CN102585897B - Method for conversion of low-hydrogen heavy oil to light fractions by hydrogenation with hydrogen-supplying hydrocarbons - Google Patents
Method for conversion of low-hydrogen heavy oil to light fractions by hydrogenation with hydrogen-supplying hydrocarbons Download PDFInfo
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a method for conversion of low-hydrogen heavy oil to light fractions by hydrogenation with hydrogen-supplying hydrocarbons, which is a process for conversion of heavy oil such as coal pitch by hydrogenation with hydrogen-supplying hydrocarbon stream enriched in hydrogen-supplying hydrocarbons. The method has the effects of inhibiting condensation coking speed, increasing liquid product yield in the process of conversion of coal tar heavy oil to light fractions, improving product quality, reducing reaction temperature increase and enhancing stability and safety of device operation. The hydrogen-supplying hydrocarbon stream can be hydrogenation reaction effluents in partial hydrogenation saturation process of bicyclic aromatic hydrocarbons or polycyclic aromatic hydrocarbons or oil products enriched in partial saturated aromatic hydrocarbons obtained in the separation process of bicyclic aromatic hydrocarbons or polycyclic aromatic hydrocarbons. The precursor substance of hydrogen-supplying solvent oil is coal tar fractions with boiling points of 350-450 DEG C, and the hydrogen-supplying solvent oil mainly comprises hydrocarbon components with ordinary boiling points of 350-450 DEG C. The combination of the method for conversion of coal tar heavy oil to light fractions by hydrogenation and method for conversion of coal tar light fractions by hydrogenation constitutes a novel combined process for conversion of full-range fractions of coal tar by hydrogenation.
Description
Technical field
The present invention relates to a kind of hydrogenation lightening method of the low hydrogen content heavy oil that uses hydrogen supply hydrocarbon, say especially, (conventional boiling point is greater than the colloid that is rich in of 450 ℃ conventionally to the present invention relates to a kind of coal tar heavy oil that uses hydrogen supply hydrocarbon, bitum coal tar fraction) hydrogenation lightening method, in hydrogenation lighting reaction process, the existence of hydrogen supply hydrocarbon has the coal tar heavy oil of dispersion and cracking small molecules reduces its polycondensation probability, thereby improve overall raw material hydrocarbon hydrogen richness and reduce hydrogenation load, quickening hydrogen transference speed suppresses the effects such as the condensation of coal tar heavy oil pyrolysis fragment, there is the retention rate (improving light-end products productive rate) that improves pyrolysis molecule, reduce condensation solid productive rate, shorten the reaction process time, reduce reaction overall temperature rise, the extending catalyst operational cycle, improve operational stability texts.
Background technology
Hydrogen supply hydrocarbon described herein, refer to the hydrocarbon component in the hydrogenation lighting reaction process such as coal tar heavy oil at low hydrogen content hydrocarbon ils with hydrogen supply function, hydrogen supply hydrocarbon comprises the double ring arene of fractional saturation, the polycyclic aromatic hydrocarbons of fractional saturation, and the kind of the hydrogen supply hydrocarbon using with gelatin liquefaction is identical with function or close.In hydrogen supply hydrocarbon, the hydrogen supply speed of dihydro body is all greater than tetrahydrochysene body, and the dihydro body of thrcylic aromatic hydrocarbon and the dihydro body of double ring arene are compared, and it is low that its hydrogen supply speed has height to have; Test verified, although polycyclic aromatic hydrocarbons without hydrogen supply capacity, has the ability of hydrogen of transmission.In the time of 400 ℃, the relative hydrogen supply speed of following component is as follows:
Coal tar heavy oil of the present invention refers to conventional boiling point from coal tar higher than 450 ℃ of cuts, is conventionally rich in polycyclic aromatic hydrocarbons, resin and asphalt.
Coal tar heavy oil hydrogenation lighting process of the present invention, refers to coal tar heavy oil hydrocracking and produces the process of conventional boiling point lower than 450 ℃ of cuts, and this process comprises hydrocracking reaction conventionally, and suitable reactor types is floating bed hydrogenation reactor.
A kind of coal tar heavy oil hydrogenation lightening method that uses floating bed hydrogenation reactor has been recorded in patent application 201010217358.1, comprises coal tar raw material pre-treatment and fractionation by distillation, coal tar heavy cut floating bed hydrocracking and the conventional upgrading course of processing of light ends oil.The process characteristic of CN201010217358.1 patent application is using being greater than the part of 370 ℃ in coal tar as the raw material of hydrocracking, adopt suspension bed or bubbling bed hydrocracking reactor to carry out hydrocracking reaction, resultant of reaction is greater than major part (about 80%) the direct circulation freshening cracking again of the mink cell focus (pitch) of 370 ℃, small portion (about 20%) carries out solid-liquid separation, freshening cracking again circulates after solid catalyst, object is the small molecules clean or white that is cracked into as much as possible macromole pitch in coal tar, the catalyzer separating gets rid of outward, the object of getting rid of is outward to remove a small amount of high molecular polymer of generating in cracking process and the catalyzer of inactivation.This technology is owing to being cracked into small molecules product most heavy bitumen freshening, and light oil yield will significantly improve, and the highest oily yield is more than 93%.Each step principal character is as follows:
