP-L of gas D2V and the hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point；
Warm high score oil D2L is divided into 2 tunnels, and first part D2L2 goes recovery system to separate as outlet product, second part D2L1 directly returns to leading portion reaction zone i.e. the first direct hydrogenation liquefaction of coal reactor USR1 progress coal as recycle hydrocarbons MR-KRDS and adds The reaction of hydrogen direct liquefaction；
5. injecting washing water WS into warm high score gas KKDV, enters leading portion cold high pressure separator D3 after then cooling down and be separated into Cold high score gas D3V and cold high score oil D3L.
As can be seen from Table 12, in warm high score oil KKDL >=weight of 230 DEG C of conventional liquid hydrocarbon (solvent naphtha) is outer confession The 37% of hydrogen supply agent weight is matched defeated coal slurry solvent naphtha so if being used as using recycle hydrocarbons MR-KRDS, can be improved 23~32% Conveying coal ability, the liquid-phase operation state volume flow of the net product of first reactor increases about 21%, it is assumed that agent coal than constant, 21% coal blending liquefying power (limitation for not considering reactor volume) at least can be improved.
Embodiment two
Based on embodiment one, under conditions of not increasing long circulating hydrogen supply dissolvent oil quantity, using air lift method of the present invention, It the use of 100,000 standard cubes m/hour is 100000Nm3The cold anticyclone separation gas of/h is as circulating gas-lifting gas.
As can be seen from Table 12, in the gas phase of the net product of first reactor >=230 DEG C of conventional liquid hydrocarbon (solvent naphtha) It is the precursor of potential recycle hydrocarbons MR-KRDS for the 53% of hydrogen supply agent weight that weight, which is outer, in warm high score oil DDKL >=230 The weight of DEG C conventional liquid hydrocarbon (solvent naphtha) is outer for the 48% of hydrogen supply agent weight, and recycle hydrocarbons MR-KRDS amount is reachable outer for hydrogen supply The 37~42% of agent weight.
Embodiment three
It is improved under conditions of not increasing long circulating hydrogen supply dissolvent oil quantity using the method for the present invention based on embodiment one The coal dust processing capacity of device is solvent naphtha with slurry using recycle hydrocarbons MR-KRDS, and prepare coal: solvent naphtha weight ratio is 45.05: 54.95 coal slurry can increase coal feeding amount at least 21% in this way, can make full use of the hydrogen supply capacity of recycle hydrocarbons MR-KRDS, improve dress The economy set.
As shown in figure 42, compared with embodiment one, process flow variation is as follows:
1. warm high score oil D2L enters separation/fractionating section FRAC1 and is used as D2L-DL3 after decompression, abjection normal boiling point is low After 230 DEG C of hydro carbons, the solvent naphtha D2L- that the mainly hydro carbons by normal boiling point higher than 230 DEG C and entrainment dust form is obtained DL；
2. solvent naphtha D2L-DL prepares part M100 in coal slurry and coal dust makes coal slurry MR-KRDS-MJ, as material MR-KRDS-TOR1 enters first reactor USR1 and participates in reaction；
Warm high score oil D2L, is divided into 2 tunnels, and first part goes recovery system to separate as outlet product D2L2.
Example IV
Based on embodiment three, the net product R2P of second reactor enters rear end high pressure hot separator R2P-THPS, is separated into heat High score gas R2P-THPS-V and hot high score oil R2P-THPS-L；Hot high score gas R2P-THPS-V is used as the hydrogen of first reactor R1 The secondary use of raw material, forms hydrogen countercurrent mode.
Due to using counter-current mode of operation, the feed hydrogen of second reactor is new hydrogen.
Foreign gas (H due to using counter-current mode of operation, in second reactor product2O、CO、CO2、NH3、H2S it) measures, Lower than 25% of the foreign gas amount in reference examples in second reactor product, therefore, the heat of the net product R2P of second reactor is high Divide the quantity of the hydro carbons carried in gas R2P-THPS-V seldom.
12 reference examples of table, the operating parameter of the separation process of the net product of the first reactor of embodiment, logistics form table
Embodiment five
Based on embodiment three, gas stripping gas BH adds the matched hydrogen supply of hydrogen direct liquefaction reaction process RU molten using hydrocarbon powder The hydrogen rich gas gas that the warm high pressure separation process of the reaction product of agent stabilized hydrogenation reaction process (not being MR) is isolated, forms Hydrogen is secondary to use operation mode.
Embodiment six
Based on embodiment three, by front reaction process RUA, that is, first reactor, before being divided into 2 grades of formulas of slurries serial operation Portion's reaction process RUA1, RUA2, using 2 estrade reactors, front reaction process RUA1 discharge containing normal boiling point be 230~ The gas RUA1-PS-V of 350 DEG C of the hydrocarbon component based on hydrogen supply dissolvent oil, front reaction process RUA2 discharge contain normal boiling point For the gas RUA2-PS-V, gas RUA1-PS-V and gas RUA2- of 230~350 DEG C of the hydrocarbon component based on hydrogen supply dissolvent oil PS-V is used as gas RUA-PS-V.
The hydrogen feed of front reaction process RUA1 and/or RUA2, can be the gas from second reactor gas-phase product Body can be hydrocarbon powder and the reaction of the matched hydrogen supply dissolvent stabilized hydrogenation reaction process of hydrogen direct liquefaction reaction process RU added to produce The hydrogen rich gas gas that the warm high pressure separation process of object is isolated.
The present embodiment has essentially formed 3 grades of direct hydrogenation liquefaction of coal reaction systems of slurries serial operation.
Embodiment seven
Based on embodiment three, direct hydrogenation liquefaction of coal reactor R1 is the liquid collecting cup being arranged in reactor and keeps collection liquid logical Cross the product liquid forced cyclic type suspension bed direct hydrogenation liquefaction of coal reaction that circulating pump is pressed to form Liquid product recycle operation System forms the relative separation of liquid material product and gas-phase product in reactor head.
The present embodiment makes full use of this characteristic, carries out gas phase, the classification processing of liquid phase.
Totally 2 tunnel, the first via are gas-liquid mixed phase material R1MP to the net product of reactor R1, are directly entered front end high pressure hot separator It is separated into gas R1MP-V and liquid phase R1MP-L in the middle part of D1, because the road material is without cooling, therefore high temperature shape can be kept State retains the vaporised hydrocarbon quantity in gas phase to greatest extent.
Totally 2 tunnel, secondary route circulating pump R1-PUMP are exported with the shape of intimate pure slurries R1-LP the net product of reactor R1 Formula conveying, vaporizing section hydro carbons becomes gas-liquid mixture R1-LP-M after mixing with gas stripping gas BH, while reducing temperature of charge, so Entering in leading portion high pressure hot separator D1 afterwards, feed inlet is located at the position under first via gas-liquid mixed phase material R1MP feed inlet, Gas phase R1-LP-M-V and liquid phase R1-LP-M-L are separated into the high pressure hot separator D1 of front end in this way.
After gas phase R1-LP-M-V rising is mixed with gas R1MP-V, from top, discharge front end high pressure hot separator D1 is used as D1V。
The lower liquid phase R1-LP-M-L of temperature is mixed with the higher liquid phase R1MP-L of temperature and is cooled down it, from before the discharge of bottom High pressure hot separator D1 is held to be used as D1L.
Embodiment eight
Dreg-oil suspension bed (slurry bubble bed) the heat from hydrogenation process of CANMET, by Canadian Minerals and energy technology center from 20 Century 70 exploitation, has built up a set of 250,000 tons/year of industrial demonstration unit in Montreal refinery in 1985, it was confirmed that The practicability of CANMET technique.
The device catalyst carries upper FeSO with ub-bituminous coal or lignite4Or cobalt CO, molybdenum MOThe compound of equal metals does not add Any component is prepared.Under conditions of heat from hydrogenation cracking, as the ub-bituminous coal of catalyst substrates or lignite itself generating unit Divide hydrogenation liquefaction, so that catalyst granules is become smaller, and form porous structure；The particle to become smaller, a part are discharged anti-with reaction product Device is answered, another part gradually becomes weight since absorption feed residue decomposes the metallic compound generated, and sinks to reactor bottom Portion is periodically discharged by bottom.
Table 13 is CANMET technique typical operation conditions summary sheet.
Table 14 is the property of CANMET catalyst and matrix coal.