1. coal tar removing impurities and fractionation: coal tar raw material is carried out to routine dehydration and removed mechanical impurity; Pretreated coal tar is adopted the method for distillation to be separated into be less than 260 ℃, 260～370 ℃ and be greater than 370 ℃ of three cuts, coal tar is less than to 260 ℃ of cuts adopts traditional coal tar dephenolize method to carry out phenol removal, obtain dephenolize oil and crude phenols, crude phenols further rectified purified, rectifying separation obtain phenolic compound as phenol, cresols, xylenol etc.;
2. the hydrocracking of the suspension bed of coal tar heavy cut heterogeneous catalyst (or bubbling bed or slurry state bed):
A, oil, catalyzer, vulcanizer step with slurry: the powdered catalyst particle (composite hydrogenation catalyst that a certain amount of ingredients oil (removed the turning oil of catalyzer and/or be greater than the coal tar heavy fractioning oil of 370 ℃), granularity is less than to 100 μ m, wherein high-activity component metal is 1: 1000 to 1: 10 with the mass ratio of low activity component metals) and vulcanizing agent together with under the agitation condition of 80 ℃～200 ℃, mix and make oil-catalyst slurry, control the solids concn of oil-catalyst slurry in 20～45% scopes;
B, oil-catalyst slurry and all the other are greater than the coal tar heavy fractioning of 370 ℃, and (hydrogenation reaction resultant is through atmospheric tower fractionation gained heavy oil of the normal end with the turning oil that contains catalyzer, account for 4/5ths quantity) mix as compound, compound boosts through feedstock pump, mixed hydrogen, after intensification, enter suspension bed (or bubbling bed or slurry state bed) hydrogenator and carry out hydrocracking reaction, the add-on of catalyzer is to control the metal of active ingredient and coal tar raw material mass ratio as 0.1: 100 to 4: 100, reactor reaction effluent is through high-temperature separator, after low-temperature separator, obtain liquid-solid phase height point oil mixt stream and hydrogen-rich gas two parts.Hydrogen-rich gas is as recycle hydrogen.A liquid-solid phase height point oil mixt is flowed through after atmospheric tower fractionation, obtain being less than 370 ℃ of benzolines, at the bottom of tower, obtain the heavy oil of the normal end (being greater than in 370 ℃ of distillates) that contains catalyzer, wherein heavy oil of most of (about 4/5ths) normal end is recycled directly to and in floating bed hydrogenation reactor, further carries out hydrogenation lighting reaction as turning oil, the heavy oil of the normal end of all the other small portions (about 1/5th) adopts the method for filtering or distill to carry out solid-liquid separation, after separation, obtain catalyst residue and floating bed hydrogenation heavy distillate, the partial solvent that the reaction raw materials of this part heavy distillate or direct and suspension bed mixes or prepares as oil-catalyst slurry, circulation enters in suspension bed or bubbling bed hydrogenator further carries out hydrogenation lighting reaction, and the catalyzer of deviating from gets rid of outward or regenerates, wherein 320～480 ℃ of floating bed hydrogenation temperature of reaction, reaction pressure 8～19MPa, volume space velocity 0.3～3.0h
-1, hydrogen to oil volume ratio 500～2000, catalyzer is the powdered granule coal tar hydrogenation catalyst of supporting compound many metal active constituents, wherein the mass ratio of high-activity component metal and low activity component metals is 1: 1000 to 1: 10, add-on is that activity component metal amount and coal tar raw material mass ratio are 0.1: 100 to 4: 100, the tail oil major part that contains catalyzer that hydrogenation reaction product separates after lightweight oil direct cycles to reactor, small part tail oil carries out being recycled to reactor after Removal of catalyst processing, further lighting, heavy oil all or maximum circulation, realize the object that coal tar maximum is produced lightweight oil and catalyst recycling, greatly improve the utilising efficiency of raw material and catalyzer,
3. the upgrading of lightweight oil processing: whole light ends oil obtained above is carried out to conventional upgrading processing, be that suspension bed or bubbling bed hydrogenation reaction product are less than 260～370 ℃ of cuts that 370 ℃ of benzolines obtain with coal tar fractional distillation step and are less than the stock oil as distillate upgrading processing together with 260 ℃ of dephenolize oil, processing oil fuel and industrial chemicals, naphtha fraction wherein can adopt catalytic reforming or catalytic reforming-Aromatics Extractive Project process integration to produce gasoline or aromatic hydrocarbon product, coal bavin cut can adopt hydrofining or selective hydrogenation cracking technology to produce aviation kerosene, diesel product.
A significant feature of patent application 201010217358.1 is that 370～480 ℃ of cuts in coal tar are all introduced to hydrocracking process of suspended bed with the coal tar heavy oil that is greater than 480 ℃.
In fact, described in patent application 201010217358.1, the goal response of hydrocracking process of suspended bed has been that target lysate is the coal tar heavy oil (bituminous matter that conventional boiling point is greater than 450 ℃, colloid, the macromole such as polycyclic aromatic hydrocarbons or group) thermo-cracking and " stabilized hydrogenation " of realizing cleaved fragment of top efficiency, reduce the probability of the synthetic charcoal reaction of pyrocondensation and cracking gas making reaction, in order to realize above-mentioned intention, based target lysate (bituminous matter, colloid, the macromole such as polycyclic aromatic hydrocarbons or group) viscosity that has is high, easily condensation and cleaved fragment " stabilized hydrogenation " need the feature of rapid, high volume hydrogen supply, in the warm and hydrocracking reaction process of target lysate, must use suitable solvent oil to serve as " dispersion agent, heat-carrying agent, hydrogen supply agent ", to stop the thermal polycondensation of target lysate, reduce reaction process temperature rise, hydrogen supply is realized and " is stablized cleaved fragment fast, stop its thermal polycondensation ".
The solvent oil that patent application 201010217358.1 is used is that conventional boiling point is the coal tar fraction of 370～450 ℃, has following characteristics:
1. one of advantage is convenient sources, is the concomitant product of coal tar heavy oil;
2. two of advantage is that " conventional boiling point is the coal tar fraction of 370～450 ℃ " is rich in polycyclic aromatic hydrocarbons, colloid, has good mutual solubility with coal tar heavy oil, is good dispersion agent;
3. one of shortcoming is that " conventional boiling point is the coal tar fraction of 370～450 ℃ " is rich in polycyclic aromatic hydrocarbons, colloid, thermostability is poor, hydrogen supply capacity is poor, in target cracking component is, the heat-processed of coalite tar heavy oil suppresses coking ability, the easy coking of coal tar heavy oil hydrogenation reaction feed coal tar heavy oil heater boiler tube;
4. two of shortcoming to be that " conventional boiling point is the coal tar fraction of 370～450 ℃ " is rich in polycyclic aromatic hydrocarbons, colloid, hydrogen supply capacity poor, in target cracking component is, the hydrocracking process of coalite tar heavy oil can not effectively suppress " the thermal condensation reaction " of cracking fragment, and coke yield is high, gas yield is high;
5. three of shortcoming is that " conventional boiling point is the coal tar fraction of 370～450 ℃ " is wherein rich in polycyclic aromatic hydrocarbons, colloid, it itself is good hydrofining raw material, can be converted into good hydrocracking raw material through hydrofining, so process that its liquid yield is high, gas yield is low, the process of hydrocracking is directly introduced 370～450 ℃ of cuts in coal tar in patent application 201010217358.1, make it experience nonideal hydrofining one hydrocracking process, because the leading function of the hydrocracking process of suspended bed of patent application 201010217358.1 is " crackings ", be suitable for suspension bed hydrogenation catalyst and the reactive system function (apparent hydrofining function and hydrocracking function) of coal tar heavy oil, conventionally not best for 370～450 ℃ of coal tar fractions, such as the region operation temperature of the floating bed hydrogenation process of coal tar heavy oil far exceeds the fixed bed hydrogenation treating process of coal tar fraction conventionally up to 420～450 ℃, the common operating temperature range of 370～420 ℃ of fixed bed hydrogenation cracking process, its cracking reaction probability must be higher,
6. four of shortcoming are, compared with petroleum base heavy-oil hydrogenation cracking process, solvent oil hydrogen richness is much lower, and solvent oil hydrogenation reaction hydrogen-consuming volume is much bigger, reaction heat is much bigger, that is to say that its heat-carrying agent efficiency (controlling general reaction process temperature rise amplitude ability) is much lower;
7. five of shortcoming are, polycyclic aromatic hydrocarbons that " conventional boiling point is the coal tar fraction of 370～450 ℃ " contained, colloid molecule is large, viscosity is large, heat movement speed is low; .
In petroleum base heavy oil floating bed hydrocracking process, the component hydrogen richness that serves as solvent oil is high, contain abundant dicyclo or polynuclear plane hydrocarbon, the aromatic hydrocarbons macromole that contains abundant fractional saturation, solvent oil itself comprise abundant biography hydrogen hydrocarbon and or hydrogen supply hydrocarbon, hot procedure anti-coking function is strong, hydrocracking process hydrogen-consuming volume is little, reaction heat is less, the method for hydrogen cracking of coalite tar heavy oil in described in contrast aforementioned patent applications 201010217358.1, the solvent oil hydrogen richness that patent application 201010217358.1 is used is low, hydrogen supply capacity is poor low, its hot procedure anti-coking function is poor, hydrocracking process hydrogen-consuming volume is large, the shortcoming that reaction heat is larger is obvious.
It is considered herein that, aforementioned patent applications 201010217358.1 methods exist a use, and " hydrogen richness is low, the easy condensation of being heated, hydrogen supply capacity is low " the technological deficiency of solvent oil, based on this conceptual understanding, the present invention proposes the scheme of a kind of improvement " solution oil characteristic " and uses the hydrogen supply dissolvent oil of excellent property instead, the hydrogen supply dissolvent oil being conveniently easy to get can be that " conventional boiling point is the hydrofined oil (or hydrogenation modification oil) of the coal tar fraction of 370～450 ℃, because its aromatic hydrocarbon substance that is rich in polynuclear hydrocarbon and fractional saturation possesses the mutual solubility good with coal tar heavy oil, (this feature has determined dispersion agent, heat-carrying agent function), because the aromatic hydrocarbon substance that its hydrogen richness is high and be rich in fractional saturation possesses good thermostability and good hydrogen supply capacity, (this feature has determined coking inhibitor, hydrogen supply agent function), can realize following main purpose:
1. improve anti-coking (the suppressing in other words coking) ability of the overall stock oil of floating bed hydrocracking in hot procedure, reduce fouling or the coking speed of interchanger, heating furnace tube, prolong operation cycle;
2. improve the overall stock oil hydrogen richness of floating bed hydrocracking, reduce the overall hydrogen-consuming volume of hydrocracking process, reduce heat of reaction, reduce reaction temperature rising, stable operation temperature;
3. realize quick hydrogen supply at hydrocracking process of suspended bed, suppress " thermal polycondensation " reaction of " cleaved fragment " of coal tar heavy oil, the retention rate (improving light-end products productive rate) with raising pyrolysis molecule reduces condensation solid productive rate simultaneously, shortens the reaction process time, improves catalyst efficiency texts, realizes highly selective, the highly effective hydrogenation cracking reaction of coal tar heavy oil;
4. at hydrocracking process of suspended bed, suppress or reduce the heat movement speed of the pyrocondensation of solvent oil and reaction, raising solvent oil;
5. the fractionation of slurry-bed hydrocracking effluent is take 450 ℃ as dividing point, 370～450 ℃ of cuts remove unifining process, strengthen the proportion of the hydrofining function in integrated artistic, optimize the distribution of hydrogenating function in integrated artistic, reduce hydrocracking process of suspended bed load, be beneficial to and improve whole technological process liquid yield.
Can find out from above contrast, in patent application 201010217358.1 methods, in " conventional boiling point is the work flow of the coal tar fraction of 370～450 ℃ " allomeric function, " floating bed hydrocracking " is that hydrocracking proportion is larger; In the inventive method, " conventional boiling point is the work flow of the coal tar fraction of 370～450 ℃ " is just contrary: the refining B1 of fixed bed hydrogenation is that hydrofining proportion is larger.