CANMET technique is improved using the present invention, it is anti-with 2 floating bed hydrogenations by floating bed hydrogenation reaction process It answers device to be divided into front conversion zone RUA and rear portion conversion zone RUB, front conversion zone RUA, that is, first reactor RUA reaction is produced Object and SAPMAC method hydrogen hybrid cooling are separated into the hot high score gas of leading portion into 410 DEG C of feeding high pressure hot separator RUA-1-THPS The RUA-1-THPS-V and hot high score oil RUA-1-THPS-L of leading portion.
The hot high score oil RUA-1-THPS-L of leading portion, goes second reactor RUB to be converted into second reactor product RUB-P, with SAPMAC method hydrogen hybrid cooling is separated into the hot high score gas of back segment into 410 DEG C of feeding back segment high pressure hot separator RUB-1-THPS The RUB-1-THPS-V and hot high score oil RUB-1-THPS-L of back segment；The hot high score oil RUB-1-THPS-L of back segment, gone after decompression separation, Fractionating system isolates residue, obtains distilled oil；The hot high score gas RUB-1-THPS-V of back segment, by back segment temperature high-pressure separator RUB-1-MHPS is separated into back segment temperature high pressure separation gas RUB-1-MHPS-V and back segment temperature high pressure separating liquid RUB-1-MHPS-L.
Back segment temperature high pressure separates gas RUB-1-MHPS-V, injects after gas RUA-1-MHPS-V mixing is separated with leading portion temperature high pressure Washing water, and be sent into cold high pressure separator RUB-1-CHPS, and be separated into cold high score gas and cold high score oil.
The hot high score gas RUA-1-THPS-V of leading portion turns in stabilized hydrogenation reaction process MR by stabilized hydrogenation reaction process MR Stabilized hydrogenation reaction product MRP is turned to, the partial hydrogenation that the hydro carbons in the hot high score gas RUA-1-THPS-V of leading portion carries out aromatic hydrocarbons is full Hydrogen supply the hydrocarbon component MR-DS is converted into reaction MRR；
Process MRP-S is being condensed and separated, in leading portion temperature high-pressure separator RUA-1-MHPS, in 260~280 DEG C of temperature Under, stabilized hydrogenation reaction product MRP be separated into leading portion temperature high pressure separation gas RUA-1-MHPS-V separate gas MRP-V with Leading portion temperature high pressure separating liquid RUA-1-MHPS-L, that is, separating liquid MRP-L；
Leading portion temperature high pressure separating liquid RUA-1-MHPS-L is mainly made of the hydrocarbon component that normal boiling point is 230~400 DEG C , it is divided into 2 tunnels, the 1st tunnel is the 15~25% of total amount and is used as outlet product, and the 2nd tunnel (is equivalent to cold for the 75~85% of total amount The 45% of lake residua weight flow rate) it is used as recycle hydrocarbons MR-KRDS.
After target material high pressure cold air lake residual oil is mixed with recycle hydrocarbons MR-KRDS, hydrogen, temperature is increased by heating furnace, so Enter front conversion zone RUA, that is, first reactor RUA afterwards.
It, can be by the external supply being mainly made of the hydrocarbon component that normal boiling point is 230~400 DEG C according to operation needs Hydrogen supply hydrocarbon precursor is added to stabilized hydrogenation reaction process MR and produces hydrogen supply dissolvent together, makes up solvent naphtha loss, maintains hydrogen supply Solvent naphtha balance.
The improved CANMET technique of the present invention, product yield of residual oil reduces by 30% or more and product residual oil hydrogen content improves 20% or more, product residual oil is sent into the delayed coking unit processing of refinery；Product heavy distillate yield reduces by 10% or more and hydrogen Content is improved to 105% or more of reduced value, naphtha, kerosene, diesel oil hydrogen content increase.Most of all, anti- It answers the coking amount of process to be greatly lowered, eliminates high conversion operation operating condition down tube road the problem of being easily completely clogged with soot, it can be with Significantly extend the continuous operation period.
The improved CANMET technique of the present embodiment is suitable for processing the high residual oil of aromatic carbon rate.
13 CANMET technique typical operation conditions summary sheet of table
The property of 14 CANMET catalyst of table and matrix coal

Claims (83)

1. the stabilized hydrogenation object reuse method of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product, it is characterised in that include Following steps:
(1) in hydrocarbon material hydrogenation process RU, there are hydrogen, conventional liq hydrocarbon, there may be the mixed phases of solid particle simultaneously Under the conditions of material, hydrogenation reaction RU-R at least is carried out containing the first raw material RU-F1 of carbon and protium and is converted into final add Hydroformylation reaction product RU-P；Recycle final hydrogenation reaction product RU-P；
First raw material RU-F1 includes liquid material RU-F1L and solid particulate materials RU-F1S that may be present；
Hydrogenation reaction RU-R, the hydrofining reaction comprising at least part liquid material RU-F1L include at least part liquid The stabilized hydrogenation of the hydrocracking reaction of state raw material RU-F1L, the free radical comprising the generation of at least part heat cracking reaction is anti- It answers, the hydrogenation liquefaction reaction of at least part solid particulate materials RU-F1S that may be present may be included；
Hydrogenation reaction RU-R may use catalyst RU-CAT；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon for the hydrocarbon component for being 230~400 DEG C containing normal boiling point is used；
In hydrocarbon material hydrogenation process RU, the external hydrogen supply for the hydrogen supply hydrocarbon SH for being 230~400 DEG C containing normal boiling point may be used Hydrocarbon OUT-TO-RU-DS；
In hydrocarbon material hydrogenation process RU, it is possible to create the hydrogen supply the hydrocarbon component RU-PRO- that normal boiling point is 230~400 DEG C DSC；
Hydrocarbon material hydrogenation process RU use hydrogenator RU-XE, final hydrogenation reaction product RU-P, for containing hydrogen, Conventional liq hydrocarbon simultaneously may the mixed phase material containing solid particle, with 1 tunnel or 2 tunnels or multichannel object when leaving reactor RU-XE Expect that the form of RU-P-X occurs, material RU-P-X is gas phase or liquid phase or gas-liquid mixed phase or gas-liquid-solid three-phase logistics；
In hydrocarbon material hydrogenation process RU, setting may include at least two conversion zone of the serial operation of the liquid material of solid；
One conversion zone refers to the gas-liquid separation step comprising liquid material hydrogenation reaction step and the step gas-liquid product Technical process；
The front conversion zone RUA of the hydrocarbon material hydrogenation process RU refers to that hydrocarbon material hydrogenation process RU's is last Any upstream reaction section or whole upstream reaction sections of one conversion zone RUJ；
In hydrocarbon material hydrogenation process RU, at least 2 hydrogenator RU-XE are used；
It is separated into separating liquid RUAP-HS-L in separation process RUAP-HS, at least part leading portion hydrogenation reaction product RUAP and contains Having normal boiling point is the separation gas RUAP-HS-V of 230~400 DEG C of the hydrocarbon component；
Separating liquid RUAP-HS-L is converted into rear portion reaction product RUBP into rear portion conversion zone RUB；
The logistics conduct that contains the hydrocarbon component that normal boiling point be 230~400 DEG C of at least part based on separation gas RUAP-HS-V Material MR-F use, it is understood that there may be residual gas RUAP-HS-V used as material RUAP-HS-V-BYPASS；
(2) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR-F warp It crosses stabilized hydrogenation reaction process MR and is converted into stabilized hydrogenation reaction product MRP, the hydro carbons in material MR-F carries out the part of aromatic hydrocarbons Hydrogen saturated reaction MRR is added to be converted into hydrogen supply the hydrocarbon component MR-DS；
(3) in return course TLOOP, at least partially based on stabilized hydrogenation reaction product MRP containing normal boiling point be 230~ The logistics of 400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Recycle hydrocarbons MR-KRDS enters hydrocarbon material hydrogenation process RU；
At least part recycle hydrocarbons MR-KRDS returns to the front of hydrocarbon material hydrogenation process RU as MR-KRDS-TO-RUA Reaction zone RUA participates in hydrocarbon material hydrogenation reaction RUA-R.
2. according to the method described in claim 1, it is characterized by:
(1) in hydrocarbon material hydrogenation process RU, using at least 2 hydrogenator RU-XE, at least 1 hydrogenator is Up flow type expanded bed hydrogenator.