The present invention is compared with patent application 201010217358.1 methods, " conventional boiling point is the work flow of the coal tar fraction of 370～450 ℃ " is just contrary: in patent application 201010217358.1, the work flow of " conventional boiling point is the coal tar fraction of 370～450 ℃ " is " first to pass through floating bed hydrocracking (comprising the circulation cracking that is greater than 370 ℃ of cuts), what then floating bed hydrocracking generation was oily passes through hydrogenation upgrading lower than 370 ℃ of cuts ", in the present invention, the work flow of " conventional boiling point is the coal tar fraction of 370～450 ℃ " is " first through the refining B1 of fixed bed hydrogenation, then the refining oil that generates of fixed bed hydrogenation is through floating bed hydrocracking B2, last floating bed hydrocracking generates oil and enters the refining B1 recycled hydrofining of fixed bed hydrogenation ".The fundamental difference of two kinds of methods that Here it is
Therefore, the first object of the present invention is to provide a kind of hydrogenation lightening method that uses the coal tar heavy oil of hydrogen supply hydrocarbon to produce clean fuel oil.
The second object of the present invention is to provide a kind of full cut coal tar hydrogenating to transform the method for preparing liquid fuel.
The 3rd object of the present invention is to provide the method for coalite tar hydrocracking preparing liquid fuel in a kind of full cut.
The 4th object of the present invention is to provide the method for coalite tar Unionfining conversion preparing liquid fuel in a kind of coal-tar heavy oil cut and full cut.
The 5th object of the present invention is to provide a kind of method that is rich in the petroleum base hydro carbons inferior of double ring arene and/or polycyclic aromatic hydrocarbons and the Unionfining of middle coalite tar pitch conversion preparing liquid fuel.
The 6th object of the present invention is to provide a kind of method of high temperature tar carbolineum or washing oil hydrocracking preparing liquid fuel.
The 7th object of the present invention is to provide a kind of inferior heavy oil hydrogenation lightening method that uses hydrogen supply hydrocarbon.
The 8th object of the present invention is to provide a kind of hydrogenation modification process and low hydrogen content hydrocarbon oil hydrogenation lighting process by the hydrocarbon ils that is rich in double ring arene and/or polycyclic aromatic hydrocarbons to combine the method for processing.
In fact, the overall characteristic of coal tar heavy oil is: hydrogen richness very low (middle coalite tar hydrogen richness be usually less than 7%, generally lower than 6.5%) and carbon content is high, when comparatively high temps (such as 250 ℃), be high viscosity fluid, but be solid-state under normal temperature, high-temperature heating is easily decomposed coking, and what can look is " the plan coal body that in coal fugitive constituent, high boiling hydrocarbon forms ".By " plan coal body " this concept, it is considered herein that direct hydrogenation liquefaction of coal process is used this technological concept of hydrogen supply dissolvent oil can transplant the hydrocracking process that is used in coal tar heavy oil, thereby patent application 201010217358.1 methods are realized to the improvement of technical process, if observe the present invention according to above-mentioned " plan coal body " concept, the present invention's design is natural.The hydrocracking reaction process of the coal tar heavy oil of contrast patent application 201010217358.1 methods, the present invention strengthened solvent oil hydrogen supply capacity, improved the hydrogen richness of solvent oil.
An important feature of coal tar heavy oil processing unit (plant) is small scale, for example extensive middle coalite tar amount of finish is by 1,000,000 tons/year of calculating, also only 10～200,000 tons/year of coal tar heavy oil quantity, because engineering must reduce investment as far as possible, therefore the combination of the hydrocracking reaction process of coal tar heavy oil and the hydro-upgrading process of coal tar lighting end is also inevitable.
Summary of the invention
The hydrogenation lightening method of a kind of low hydrogen content heavy oil that uses hydrogen supply hydrocarbon of the present invention, comprises the steps:
Heavy oil streams HDS is mainly made up of higher than the hydrocarbon component HD of 450 ℃ conventional boiling point, and heavy oil streams HDS is selected from one or more in following material:
1. coalite tar heavy oil fraction;
2. coal-tar middle oil heavy oil fraction;
3. coal-tar heavy oil heavy oil fraction;
4. petroleum base heavy oil thermal course of processing gained heavy oil fraction product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;
5. shale oil basic weight oil hot procedure gained heavy oil fraction product;
6. tar sand basic weight oil hot procedure gained heavy oil fraction product;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, under hydrogen and catalyzer existence condition, the hydrogenation lighting reaction HPU21R that heavy oil streams HDS comprises hydrocracking reaction, at least a portion hydrocarbon component HD completes hydrocracking reaction and obtains reaction effluent HPU21P, it is characterized in that the hydrogen supply hydrocarbon stream SHS that contains hydrogen supply hydrocarbon SH enters hydroconversion reaction zone HPU21, in hydrogenation reaction HPU21R process, hydrogen supply hydrocarbon SH contacts with hydrocarbon component HD;
Described hydrogen supply hydrocarbon SH refer to fractional saturation double ring arene and or the polycyclic aromatic hydrocarbons of fractional saturation; In logistics SHS, gum level is lower than 10 % by weight, and asphalt content is lower than 1 % by weight; In logistics SHS, in hydrogen supply hydrocarbon SH weight and logistics SHS, the ratio of conventional liquid hydrocarbon component gross weight exceeds in heavy oil streams HDS the ratio at least 3% of conventional liquid hydrocarbon component gross weight in hydrogen supply hydrocarbon SH weight and heavy oil streams HDS; In logistics SHS, conventional liquid hydrocarbon component protium weight in average content exceeds the protium weight content at least 2% of heavy oil streams HDS;
Hydrogen supply hydrocarbon stream SHS is prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target from processing hydrogen supply hydrocarbon precursor logistics SHSBF's with hydrogen supply hydrocarbon; In logistics SHS, hydrogen supply hydrocarbon SH weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight; In the weight rate SHSW of hydrogen supply hydrocarbon stream SHS and heavy oil streams HDS, conventional boiling point is higher than the ratio K=SHSW/HDW of the weight rate HDW of the hydrocarbon component HD of 450 ℃, K=0.1～10.
It is middle coalite tar heavy oil and hydrogen supply hydrocarbon precursor logistics SHSBF is the processing of combining of middle coalite tar lighting end that the present invention is particularly suitable for heavy oil streams HDS, it is characterized in that: hydrogen richness is mainly made up of higher than the hydrocarbon component HD of 450 ℃ conventional boiling point lower than the heavy oil streams HDS of 8 % by weight; Heavy oil streams HDS is selected from one or both in following material:
1. coalite tar heavy oil fraction;
2. coal-tar middle oil heavy oil fraction;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor HPU21-SB, charging autoreactor HPU21-SB bottom enters, temperature be 300～500 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 500: 1～4000: 1, hydrogenation catalyst HPU21-CAT add weight be HDS weight 0.01～5.0%, volume space velocity is 0.1～10.0hr
-1reaction conditions under, complete the hydrogenation lighting reaction that comprises hydrocracking reaction and obtain hydrogenation lighting reaction effluent HPU21P, flow out on reaction effluent HPU21P autoreactor HPU21-SB top;
Hydrogen supply hydrocarbon stream SHS is prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target from processing hydrogen supply hydrocarbon precursor logistics SHSBF's with hydrogen supply hydrocarbon; In logistics SHS, hydrogen supply hydrocarbon SH weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight; In the weight rate SHSW of hydrogen supply hydrocarbon stream SHS and heavy oil streams HDS, conventional boiling point is higher than the ratio K=SHSW/HDW of the weight rate HDW of the hydrocarbon component HD of 450 ℃, K=0.2～5;
Hydrogen supply hydrocarbon precursor logistics SHSBF is selected from one or more in following logistics:
1. be mainly the logistics of the coalite tar fractions consisting of 350～450 ℃ by conventional boiling point;
2. be mainly the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ by conventional boiling point;
3. be mainly the logistics of the coal-tar heavy oil fractions consisting of 230～450 ℃ by conventional boiling point;
4. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coalite tar fractions consisting of 350～450 ℃ of cuts by comprising conventional boiling point;
5. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ of cuts by comprising conventional boiling point;
6. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coalite tar fractions consisting of 350～450 ℃ of cuts by the conventional boiling point after dephenolize;
7. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ of cuts by the conventional boiling point after dephenolize.
When hydrogen supply hydrocarbon precursor logistics SHSBF of the present invention is the middle coalite tar cut of 350～450 ℃, the selection of hydrogen supply hydrocarbon stream SHS is: at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS hydrogen supply hydrocarbon processed hydrogenation reaction HPU1R forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar, at least a portion hydrocarbon component MF completes hydrogenation modification reaction and obtains hydrogenation reaction effluent HPU1P, and the hydrogen supply hydrocarbon stream SHS obtaining based on hydrogenation reaction effluent HPU1P is selected from one or several of following logistics:
1. reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
2. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1-HSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
3. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1-HSO is as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21, and the hot high score oil of at least a portion HPU1-HSO step-down, degassed rear gained liquid HPU1-HSOA enter hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
4. reaction effluent HPU1P enters cold anticyclone sepn process HPU1-CS and is separated into cold high score oil HPU1-CSO and cold high score gas HPU1-CSV, the cold high score oil of at least a portion HPU1-CSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
5. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1P0 fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
6. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion mainly by conventional boiling point be 350～450 ℃ be rich in logistics that hydrogen supply hydrocarbon component forms as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS.
When hydrogen supply hydrocarbon precursor logistics SHSBF of the present invention is the middle coalite tar cut of 60～450 ℃, the selection of hydrogen supply hydrocarbon stream SHS is: at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from containing of coal tar conventional boiling point be that the logistics LMFS of 60～450 ℃ of hydrocarbon LMF completes deep hydrofinishing reaction HPU1R and is converted into hydrogenation reaction effluent HPU1P, conventional boiling point is that the hydrocarbon of 60～350 ℃ is converted into petroleum naphtha and diesel component, conventional boiling point is that the hydrocarbon of 350～450 ℃ is converted into the hydrogenation tail oil that is rich in hydrogen supply hydrocarbon SH, the hydrogen supply hydrocarbon stream SHS obtaining based on hydrogenation reaction effluent HPU1P is selected from one or several of following logistics:
1. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1-HSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
2. the intermediate reaction effluent HPU1MP that is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon enters thermal high sepn process HPU1M-HS and is separated into hot high score oil HPU1M-HSO and hot high score gas HPU1MP-HSV, the hot high score oil of at least a portion HPU1M-HSO is as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21, after the degassed rear gained degas oil HPU1M-HSOA of the hot high score oil HPU1M-HSO step-down of at least a portion mixes with heavy oil streams HDS, enters hydroconversion reaction zone HPU21;
3. separating reaction effluent HPU1P obtains hydrogenated oil HPU1P0 and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
4. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion mainly by conventional boiling point be 350～450 ℃ be rich in logistics that hydrogen supply hydrocarbon component forms as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS.
When hydrogen supply hydrocarbon precursor logistics SHSBF of the present invention is the middle coalite tar cut of 60～450 ℃, at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from coal tar be mainly that the hydrogenation modification that logistics LMFS that 60～450 ℃ of hydrocarbon LMF forms carries out reacts HPU1R by conventional boiling point, can select to produce to greatest extent hydrogen supply hydrocarbon is target.
Heavy oil streams HDS of the present invention mainly by conventional boiling point higher than 450 ℃ hydrogen richness while forming lower than the coal tar heavy fractioning HD of 6.5 % by weight, turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight, temperature be 320～480 ℃, pressure be 10.0～20.0MPa, hydrogen/stock oil volume ratio be 1000: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.1～2.0%, volume space velocity is 0.2～5.0hr
-1reaction conditions under operate; In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.3～3.