3. according to the method described in claim 1, it is characterized by:
(3) hydro carbons in return course TLOOP, recycle hydrocarbons MR-KRDS in weight mainly by normal boiling point be 230~400 DEG C the hydrocarbon component composition.
4. according to the method described in claim 1, it is characterized by:
(2) in stabilized hydrogenation reaction process MR, simultaneous processing hydrogen supply hydrocarbon precursor MR-FK；
In stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, hydrogen supply hydrocarbon precursor MR-FK, material MR-F are converted into stabilized hydrogenation reaction product MRP, the hydrocarbon in material MR-F by stabilized hydrogenation reaction process MR The partial hydrogenation saturated reaction MRR that class carries out aromatic hydrocarbons is converted into hydrogen supply the hydrocarbon component MR-DS.
5. according to the method described in claim 1, it is characterized by:
(1) in hydrocarbon material hydrogenation process RU, the hydrogenator and separation process RUAP-HS of front conversion zone RUA is used Equipment, independently of each other.
6. according to the method described in claim 1, it is characterized by:
(1) in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA is de- with product section Liquid separation function, obtains separating liquid and gas-liquid mixed phase material, separation process RUAP-HS front conversion zone RUA last It is carried out in hydrogenator.
7. according to the method described in claim 1, it is characterized by:
(1) in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA has product gas-liquid clear Clear separation function, obtains separating liquid and separation gas, last plus hydrogen of the separation process RUAP-HS in front conversion zone RUA are anti- It answers in device and carries out.
8. according to the method described in claim 1, it is characterized by:
(1) in hydrocarbon material hydrogenation process RU, last hydrogenator of front conversion zone RUA has product gas-liquid clear Clear separation function, obtains separating liquid and separation gas, last plus hydrogen of the separation process RUAP-HS in front conversion zone RUA are anti- It answers in device and carries out, last hydrogenator mode of operation is gas-liquid counter current operation mode.
9. according to the method described in claim 1, it is characterized by:
(1) it in hydrocarbon material hydrogenation process RU, is used at least partially based on separation gas RUAP-HS-V as material MR-F.
10. according to the method described in claim 1, it is characterized by:
(1) in hydrocarbon material hydrogenation process RU, thermal high separation process is entered based on separation gas RUAP-HS-V at least partially AP-HS is separated into hot high score gas AP-HS-V and hot high score oil AP-HS-L；
The logistics conduct that contains the hydrocarbon component that normal boiling point be 230~400 DEG C of at least part based on hot high score oil AP-HS-L Material MR-F is used.
11. according to the method described in claim 1, it is characterized by:
(1) in hydrocarbon material hydrogenation process RU, thermal high separation process is entered based on separation gas RUAP-HS-V at least partially AP-HS is separated into hot high score gas AP-HS-V and hot high score oil AP-HS-L；
The logistics conduct that contains the hydrocarbon component that normal boiling point be 230~400 DEG C of at least part based on hot high score gas AP-HS-V Material MR-F is used.
12. according to the method described in claim 1, it is characterized by:
(3) in return course TLOOP, at least partially based on stabilized hydrogenation reaction product MRP containing normal boiling point be 230~ The logistics of 400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
At least part stabilized hydrogenation reaction product MRP is used as recycle hydrocarbons MR-KRDS.
13. according to the method described in claim 1, it is characterized by:
(3) in return course TLOOP, at least partially based on stabilized hydrogenation reaction product MRP containing normal boiling point be 230~ The logistics of 400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Stabilized hydrogenation reaction product MRP is separated, the liquid object for the hydrogen supply the hydrocarbon component for being 230~400 DEG C containing normal boiling point is obtained XXK is flowed, the logistics at least partially based on liquid stream XXK is used as recycle hydrocarbons MR-KRDS.
14. according to the method described in claim 1, it is characterized by:
(3) in return course TLOOP, at least partially based on stabilized hydrogenation reaction product MRP containing normal boiling point be 230~ The logistics of 400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
Stabilized hydrogenation reaction product MRP is separated, the gaseous state object for the hydrogen supply the hydrocarbon component for being 230~400 DEG C containing normal boiling point is obtained YYK is flowed, the logistics at least partially based on gaseous stream YYK is used as recycle hydrocarbons MR-KRDS.
15. according to the method described in claim 1, it is characterized by:
(3) in return course TLOOP, at least partially based on stabilized hydrogenation reaction product MRP containing normal boiling point be 230~ The logistics of 400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
At least part recycle hydrocarbons MR-KRDS enters hydrocarbon material hydrogenation process RU after mixing with the first raw material RU-F1.
16. according to the method described in claim 1, it is characterized by:
(3) in return course TLOOP, at least partially based on stabilized hydrogenation reaction product MRP containing normal boiling point be 230~ The logistics of 400 DEG C of hydrogen supply the hydrocarbon component is used as recycle hydrocarbons MR-KRDS；
After first raw material RU-F1 of at least part recycle hydrocarbons MR-KRDS and at least part solid powder shape is mixed into slurry, Into hydrocarbon material hydrogenation process RU.
17. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) hydrogen supply hydrocarbon RUA-DS is used in front conversion zone RUA in hydrocarbon material hydrogenation process RU；
Leading portion hydrogenation reaction RUA-R, uses catalyst RUA-CAT；
(3) hydro carbons in return course TLOOP, recycle hydrocarbons MR-KRDS.In weight mainly by normal boiling point be 230~400 DEG C the hydrocarbon component composition.
18. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation process States of matter is the hydrocarbon powder of solid particle when the reactor of RU.
19. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, lower than the behaviour of hydrogenation reaction product RUAP Make 0~1.0MPa of pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is 350~480 DEG C.
20. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, lower than the behaviour of hydrogenation reaction product RUAP Make 0~0.5MPa of pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP is 400~450 DEG C.
21. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, lower than the behaviour of hydrogenation reaction product RUAP Make 0~1.0MPa of pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, the operation than hydrogenation reaction product RUAP Temperature is 5~80 DEG C low.
22. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
The operating pressure of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, lower than the behaviour of hydrogenation reaction product RUAP Make 0~1.0MPa of pressure；
The operation temperature of the separation process RUAP-HS of leading portion hydrogenation reaction product RUAP, under conditions of guaranteeing material noncoking, The difference DT of its operation temperature and the operation temperature of hydrogenation reaction product RUAP is small as far as possible.
23. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) in hydrocarbon material hydrogenation process RU, setting may include 2 or multiple reactions of the serial operation of the liquid material of solid Section wherein reacted between conversion zone in the presence of the series flow for the liquid material that may include solid with the liquid material that may include solid Flowing between section is forward direction, the type of flow classification of hydrogen material between conversion zone, a kind or several selected from following manner:
1. hydrogen material flows to cocurrent in the same direction with the main body of serum materials, belong to liquid, gas cocurrent tandem reactor process；
2. slurry series connection, tandem reactor process of the hydrogen short circuit across stream；
3. gas-phase product does not enter the reaction process of other any conversion zones, and gas raw material is not there are at least one conversion zone Using the hydrogen from other any conversion zones, belong to there are hydrogen material parallel operation reaction process；
4. reaction process receives the hydrogen product of downstream reaction section there are at least one conversion zone, belong between conversion zone There are the reaction process of hydrogen gas product counter-current operation.
24. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation process States of matter is the hydrocarbon powder of solid particle when the reactor of RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being mainly 230~400 DEG C by normal boiling point is used The hydrogen supply hydrocarbon TO-RUA-DS of composition.
25. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation process States of matter is the hydrocarbon powder of solid particle when the reactor of RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the confession for the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid RUAP- is separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V is used as material MR-F.
26. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation process States of matter is the hydrocarbon powder of solid particle when the reactor of RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the confession for the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid RUAP- is separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
Warm high pressure separate section RUAP-HS-V-MS is set, separation gas RUAP-HS-V is separated into gas RUAP-HS-V-MS-V With separating liquid RUAP-HS-V-MS-L；The hydrocarbon group for being 230~400 DEG C containing normal boiling point in separating liquid RUAP-HS-V-MS-L Point；
At least part separating liquid RUAP-HS-V-MS-L is used as material MR-F.
27. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation process States of matter is the hydrocarbon powder of solid particle when the reactor of RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the confession for the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid RUAP- is separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
It is set using the warm high pressure separate section RUAP-HS-V-MS of gas stripping gas RUAP-HS-V-MS-BH, gas RUAP- will be separated HS-V is separated into gas RUAP-HS-V-MS-V and separating liquid RUAP-HS-V-MS-L；
Separating liquid RUAP-HS-V-MS-L and gas stripping gas RUAP-HS-V-MS-BH completes to separate, and is separated into air lift discharge gas The gentle extract RUAP-HS-V-MS-L-BL of RUAP-HS-V-MS-L-BV；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid RUAP-HS-V-MS-L-BL；
At least part air lift liquid RUAP-HS-V-MS-L-BL is used as material MR-F.
28. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation process States of matter is the hydrocarbon powder of solid particle when the reactor of RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the confession for the hydro carbons for being 230~400 DEG C containing normal boiling point is used Hydrogen hydrocarbon TO-RUA-DS；
Separation gas RUAP-HS-V and separating liquid RUAP- is separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
It is set using the warm high pressure separate section RUAP-HS-V-MS of gas stripping gas RUAP-HS-V-MS-BH, gas RUAP- will be separated HS-V is separated into gas RUAP-HS-V-MS-V and separating liquid RUAP-HS-V-MS-L；
Separating liquid RUAP-HS-V-MS-L and gas stripping gas RUAP-HS-V-MS-BH completes to separate, and is separated into air lift discharge gas The gentle extract RUAP-HS-V-MS-L-BL of RUAP-HS-V-MS-L-BV；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid RUAP-HS-V-MS-L-BL；
At least part air lift liquid RUAP-HS-V-MS-L-BL is used as material MR-F；
(3) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR-F warp It crosses stabilized hydrogenation reaction process MR and is converted into stabilized hydrogenation reaction product MRP, the hydro carbons in material MR-F carries out the part of aromatic hydrocarbons Hydrogen saturated reaction MRR is added to be converted into hydrogen supply the hydrocarbon component MR-DS；
(4) separation gas is separated into the separation process MRP-S using gas stripping gas MRP-S-BH, stabilized hydrogenation reaction product MRP The separating liquid MRP-L of MRP-V and the hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point；
Separating liquid MRP-L and gas stripping gas MRP-S-BH completes to separate, and is separated into the air lift discharge gentle extract of gas MRP-L-BV MRP-L-BL；
The hydrocarbon component for being 230~400 DEG C containing normal boiling point in air lift liquid MRP-L-BL；
Material of at least part based on air lift liquid MRP-L-BL is used as recycle hydrocarbons MR-KRDS.
29. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) it is mainly made of heavy object HNBPC in hydrocarbon material hydrogenation process RU, the first raw material RU-F1；
The heavy object HNBPC refers to the hydrocarbon component of the normal boiling point higher than 450 DEG C and/or enters hydrocarbon material hydrogenation process States of matter is the hydrocarbon powder of solid particle when the reactor of RU；
In the preceding conversion zone RUA of hydrocarbon material hydrogenation process RU, the hydro carbons for being mainly 230~400 DEG C by normal boiling point is used The hydrogen supply hydrocarbon TO-RUA-DS of composition；
(2) separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V is used as material MR-F, and existing residual gas RUAP-HS-V is as material RUAP-HS-V-BYPASS is used；
Material RUAP-HS-V-BYPASS enters separation process, is separated into gas RUAP-HS-V-BYPASS-V and containing conventional boiling The lime set RUAP-HS-V-BYPASS-L for the hydrocarbon component that point is 230~400 DEG C；
At least part lime set RUAP-HS-V-BYPASS-L, into hydrocarbon material hydrogenation process RU；
At least part lime set RUAP-HS-V-BYPASS-L returns to the front reaction zone RUA of hydrocarbon material hydrogenation process RU Participate in hydrocarbon material hydrogenation reaction RUA-R.
30. according to the method described in claim 1, it is characterized by:
(1) hydrocarbon material hydrogenation process RU adds hydrogen direct liquefaction reaction process RU, setting for the hydrocarbon powder RU-F1S of raw material 2 or multiple conversion zones of slurries serial operation；
One conversion zone refers to the gas-liquid separation step comprising slurry hyd reaction step and the step gas-liquid product Technical process；
The front conversion zone RUA refers to any conversion zone in the upstream of the last one conversion zone or whole upstream reaction sections；
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, there are hydrogen, the conventional liq hydrocarbon comprising hydrogen supply hydrocarbon, hydrocarbon powder Expect and there may be under conditions of catalyst, the hydrocarbon powder RU-F1S's of progress at least part adds the reaction of hydrogen direct liquefaction RU-R is converted into hydrocarbon powder and adds hydrogen direct liquefaction final reacting product RU-P；Final hydrogenation reaction product RU-P is 1 tunnel or 2 Road or multichannel material；Recycle final hydrogenation reaction product RU-P；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon TO-RU-DS for the hydro carbons for being 230~400 DEG C containing normal boiling point is used；
In front conversion zone RUA, the hydrogen supply hydrocarbon RUA-DS for the hydro carbons for being 230~400 DEG C containing normal boiling point is used；
Add the front conversion zone RUA of hydrogen direct liquefaction reaction process RU in hydrocarbon powder, there are hydrogen, include the normal of hydrogen supply hydrocarbon It advises liquid hydrocarbon, hydrocarbon powder and there may be under conditions of catalyst, it is hydrocarbon that hydrocarbon powder RU-F1S carries out at least part Powder adds hydrogen direct liquefaction front reaction RUA-R to be converted into hydrocarbon powder and adds hydrogen direct liquefaction front reaction product RUAP；Front Reaction product RUAP is 1 tunnel or 2 tunnels or multichannel material；
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU, can while processing comes from the recycle hydrocarbons MR-KRDS of step (5) It is capable of processing other hydrogen supply dissolvent oil BDS and hydrocarbon powder KS；
(2) separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
At least part separation gas RUAP-HS-V used as material MR-F, it is understood that there may be residual gas RUAP-HS-V conduct Material RUAP-HS-V-BYPASS is used；
(3) in stabilized hydrogenation reaction process MR, under conditions of there are hydrogen and stabilized hydrogenation catalyst MRC, material MR-F warp It crosses stabilized hydrogenation reaction process MR and is converted into stabilized hydrogenation reaction product MRP, the hydro carbons in material MR-F carries out the part of aromatic hydrocarbons Hydrogen saturated reaction MRR is added to be converted into hydrogen supply the hydrocarbon component MR-DS；
(4) separation gas MRP-V is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP and be containing normal boiling point The separating liquid MRP-L of 230~400 DEG C of hydrogen supply the hydrocarbon component MR-DS；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
(5) enter hydrocarbon material hydrogenation process RU in return course TLOOP, recycle hydrocarbons MR-KRDS；
At least part recycle hydrocarbons MR-KRDS returns to the front of hydrocarbon material hydrogenation process RU as MR-KRDS-TO--RUA Reaction zone RUA participates in hydrocarbon material hydrogenation reaction RUA-R.
31. according to the method for claim 30, it is characterised in that:
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
Material of a part based on separating liquid MRP-L goes hydrocarbon powder to add the rear portion conversion zone of hydrogen direct liquefaction reaction process RU RUB contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react.
32. according to the method for claim 30, it is characterised in that:
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, at least two conversion zone of slurries serial operation is set, wherein reacting There are the series flows of slurry between section, are forward direction with flowing of the slurry between conversion zone, hydrogen material between conversion zone Type of flow classification, a kind or several selected from following manner:
1. hydrogen material flows to cocurrent in the same direction with the main body of serum materials, belong to liquid, gas cocurrent tandem reactor process；
2. slurry series connection, tandem reactor process of the hydrogen short circuit across stream；
3. gas-phase product does not enter the reaction process of other any conversion zones, and gas raw material is not there are at least one conversion zone Using the hydrogen from other any conversion zones, belong to there are hydrogen material parallel operation reaction process；
4. reaction process receives the hydrogen product of downstream reaction section there are at least one conversion zone, belong between conversion zone There are the reaction process of hydrogen gas product counter-current operation.
33. according to the method for claim 30, it is characterised in that:
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, reaction time of the slurries raw material in front conversion zone RUA accounts for Slurries raw material adds the 30~65% of the general reaction residence time of hydrogen direct liquefaction reaction process RU in whole hydrocarbon powder.
34. according to the method for claim 30, it is characterised in that:
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Most of hydro carbons in separating liquid MRP-L, a kind or several in following conventional boiling range:
1. the conventional liquid hydrocarbon that normal boiling point is 230~400 DEG C；
2. the conventional liquid hydrocarbon that normal boiling point is 230~350 DEG C；
3. the conventional liquid hydrocarbon that normal boiling point is 230~300 DEG C.