When the hydroconversion reaction zone HPU3 of setting of the present invention take the upgrading of lightweight carburetion as target, the first mode of operation is:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst PU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
When the hydroconversion reaction zone HPU3 of setting of the present invention take the upgrading of lightweight carburetion as target, the second mode of operation is:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21P0 and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
When the hydroconversion reaction zone HPU3 of setting of the present invention take the upgrading of lightweight carburetion as target, the third mode of operation is:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21P0 and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that the hydrocarbon that at least a portion is mainly 350～450 ℃ by conventional boiling point forms removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target; The logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
When the present invention arranges hydrogenation upgrading cascade reaction district HPU22, be characterised in that:
The hydrogenation reaction effluent HPU21P that turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight enters the hot high score fluid body HPU21P-HSL that hot high-pressure separator HPU21P-HS is separated into hot high score gas HPU21P-HSV and contains solid particulate, and hot high-pressure separator HPU21P-HS is to operate under 350～500 ℃, the pressure condition that is 6.0～28.0MPa in temperature; The main oil product being made up of higher than the hydrocarbon of 450 ℃ conventional boiling point that heat of dissociation high score fluid body HPU21P-HSL obtains enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and contacts with catalyzer HPU21-CAT;
Hot high score gas HPU21P-HSV enters hydrogenation upgrading cascade reaction district HPU22, the main liquid hydrocarbon being made up of lower than the hydrocarbon of 450 ℃ conventional boiling point that heat of dissociation high score oil HPU21P-HSL obtains enters hydrogenation upgrading cascade reaction district HPU22, the main logistics LFS being made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar existing enters hydrogenation upgrading cascade reaction district HPU22, hydrogenation upgrading cascade reaction district HPU22 operational condition is: temperature is 280～440 ℃, pressure is 6.0～28.0MPa, hydrogen/stock oil volume ratio is 300: 1～3000: 1, hydrogenation catalyst HPU22-CAT volume space velocity is 0.05～5.0hr
-1, complete hydrogenation upgrading cascade reaction and obtain hydrogenation upgrading cascade reaction effluent HPU22P,
At the separate part HPU22P-S of hydrogenation upgrading cascade reaction effluent HPU22P, separate hydrogenation upgrading cascade reaction effluent HPU22P and obtain hydrogen-rich gas HPU22PH and hydrogenated oil HPU22PO, at least a portion hydrogen-rich gas HPU22PH returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
At hydrogenated oil HPU22PO separate part HPU22PO-FS, separate hydrogenated oil HPU22PO and obtain gas and narrow fraction oil product.
When the present invention arranges hydrogenation upgrading cascade reaction district HPU22, at hydrogenated oil HPU22PO separate part HPU22PO-FS, separate the main oil product being formed higher than the hydrocarbon of 350 ℃ by conventional boiling point that hydrogenated oil HPU22P0 obtains, enter the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and catalyzer HPU21-CAT and contact or enter the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and contact with catalyzer HPU1-CAT.
The hydrogenation upgrading cascade reaction district HPU22 that the present invention arranges should use ebullated bed reactor or suspended-bed reactor, with the raw material that adapts to contain tiny solid particle.
For simple flow, the hydroconversion reaction zone HPU1 that the present invention can be prepared as target with hydrogen supply hydrocarbon by heavy oil lighting generation oil introducing separation completes upgrading object, and its first flow process is:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1P0 and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separation hydrogenated oil HPU1PO obtains being rich in the logistics of hydrogen supply hydrocarbon component, and what at least a portion was mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21P0 and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target.
For simple flow, the hydroconversion reaction zone HPU1 that the present invention can be prepared as target with hydrogen supply hydrocarbon by heavy oil lighting generation oil introducing separation completes upgrading object, and its second flow process is:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separation hydrogenated oil HPU1PO obtains being rich in the logistics of hydrogen supply hydrocarbon component, and what at least a portion was mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21P0 and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target.
When hydrogen supply hydrocarbon precursor logistics SHSBF is the middle coalite tar cut of 350～450 ℃, for simple flow, the first flow process of the present invention is:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P, and at least a portion reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21P0 and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics HPU3-F1 that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
When hydrogen supply hydrocarbon precursor logistics SHSBF is the middle coalite tar cut of 350～450 ℃, for simple flow, the second flow process of the present invention is:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from coal tar be mainly that logistics MFS that 350～450 ℃ of hydrocarbon MF forms completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P by conventional boiling point, at least a portion reaction effluent HPU1P is used as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that the hydrocarbon that at least a portion is mainly 350～450 ℃ by conventional boiling point forms removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target; The logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
When hydrogen supply hydrocarbon precursor logistics SHSBF is the middle coalite tar cut of 350～450 ℃, for simple flow, the third flow process of the present invention is:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P, and at least a portion reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21P0 fractionation part, separate hydrogenated oil HPU21P0 and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
The present invention arranges hydrocracking reaction process HPU4 and processes while being prepared as the separating obtained oil product HPU1PO-DO being made up of higher than 350 ℃ of hydrocarbon conventional boiling point of hydrogenated oil HPU1PO of hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon, for simple flow, the present invention is characterised in that:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate hydrogenated oil HPU1PO and obtain gas, narrow fraction oil product, the logistics that is rich in hydrogen supply hydrocarbon component that part is mainly made up of higher than 350 ℃ of hydrocarbon conventional boiling point is as hydrogen supply hydrocarbon stream SHS; The oil product HPU1PO-DO that part is mainly made up of higher than 350 ℃ of hydrocarbon conventional boiling point goes hydrocracking reaction process HPU4 to be converted into hydrocracking reaction effluent HPU4P, and hydrocracking reaction effluent HPU4P mixes with one or several in following logistics:
1. be prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon;
2. the hydrogenation upgrading cascade reaction effluent HPU22P existing;
3. the hydrogenation reaction effluent HPU3P of the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target existing.
In the middle of existing, the hydroconversion reaction zone HPU21 that the present invention turns to target with heavy oil lightweight when turning oil system, it is characterized in that:
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, the main heavy oil streams HDS being made up of higher than the coal tar heavy fractioning HD of 450 ℃ conventional boiling point enters the first reaction zone HPU211, temperature be 300～500 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 500: 1～4000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.05～5%, volume space velocity is 0.2～5.0hr
-1reaction conditions under, complete shallow degree hydrocracking reaction and obtain intermediate reaction effluent HPU211P; The intermediate reaction effluent HPU211P1 of first part is separated into intermediate gas and middle hydrocarbon ils, and middle hydrocarbon ils returns to the first reaction zone HPU211 as middle circulation hydrocarbon ils and contacts with hydrogenation catalyst HPU211-CAT; The second reaction zone HPU212 that second section intermediate reaction effluent HPU211P2 and intermediate gas enter hydroconversion reaction zone HPU21 carries out overhydrocracking reaction and obtains hydrogenation reaction effluent HPU212P, and reaction effluent HPU212P is as the hydrogenation reaction effluent HPU21P that turns to the hydroconversion reaction zone of target with heavy oil lightweight; The ratio K=HPU211P1W/HPU211P2W of the weight rate HPU211P1W of the intermediate reaction effluent HPU211P1 of first part and the weight rate HPU211P2W of second section intermediate reaction effluent HPU211P2, conventionally K=0.5～2.
When the present invention exists two-way hydrogen supply hydrocarbon stream, the first flow scheme is:
There is two-way hydrogen supply hydrocarbon precursor material: lightweight hydrogen supply hydrocarbon precursor SHB1 and heavy hydrogen supply hydrocarbon precursor SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 obtains hydrogenation reaction effluent HPU11P through aromatic hydrogenation fractional saturation process HPU11, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, hydrogenation reaction effluent HPU11P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 obtains hydrogenation reaction effluent HPU12P through aromatic hydrogenation fractional saturation process HPU12, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, hydrogenation reaction effluent HPU12P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD.
When the present invention exists two-way hydrogen supply hydrocarbon stream, the second flow scheme is:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 is the distillate HPU11PSP of 60～350 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU11 gained hydrogenation reaction effluent HPU11P, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1; Distillate HPU11PSP enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 is the distillate HPU12PSP of 350～450 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU12 gained hydrogenation reaction effluent HPU12P, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1; Distillate HPU12PSP enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and makes hydrogen supply hydrocarbon and coal-tar hydrocarbon component HD connect angle to touch.
When the present invention exists two-way hydrogen supply hydrocarbon stream, the third flow scheme is:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 obtains hydrogenation reaction effluent HPU11P through aromatic hydrogenation fractional saturation process HPU11, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 obtains hydrogenation reaction effluent HPU12P through aromatic hydrogenation fractional saturation process HPU12, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～20.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
There is the first reaction zone HPU211 and the second reaction zone HPU212 of serial operation in the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, coal tar heavy oil HDS enters the first reaction zone HPU211, SHB1 transforms the reaction effluent HPU11P obtaining and enters the first reaction zone HPU211 hydrogen supply hydrocarbon is contacted with coal-tar hydrocarbon component HD or its intermediate product, obtains the first reaction zone HPU211 reaction effluent HPU211P; Reaction effluent HPU211P enters the second hydroconversion reaction zone HPU212, SHB2 transforms the reaction effluent HPU12P obtaining and enters the second hydroconversion reaction zone HPU212 hydrogen supply hydrocarbon is contacted with the intermediate product of coal-tar hydrocarbon component HD, and second reaction zone HPU212 service temperature is compared with at least 10 ℃ of the first reaction zone HPU211 service temperature height.
When the present invention exists two-way hydrogen supply hydrocarbon stream, the 4th kind of flow scheme is:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 is the distillate HPU11PSP of 60～350 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU11 gained hydrogenation reaction effluent HPU11P, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 is the distillate HPU12PSP of 350～450 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU12 gained hydrogenation reaction effluent HPU12P, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
There is the first reaction zone HPU211 and the second reaction zone HPU212 of serial operation in the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, coal-tar hydrocarbon component HD enters the first reaction zone HPU211, SHB1 transforms the distillate HPU11PSP obtaining and enters the first reaction zone HPU211 hydrogen supply hydrocarbon is contacted with coal-tar hydrocarbon component HD or its intermediate product, obtains the first reaction zone HPU211 reaction effluent HPU211P; Reaction effluent HPU211P enters the second hydroconversion reaction zone HPU212, SHB2 transforms the distillate HPU12PSP obtaining and enters the second hydroconversion reaction zone HPU212 hydrogen supply hydrocarbon is contacted with the intermediate product of coal-tar hydrocarbon component HD, and second reaction zone HPU212 service temperature is compared with at least 15 ℃ of the first reaction zone HPU211 service temperature height.
The first flow scheme that the present invention processes full cut coal tar is:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the lighting end LMFS being mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point and the last running HS being mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point, last running HS is as heavy oil streams HDS, and lighting end LMFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB completes deep hydrofinishing reactive moieties at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and obtains hydrogenation reaction effluent HPU1P, the hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 200～440 ℃, pressure are as 6.0～28.0MPa, HPU21-CAT volume space velocity are as 0.05～10.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, in hydrogenation reaction effluent HPU1P, full cut diesel-fuel cetane number is higher than 24;
Separate the distillate HPU1P-FHO that hydrogenation reaction effluent HPU1P obtains gas, the main distillate HPU1P-FLO being made up of lower than the hydrocarbon of 350 ℃ conventional boiling point and is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point, at least a portion distillate HPU1P-FHO enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight after mixing with heavy oil streams HDS as logistics SHS, and in logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, temperature be 350～500 ℃, pressure be 3.0～28.0MPa, hydrogen/stock oil volume ratio be 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under, carry out hydrogenation lighting reaction and obtain hydrogenation lighting reaction effluent HPU21P; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.2～5; Hydrogenation lighting reaction effluent HPU21P enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21-HPV and contains solid particulate, hot high score gas HPU21-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU21-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to hydroconversion reaction zone HPU21 and recycles;
The hot high score fluid of fractionation body HPU21-HPL and or cold high score fluid body HPU21-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight; Outer oil extraction WPY penetration depth hydrofining reaction part HPU1 contacts with its Hydrobon catalyst, and outer oil extraction WPY completes hydrogenation upgrading reaction, and the hydrogenation upgrading reaction effluent obtaining enters in hydrogenation reaction effluent HPU1P.