35. according to the method for claim 30, it is characterised in that:
(4) separation gas MRP-V and separating liquid MRP-L is separated into separation process MRP-S, stabilized hydrogenation reaction product MRP；
The hydrogen supply the hydrocarbon component MR-DS for being 230~400 DEG C containing normal boiling point in separating liquid MRP-L；
Material of at least part based on separating liquid MRP-L is used as recycle hydrocarbons MR-KRDS；
The weight of recycle hydrocarbons MR-KRDS is the 5~95% of separating liquid MRP-L weight.
36. according to the method for claim 30, it is characterised in that:
(5) hydrogen direct liquefaction is added to react by hydrocarbon powder in return course TLOOP, at least part recycle hydrocarbons MR-KRDS Whole main body reaction compartments of the first reactor of the first conversion zone of journey RU carry out hydrocarbon powder and hydrogen direct liquefaction are added to react.
37. according to the method for claim 30, it is characterised in that:
(5) hydrocarbon powder is gone to add hydrogen direct liquefaction reaction process in return course TLOOP, at least part recycle hydrocarbons MR-KRDS RU contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react, and working method is selected from one of the following or several:
1, at least part recycle hydrocarbons MR-KRDS are selected, gravity flow returns to the front conversion zone of direct hydrogenation liquefaction of coal reaction process, Contact slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
2, at least part recycle hydrocarbons MR-KRDS are selected, the front conversion zone contact of direct hydrogenation liquefaction of coal reaction process is returned Slurry carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
3, at least part recycle hydrocarbons MR-KRDS is selected to return to the front of direct hydrogenation liquefaction of coal reaction process after heat exchange heating Conversion zone, contact slurry carry out hydrocarbon powder and hydrogen direct liquefaction are added to react；
Selection 4, at least part recycle hydrocarbons MR-KRDS are used as coal slurry and prepare solvent naphtha configuration coal slurry MKDS-MJ, then coal slurry MKDS-MJ enters direct hydrogenation liquefaction of coal reaction process, carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
Selection 5, at least part recycle hydrocarbons MR-KRDS are used as coal slurry and prepare solvent naphtha configuration coal slurry MKDS-MJ, then coal slurry MKDS-MJ enters the front conversion zone of direct hydrogenation liquefaction of coal reaction process, carries out hydrocarbon powder and hydrogen direct liquefaction is added to react；
6, at least part recycle hydrocarbons MR-KRDS are selected, in washing step DW, the washing oil as gas RUAP-HS-V is used To wash the dust in abjection gas RUAP-HS-V；While completing to wash dedirt, by the part in gas RUAP-HS-V Hydro carbons is condensed into liquid phase DWL；
At least part liquid phase DWL returns to direct hydrogenation liquefaction of coal reaction process, and contact slurry carries out hydrocarbon powder and adds hydrogen direct Liquefaction reaction；
7, at least part recycle hydrocarbons MR-KRDS are selected, in washing step DW, the washing oil as gas RUAP-HS-V is used To wash the dust in abjection gas RUAP-HS-V；While completing to wash dedirt, by the part in gas RUAP-HS-V Hydro carbons is condensed into liquid phase DWL；
At least part liquid phase DWL returns to the front conversion zone of direct hydrogenation liquefaction of coal reaction process, and contact slurry carries out hydrocarbon Powder adds hydrogen direct liquefaction to react；
8, at least part liquid phase DWL are selected, the hydrocarbon powder of direct hydrogenation liquefaction of coal reaction process contact slurry progress is returned and adds Before the reaction of hydrogen direct liquefaction, it is used as Conduit rinse oil or pump flushing oil or instrument flushing oil.
38. according to the method for claim 30, it is characterised in that:
At least part recycle hydrocarbons MR-KRDS is used as hydrocarbon powder slurry preparation solvent naphtha and configures hydrocarbon powder slurry MR-KRDS-MJ, Then hydrocarbon powder slurry MR-KRDS-MJ enters hydrocarbon powder and adds hydrogen direct liquefaction reaction process RU-RU, carries out hydrocarbon powder and adds The reaction of hydrogen direct liquefaction, working method are selected from one of the following or several:
1, recycle hydrocarbons MR-KRDS are selected, hydrocarbon powder slurry MR-KRDS-BDS- is prepared after mixing with other hydrogen supply dissolvent oil BDS MJ, hydrocarbon powder slurry MR-KRDS-BDS-MJ are used as hydrocarbon powder and starch MR-KRDS-MJ；
2, recycle hydrocarbons MR-KRDS are selected, hydrocarbon powder slurry preparation solvent naphtha is used alone as and configures hydrocarbon powder slurry MR-KRDS-MJ；
Other hydrogen supply dissolvent oil BDS prepare hydrocarbon powder and starch BDS-MJ.
39. according to the method for claim 30, it is characterised in that:
At least part recycle hydrocarbons MR-KRDS is used alone as hydrocarbon powder slurry preparation solvent naphtha and configures hydrocarbon powder slurry MR- KRDS-MJ；
Other hydrogen supply dissolvent oil BDS prepare hydrocarbon powder and starch BDS-MJ；
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the reaction time of hydrocarbon powder slurry MR-KRDS-MJ with it is hydrocarbon The reaction time that powder starches BDS-MJ is not identical.
40. according to the method for claim 30, it is characterised in that:
(2) separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In washing process BW10, separates gas RUAP-HS-V and at least contacted 1 time with wash cooling liquid CWL, separate gas RUAP-HS-V In at least part hydrocarbon gas be changed into hydrocarbon liquid and enter in rich cleaning solution BW10-L, leave washing process BW10 discharge gas BW10-V；The weight flow of rich cleaning solution BW10-L is greater than the weight flow of wash cooling liquid CWL；
At least part gas BW10-V is used as material MR-F.
41. according to the method for claim 30, it is characterised in that:
(2) separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In washing process BW10, separates gas RUAP-HS-V and at least contacted 1 time with wash cooling liquid CWL, separate gas RUAP-HS-V In at least part hydrocarbon gas be changed into hydrocarbon liquid and enter in rich cleaning solution BW10-L, leave washing process BW10 discharge gas BW10-V；The weight flow of rich cleaning solution BW10-L is greater than the weight flow of wash cooling liquid CWL；
Rich cleaning solution BW10-L, whereabouts are selected from one of the following or several:
1. being mixed into separating liquid RUAP-HS-L；
2. conversion zone RUA before going；
3. removing rear conversion zone RUB；
4. hydrocarbon powder process with slurry is gone to make to use with slurry solvent.
42. according to the method for claim 40, it is characterised in that:
(2) in washing process BW10, the contact separation mode of operation of gas RUAP-HS-V and wash cooling liquid CWL is separated, is selected from down One or more of column:
1. separating after mixing, 1 contact, 1 separation is carried out；
2. counter current contacting carries out 2 contacts and 2 separation；
3. counter current contacting carries out multiple-contact and separating for several times.
43. according to the method for claim 30, it is characterised in that:
(2) separation process RUAP-HS is carried out in last hydrogenator of leading portion hydrogenation process RUA, last Platform hydrogenator is unit equipment.
44. according to the method for claim 30, it is characterised in that:
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, a kind or several in following of hydrocarbon powder RU-F1S:
1. coal dust；
2. molding powder；
3. rubber powder；
4. direct hydrogenation liquefaction of coal reaction process RU mixes other hydrocarbon powders of refining.
45. according to the method for claim 30, it is characterised in that:
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, a kind or several in following of existing solid:
1. coal dust；
2. catalyst solid particle；
3. sulphur powder；
4. hydrocarbon ils coking material carrier semicoke particle；
5. molding powder；
6. rubber powder；
7. other solid powders that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to need to input.
46. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process, during following process 1 kind or several:
1. using the direct hydrogenation liquefaction of coal liquefaction process of hydrogen supply dissolvent oil；
2. not using the direct hydrogenation liquefaction of coal liquefaction process of hydrogen supply dissolvent oil；
3. kerosene refines process altogether；
4. coal faces hydrogen thermosol liquefaction process.
47. according to the method for claim 30, it is characterised in that:
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the hydrocarbon powder used adds the work of hydrogen direct liquefaction reactor XRUE Make a kind or several of mode in following:
1. suspended-bed reactor, that is, paste state bed reactor；
2. fluidized bed reactor；
3. suspension bed and ebullated bed combination type reactor.
48. according to the method for claim 30, it is characterised in that:
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the hydrocarbon powder used adds the work of hydrogen direct liquefaction reactor XRUE Make mode, a kind or several in following:
Option 1, liquid material and gas material use the counter-current reactor of pure adverse current working method；
Option 2, reactor XRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of XRUE material inlet；
Option 3, reactor XRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of XRUE material inlet；
Option 4, reactor XRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of XRUE material inlet, while circulating pump conveys circulation fluid, downstream transport liquid material product；
Option 5, reactor XRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of XRUE material inlet, while circulating pump conveys circulation fluid, downstream transport liquid material product；
Option 6, reactor XRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of XRUE material inlet, the other collection liquids for being collected simultaneously cup discharge pass through other dedicated feeding engines downstream Convey liquid material product；
Option 7, reactor XRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of XRUE material inlet, the other collection liquids for being collected simultaneously cup discharge pass through other dedicated feeding engines downstream Convey liquid material product；
Option 8, reactor XRUE, top are arranged liquid collecting cup and liquid material product are discharged by the production of dedicated feeding engine downstream transport liquid material Object is not provided with the fluidized bed reactor system of liquid material product forced circulation；
Option 9, reactor XRUE, top are arranged liquid collecting cup and liquid material product are discharged by the production of dedicated feeding engine downstream transport liquid material Object is not provided with the suspended-bed reactor system of liquid material product forced circulation；
Option 10, reactor XRUE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device XRUE material inlet and the combination type reactor of ebullated bed；
Option 11, reactor XRUE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device XRUE material inlet and the combination type reactor of ebullated bed, it is downstream defeated while circulating pump conveys circulation fluid Liquor charging material product；
Option 12, reactor XRUE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device XRUE material inlet and the combination type reactor of ebullated bed are collected simultaneously other collection liquids of cup discharge by it Its dedicated feeding engine downstream transport liquid material product；
The suspended-bed reactor system of flow pattern under the center upstream surrounding of internal guide cylinder is arranged in option 13；
The suspended-bed reactor system of flow pattern in the dirty surrounding in center of internal guide cylinder is arranged in option 14；
Option 15, empty cylinder bubbling bed suspended-bed reactor system；
It is anti-to form the dirty Returning reactor lower part of reactor top reaction zone liquid phase using the external circulation pipe of reactor for option 16 Answer the device outside circulation in area.
49. according to the method for claim 30, it is characterised in that:
Add hydrogen direct liquefaction reaction process RU in hydrocarbon powder, conversion zone obtains the mode of product slurry, in following manner 1 kind or several:
1. the slurries that the gas-liquid separation process of autoreaction section reaction product is discharged, as final reaction section product slurry；
2. the final reactor of conversion zone uses pure counter-current reactor, the bottom liquid phase region of the final reactor of autoreaction section is discharged Slurries, as conversion zone product slurry；
3. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup in the final reactor of autoreaction section is through water conservancy diversion The slurries of pipe discharge, as conversion zone product slurry；
4. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup in the final reactor of autoreaction section is through water conservancy diversion The slurries of pipe discharge, as slurry to be de-gassed；
Slurry to be de-gassed is separated into the liquid stream rich in bubble, the liquid stream that lean gas steeps all the way all the way by cyclonic separation step；
The liquid stream of lean gas bubble, is used as conversion zone product slurry.
50. according to the method for claim 30, it is characterised in that:
Add hydrogen direct liquefaction reaction process RU, last hydrogenator RU19 of the first conversion zone in hydrocarbon powder, for top The reactor that there is part to take off liquid function of liquid collecting cup is arranged in portion, and collection liquid RU19-DL-L derived from liquid collecting cup is anti-as first A section product slurry is answered, whereabouts is selected from one of the following or several:
1. going the reaction step of the second conversion zone；
2. removing the gas-liquid separator of the first conversion zone product slurry, it is separated into degassing slurries and gas；
3. going the first conversion zone cyclic process；
4. portion collection liquid RU19-DL-L removes separation and recovery system after dropping valve is depressured.
51. according to the method for claim 30, it is characterised in that:
In separation and recovery process SYS300, recycles final hydrogenation reaction product RU-P and obtain hydrogen rich gas gas RH, at least part Hydrogen rich gas gas RH returns to hydrocarbon powder and hydrogen direct liquefaction reaction process RU is added to be used as circulating hydrogen.
52. method according to claim 51, it is characterised in that:
The working method of separation and recovery process SYS300, hydrogen upgrading process H2UPU, H2UPU comprising hydrogen material are selected from down One or more of column:
1. using membrane separation process concentrate hydrogen；
2. using PSA pressure swing adsorption technique concentrate hydrogen；
3. using deep cooling process for separating concentrate hydrogen.
53. according to the method for claim 30, it is characterised in that:
In separation and recovery process SYS300, recycles final hydrogenation reaction product RU-P and obtain hydrogen rich gas gas RH, working method Selected from one of the following or several:
1. thermal high separation process RU-P-THPS, cold anticyclone separation process CHPS is arranged in separation and recovery process SYS300；
Thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P be separated into hot high score gas RU-P-THPS-V and Hot high score liquid material RU-P-THPS-L；
Cold high score gas CHPS-V and cold high score liquid material are separated into cold anticyclone separation process CHPS, hot high score gas RU-P-THPS-V CHPS-L；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH；
2. setting thermal high separation process RU-P-THPS, warm high pressure separation process MHPS, cold in separation and recovery process SYS300 High pressure separation process CHPS；
Thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P be separated into hot high score gas RU-P-THPS-V and Hot high score liquid material RU-P-THPS-L；
Warm high score gas MHPS-V and warm high score liquid material are separated into warm high pressure separation process MHPS, hot high score gas RU-P-THPS-V MHPS-L；
Cold high score gas CHPS-V and cold high score liquid material CHPS- are separated into cold anticyclone separation process CHPS, warm high score gas MHPS-V L；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH；
3. the thermal high separation process RU-P- with gas condensation collection step LCD is arranged in separation and recovery process SYS300 THPS, cold anticyclone separation process CHPS；
Hot high score gas RU-P-THPS-V is first separated into thermal high separation process RU-P-THPS, final hydrogenation reaction product RU-P With hot high score liquid material RU-P-THPS-L；Hot high score gas RU-P-THPS-V is separated into cold in gas condensation collection step LCD cooling Lime set LCD-L and de- liquid gas LCD-V；
Cold high score gas CHPS-V and cold high score liquid material CHPS-L are separated into cold anticyclone separation process CHPS, de- liquid gas LCD-V；
It processes cold high score gas CHPS-V and obtains hydrogen rich gas gas RH.
54. according to the method for claim 30, it is characterised in that:
(2) separation gas RUAP-HS-V and separating liquid are separated into separation process RUAP-HS, leading portion hydrogenation reaction product RUAP RUAP-HS-L；Separate the hydrocarbon component for being 230~400 DEG C containing normal boiling point in gas RUAP-HS-V；
In separation process RUAP-HS, stripping step BH-S, which is arranged, using gas stripping gas BH makes leading portion hydrogenation reaction product RUAP's The hydrocarbon component based on hydrogen supply dissolvent oil that at least part normal boiling point in liquid phase RUAP-L is 230~400 DEG C, which vaporizes, to be entered It separates in gas RUAP-HS-V, increases the weight flow for the hydro carbons that normal boiling point is 230~400 DEG C in separation gas RUAP-HS-V.
55. method according to claim 54, it is characterised in that:
(1) hydrocarbon powder add the working method of hydrogen direct liquefaction reaction process RU, stripping step BH-S in following one Kind is several:
1. being mixed with gas stripping gas BH with the gas-liquid mixed phase product RUAP of front reaction zone, the hydro carbons in air lift slurries；
2. being contacted with gas stripping gas BH with the pure product slurry RUAP-LP of front reaction zone；
3. dividing front reaction process RUA to 2 grades of formula front reaction process RUA1, RUA2 for slurries serial operation, front reaction The gas RUA1-P-XV for the hydrocarbon component based on hydrogen supply dissolvent oil that process RUA1 discharge is 230~400 DEG C containing normal boiling point, The gas for the hydrocarbon component based on hydrogen supply dissolvent oil that reaction process RUA2 discharge in front is 230~400 DEG C containing normal boiling point RUA2-P-XV, gas RUA1-P-XV and/or gas RUA2-P-XV are used as separation gas RUAP-HS-V.
56. method according to claim 54, it is characterised in that:
(1) add hydrogen direct liquefaction reaction process RU, the gas stripping gas BH that stripping step BH-S is used in hydrocarbon powder, be selected from following object One or more of material:
1. the new hydrogen that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
2. the circulating hydrogen that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
3. the circulating hydrogen after the hydrogen upgrading that hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to use；
4. adding in hydrogen direct liquefaction reaction process RU in hydrocarbon powder, the downstream of the front reaction zone of product slurry RUA-LP is discharged Reaction zone discharge hydrogen rich gas material or its derive gas；
5. hydrocarbon powder adds the matched hydrogen supply dissolvent stabilized hydrogenation in addition to MR reaction process of hydrogen direct liquefaction reaction process RU The hydrogen rich gas gas or its derivative gas that the reaction product of reaction process is isolated；
6. hydrocarbon powder adds the matched hydrocarbon powder liquefaction oil of hydrogen direct liquefaction reaction process RU to add the anti-of hydrogen upgrading reaction process The hydrogen rich gas gas for answering product to isolate or its derivative gas.
57. according to the method for claim 30, it is characterised in that:
(4) in separation and recovery process SYS700, separation process MRP-S is set, stabilized hydrogenation reaction product MRP is separated into separation gas MRP-V and separating liquid MRP-L；
Separation and recovery process SYS700, working method are selected from one of the following or several:
1. thermal high separation process MRP-THPS is arranged in separation and recovery process SYS700；
Hot high score gas MRP-THPS-V and heat are separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP High score liquid material MRP-THPS-L；
Based on hot high score liquid material MRP-THPS-L, separating liquid MRP-L is obtained；
2. thermal high separation process MRP-THPS, cold anticyclone separation process MRP-CHPS is arranged in separation and recovery process SYS700；
Hot high score gas MRP-THPS-V and heat are separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP High score liquid material MRP-THPS-L；
Cold high score gas MRP-CHPS-V and cold height are separated into cold anticyclone separation process MRP-CHPS, hot high score gas MRP-THPS-V Liquid separation material MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or cold high score liquid material MRP-CHPS-L, separating liquid MRP-L is obtained；
3. in separation and recovery process SYS700, setting thermal high separation process MRP-THPS, warm high pressure separation process MRP-MHPS, Cold anticyclone separation process MRP-CHPS；
Hot high score gas MRP-THPS-V and heat are separated into thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP High score liquid material MRP-THPS-L；
Warm high score gas MRP-MHPS-V and Wen Gao are separated into warm high pressure separation process MRP-MHPS, hot high score gas MRP-THPS-V Liquid separation material MRP-MHPS-L；
Cold high score gas MRP-CHPS-V and cold height are separated into cold anticyclone separation process MRP-CHPS, warm high score gas MRP-MHPS-V Liquid separation material MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or warm high score liquid material MRP-MHPS-L, separating liquid MRP-L is obtained；
4. the thermal high separation process MRP- with gas condensation collection step MRP-LCD is arranged in separation and recovery process SYS700 THPS, cold anticyclone separation process MRP-CHPS；
Thermal high separation process MRP-THPS, stabilized hydrogenation reaction product MRP be first separated into hot high score gas MRP-THPS-V and Hot high score liquid material MRP-THPS-L；Hot high score gas MRP-THPS-V is separated into cold in gas condensation collection step MRP-LCD cooling Lime set MRP-LCD-L and de- liquid gas MRP-LCD-V；
Cold high score gas MRP-CHPS-V and cold high score liquid material are separated into cold anticyclone separation process CHPS, de- liquid gas MRP-LCD-V MRP-CHPS-L；
Based on hot high score liquid material MRP-THPS-L and/or condensate liquid MRP-LCD-L, separating liquid MRP-L is obtained.
58. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU, the slurries MR-KRDS-MJ's that fabrication cycles hydrocarbon MR-KRDS is prepared Meanwhile the slurries BDS-MJ that other hydrogen supply dissolvent oil BDS are prepared is processed, working method is selected from one of the following:
1. slurries MR-KRDS-MJ, slurries BDS-MJ enter hydrocarbon powder and add that hydrogen direct liquefaction reaction process RU's is anti-after mixing It answers in device；
2. slurries MR-KRDS-MJ, slurries BDS-MJ, add that hydrogen direct liquefaction reaction process RU's is same anti-into hydrocarbon powder It answers in the same reaction space of device；
3. positive on the basis of flowing through the main body flow direction in hydrogenation reaction space by slurries, the hydrocarbon material of slurries MR-KRDS-MJ adds hydrogen straight Liquefied intermediate reaction product is connect, subsequent hydrocarbon material is entered after mixing with slurries BDS-MJ and is added in hydrogen direct liquefaction reaction process；
4. positive on the basis of crossing the main body flow direction in hydrogenation reaction space by oil powder slurries stream, the hydrocarbon material of slurries BDS-MJ adds hydrogen The intermediate reaction product of direct liquefaction adds hydrogen direct liquefaction to react with subsequent hydrocarbon material is entered after slurries MR-KRDS-MJ mixing Cheng Zhong.
59. according to the method for claim 30, it is characterised in that:
Adding hydrogen direct liquefaction reaction process RU, slurries MR-KRDS-MJ to enter hydrocarbon powder in hydrocarbon powder adds hydrogen direct liquefaction anti- Answering process RU to participate in hydrocarbon powder adds hydrogen direct liquefaction to react, and what is contacted first is other containing serum materials, and one in following Kind is several:
1. adding the hydrocarbon powder of participation of hydrogen direct liquefaction reaction process RU that hydrogen direct liquefaction is added to react other into hydrocarbon powder Slurries BDS-MJ；
2. hydrocarbon powder add that the hydrocarbon powder of participation of hydrogen direct liquefaction reaction process RU adds that hydrogen direct liquefaction reacts containing slurries Recycle stock；
3. hydrocarbon powder add that hydrogen direct liquefaction reaction process RU generates containing serum materials, add hydrogen direct liquefaction from hydrocarbon powder The intermediate product of reaction process RU；
4. hydrocarbon powder add that hydrogen direct liquefaction reaction process RU generates containing serum materials, add hydrogen direct liquefaction from hydrocarbon powder The final product of reaction process RU.
60. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, and slurries serial operation is arranged At least two conversion zone, whole oil powders slurry raw materials, which enter, to be participated in hydrocarbon powder in the reaction process of the first conversion zone and adds hydrogen direct Liquefaction reaction.
61. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, and the liquefied fraction of coal dust is greater than 85%.
62. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, and the liquefied fraction of coal dust is 85 ~98%.
63. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, while mixing the non-coal base weight of refining Oily FD.
64. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, while mixing the non-coal base weight of refining Oily FD；The cracking conversion rate of heavy oil FD is greater than 90%.
65. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, operating condition are as follows: reaction Temperature is 400~485 DEG C, and reactor pressure is 6~30MPa, and vapor phase hydrogen volumetric concentration 50~95%, gas-liquid volume ratio is 300~1500NL/kg, deliquescence accelerant additive amount are 0.1~3 mass % of dry pulverized coal weight, and co-catalyst additive amount is to help Sulphur/catalyst activity metal molar ratio is 1.0~2.0 in catalyst, and coal slurry solid concentration is 40~60 mass %, and reaction stops Staying time TRU is 0.5~4 hour.
In preceding conversion zone RUA, ratio, that is, agent coal ratio JK10 of hydrogen supply agent weight and coal dust weight is 0.5~2.0；
In rear conversion zone RUB, ratio, that is, agent coal ratio JK20 of hydrogen supply agent weight and coal dust weight is 0.5~2.0.
66. method according to claim 65, it is characterised in that:
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.30~0.95 of the agent coal ratio JK10 of preceding conversion zone RUA.
67. method according to claim 65, it is characterised in that:
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.45~0.80 of the agent coal ratio JK10 of preceding conversion zone RUA.
68. method according to claim 65, it is characterised in that:
The agent coal ratio JK20 of conversion zone RUB afterwards is the 0.50~0.70 of the agent coal ratio JK10 of preceding conversion zone RUA.
69. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, adds hydrogen into hydrocarbon powder Hydrocarbon ils at least part that direct liquefaction reaction process RU participates in direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply dissolvent At least part of DS is used as the solvent for preparing coal slurry；
The ratio of the weight flow rate KS-W of the weight flow rate DS-W and coal dust KS of hydrogen supply dissolvent DS be agent coal ratio K100=(DS-W)/ (KS-W), K100 is 0.5~2.0.
70. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, adds hydrogen into hydrocarbon powder Hydrocarbon ils at least part that direct liquefaction reaction process RU participates in direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply dissolvent At least part of DS is used as the solvent for preparing coal slurry；
Hydrogen supply dissolvent DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, and the weight content of part saturation aromatic hydrocarbons is big In 15%, aromatic carbon rate be 0.35~0.70.
71. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, adds hydrogen into hydrocarbon powder Hydrocarbon ils at least part that direct liquefaction reaction process RU participates in direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS, hydrogen supply dissolvent At least part of DS is used as the solvent for preparing coal slurry；
Hydrogen supply dissolvent DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, and the weight content of part saturation aromatic hydrocarbons is big In 25%, aromatic carbon rate be 0.45~0.60.
72. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, and the coal hydrogenation used is direct Deliquescence accelerant is a kind of composite hydrogenation catalyst, includes high-activity component and low activity component；The high-activity component gold Belonging to the weight ratio of low activity component metals is 1: 10 to 10: 1；The high-activity component be molybdenum water soluble salt compound or Its mixture；The low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, Direct hydrogenation liquefaction of coal catalyst water content is lower than 2wt%；Direct hydrogenation liquefaction of coal catalyst particle diameter is 1~100 μm Powdered granule.
73. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, and the coal hydrogenation used is direct Deliquescence accelerant is nanometer ultra-fine grain aqua oxidation iron catalyst and/or iron oxide and/or pyrite and/or bloodstone and/or oxygen Change molybdenum and/or molybdenum sulfide and/or ammonium molybdate and/or nickel sulfide.
74. according to the method for claim 30, it is characterised in that:
Hydrocarbon powder adds hydrogen direct liquefaction reaction process RU to be direct hydrogenation liquefaction of coal reaction process RU, adds hydrogen into hydrocarbon powder Hydrocarbon ils at least part that direct liquefaction reaction process RU participates in direct hydrogenation liquefaction of coal reaction is hydrogen supply dissolvent DS.
75. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C is used TO-RU-DS；
Hydrogen supply hydrocarbon TO-RU-DS, the external hydrogen supply hydrocarbon including the hydrogen supply hydrocarbon SH for being 230~400 DEG C containing normal boiling point may be used OUT-TO-RU-DS, including recycle hydrocarbons MR-KRDS；
The ratio of the weight flow rate heavy oil RU-F1L-W of the weight flow rate TO-RU-DS-W and heavy oil RU-F1L of hydrogen supply hydrocarbon TO-RU-DS Value is oil ratio KP80, and KP80=(TO-RU-DS-W)/(RU-F1L-W), KP70 are 0.05~1.0.
76. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the heavy hydrocarbon HNBPC heat from hydrogenation cracking reaction conversion ratio of front reaction zone RUA, choosing From one of the following or several:
1. heat from hydrogenation cracking reaction conversion ratio is lower than 20% stage of reaction；
2. heat from hydrogenation cracking reaction conversion ratio is lower than 35% stage of reaction；
3. heat from hydrogenation cracking reaction conversion ratio is lower than 50% stage of reaction.
77. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(4) in separation and recovery process SYS700, separation process MRP-S is set, stabilized hydrogenation reaction product MRP is separated into separation gas MRP-V and separating liquid MRP-L；
The whereabouts of gas MRP-V is separated, one of the following or several is selected from:
1. at least part hydrogen rich gas gas MRP-V becomes cold anticyclone and separates gas MRP-V-CHPS-V after cooling and dewatering, de-oiling, At least part MRP-V-CHPS-V uses return direct hydrogenation liquefaction of coal reaction process RU to use as recycle hydrogen；
2. at least part hydrogen rich gas gas MRP-V becomes cold anticyclone and separates gas MRP-V-CHPS-V after cooling and dewatering, de-oiling, At least part MRP-V-CHPS-V deviates from least part non-hydrogen gas by hydrogen purification process HUPSYS, obtains high-purity Spend hydrogen MRP-V-CHPS-V-PH；At least part high-purity hydrogen MRP-V-CHPS-V-PH is used as recycle hydrogen and is returned to coal Hydrogen direct liquefaction reaction process RU is added to use；
3. at least part hydrogen rich gas gas MRP-V becomes warm high pressure and separates gas MRP-V-KMHPS-V after cooling and dewatering, de-oiling, The warm high pressure separation gas MRP-V-KMHPS-V gravity flow of at least part enters the operating pressure of direct hydrogenation liquefaction of coal reaction process RU The lower secondary use of reaction zone；
4. at least part hydrogen rich gas gas MRP-V, gravity flow into direct hydrogenation liquefaction of coal reaction process RU operating pressure compared with The secondary use of low reaction zone；
5. at least part hydrogen rich gas gas MRP-V, into the removal process of rear portion reaction zone RUB product.
78. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) in hydrocarbon material hydrogenation process RU, the removal process of front reaction zone RUA product, with rear portion reaction zone RUB product Removal process, partly or entirely share.
79. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) in hydrocarbon material hydrogenation process RU, the removal process of the gaseous product of front reaction zone RUA, with rear portion reaction zone The removal process of the gaseous product of RUB partly or entirely shares.
80. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) in hydrocarbon material hydrogenation process RU, the removal process of the liquid material product of front reaction zone RUA, with rear portion reaction zone The removal process of the liquid material product of RUB partly or entirely shares.
81. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) in hydrocarbon material hydrogenation process RU, the removal process of the product slurry of front reaction zone RUA, with rear portion reaction zone The removal process of the product slurry of RUB partly or entirely shares.
82. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon being mainly made of the hydro carbons that normal boiling point is 230~530 DEG C is used TO-RU-DS；
The hydrogen supply hydrocarbon TO-RU-DS of 50 weight % or more, is provided by recycle hydrocarbons MR-KRDS；
In hydrocarbon material front hydrogenation process RUA, the confession being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C is used Hydrogen hydrocarbon TO-RUA-DS；
The hydrogen supply hydrocarbon TO-RUA-DS of 50 weight % or more, is provided by recycle hydrocarbons MR-KRDS.
83. described according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 Method, it is characterised in that:
(1) hydrocarbon material hydrogenation process RU is heavy oil hydrogenation process, and the first raw material RU-F1 is mainly by heavy hydrocarbon The heavy oil RU-F1L of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；
In hydrocarbon material hydrogenation process RU, the hydrogen supply hydrocarbon being mainly made of the hydro carbons that normal boiling point is 230~530 DEG C is used TO-RU-DS；
In hydrocarbon material front hydrogenation process RUA, the confession being mainly made of the hydro carbons that normal boiling point is 230~400 DEG C is used Hydrogen hydrocarbon TO-RUA-DS；
The hydrogen supply hydrocarbon TO-RUA-DS of 100 weight %, is provided by recycle hydrocarbons MR-KRDS.
CN201810109800.5A 2018-01-24 2018-01-24 The stabilized hydrogenation object reuse method of middle matter hydrocarbon in hydrocarbon material either shallow heat from hydrogenation cracked gas product Withdrawn CN110066685A (en)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101927167A (en) * 2010-06-23 2010-12-29 煤炭科学研究总院 Compound coal tar hydrogenation catalyst and preparation method thereof
CN105602616A (en) * 2016-01-30 2016-05-25 何巨堂 Hydrocarbon material hydrogenation method and combined expanded bed hydrogenation reactor
CN106190278A (en) * 2016-07-08 2016-12-07 何巨堂 Cracking intermediate liquid product returns the hydrocarbon heat from hydrogenation cracking method inferior of pre-hydrogenation

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101927167A (en) * 2010-06-23 2010-12-29 煤炭科学研究总院 Compound coal tar hydrogenation catalyst and preparation method thereof
CN105602616A (en) * 2016-01-30 2016-05-25 何巨堂 Hydrocarbon material hydrogenation method and combined expanded bed hydrogenation reactor
CN106190278A (en) * 2016-07-08 2016-12-07 何巨堂 Cracking intermediate liquid product returns the hydrocarbon heat from hydrogenation cracking method inferior of pre-hydrogenation

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