The first flow scheme that the present invention processes full cut coal tar comprises while extracting phenol component process, it is characterized in that:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the carbolic oil that the hydrocarbon that is mainly 160～250 ℃ by conventional boiling point forms, carbolic oil is through becoming dephenolize oil containing after alkali aqueous solution extraction step, dephenolize oil enters treating tower, using conventional boiling point be 100～140 ℃ with the segregative hydrocarbon ils of water as interval hydrocarbon introduce treating tower, the low oily quantity for the treatment of tower tower is 5～20% of dephenolize oil, all the other dephenolizes oil autofining tower lateral line withdrawal functions, the tower top oil gas mainly be made up of interval hydrocarbon and water vapor leaves to be refined tower top and is separated into water and oil after cooling; The low oil for the treatment of tower tower removes coal tar fractional distillation tower; Treating tower side line oil enters hydrogenation reaction part HPU1 as dephenolize oil after refining as hydrogenating materials and contacts with its hydrogenation catalyst.
The preferred operational condition of the first flow scheme that the present invention processes full cut coal tar is:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～420 ℃, pressure are as 10.0～25.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are as 0.1～2.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 800: 1～2500: 1, in hydrogenation reaction effluent HPU1P, full cut diesel-fuel cetane number is higher than 28;
In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight;
Turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight, temperature be 350～480 ℃, pressure be 10.0～25.0MPa, hydrogen/stock oil volume ratio be 800: 1～2500: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under operate, in the whole hydrocarbon feeds of hydroconversion reaction zone HPU21, conventional boiling point is greater than 40 % by weight higher than the cracking rate of the hydrocarbon component of 450 ℃.
When the present invention processes the first flow scheme of full cut coal tar, the weight rate SHW of hydrogen supply hydrocarbon SH and the ratio K=SHW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, conventionally K=0.3～3.
The second flow scheme that the present invention processes full cut coal tar is:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, the first cut LFS that in separation, coalite tar obtains mainly be made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, the second cut MFS and the main last running HS being formed higher than the hydrocarbon of 450 ℃ by conventional boiling point that mainly the hydrocarbon that is 350～450 ℃ by conventional boiling point forms, last running HS is as heavy oil streams HDS, and the second cut MFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB is converted into hydrogenation reaction effluent HPU1P at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, and hydroconversion reaction zone HPU1 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
At least a portion hydrogenation reaction effluent HPU1P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight as logistics SHS after mixing with heavy oil streams HDS, and in logistics SHS, hydrogen supply hydrocarbon SH weight accounts in logistics SHS conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
The hydroconversion reaction zone HPU21 that turns to target take heavy oil lightweight in temperature as 350～500 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio add as 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT weight as HD weight 0.01～2%, volume space velocity completes hydrogenation lighting reaction and obtains hydrogenation reaction effluent HPU21P under the reaction conditions of 0.1～10.0hr-1; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.1～10; At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor, charging autoreactor bottom enters, and flow out on hydrogenation lighting reaction effluent HPU21P autoreactor top;
Reaction effluent HPU21P enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21-HPV and contains solid particulate, hot high score gas HPU21-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU21-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
The hot high score fluid of fractionation body HPU21-HPL and or cold high score fluid body HPU21-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight;
The hydroconversion reaction zone HPU3 of oil extraction WPY hydrogenation upgrading reaction zone take the upgrading of lightweight carburetion as target is outside that 260～440 ℃, pressure are that 6.0～28.0MPa, hydrogen/stock oil volume ratio are that 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.05～5.0hr in temperature
-1reaction conditions under, outer oil extraction WPY and the first cut LFS that combines processing complete the reaction of hydrogenation upgrading system, obtain hydrogenation upgrading reaction effluent HPU3P;
At the separate part HPU3P-HS of hydrogenation upgrading reaction effluent, separation hydrogenation upgrading reaction effluent HPU3P obtains hydrogen-rich gas HPU3P-HSV and upgrading generates oily HPU3P-0P, and the hydroconversion reaction zone HPU3 that at least a portion hydrogen-rich gas HPU3P-HSV returns take the upgrading of lightweight carburetion as target recycles;
Separate upgrading and generate oily HPU3P-0P, obtain gas products and narrow fraction oil product.
The third flow scheme that the present invention processes full cut coal tar is:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the lighting end LMFS being mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point and the last running HS being mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point, last running HS is as heavy oil streams HDS, and lighting end LMFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB is converted into hydrogenation reaction effluent HPU1P through the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, and hydroconversion reaction zone HPU1 is that 200～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
At least a portion hydrogenation reaction effluent HPU1P enters hydroconversion reaction zone HPU21 as logistics SHS after mixing with heavy oil streams HDS, in logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
Hydroconversion reaction zone HPU21 temperature be 300～550 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0,1～10.0hr
-1reaction conditions under, carry out hydrogenation lighting reaction and obtain hydrogenation lighting reaction effluent HPU21P; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.1～10; At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor, charging autoreactor bottom enters, and flow out on hydrogenation lighting reaction effluent HPU21P autoreactor top;
The reaction effluent HPU21P that turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21-HPV and contains solid particulate, hot high score gas HPU21-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU21-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
The hot high score fluid of fractionation body HPU21-HPL and or cold high score fluid body HPU21-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight;
Outer oil extraction WPY hydrogenation upgrading reaction zone HPU3 is that 260～440 ℃, pressure are that 6.0～28.0MPa, hydrogen/stock oil volume ratio are that 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.05～5.0hr in temperature
-1reaction conditions under, outer oil extraction WPY completes hydrogenation upgrading system reaction, obtains hydrogenation upgrading reaction effluent HPU3P;
At the separate part HPU3P-HS of hydrogenation upgrading reaction effluent, separation hydrogenation upgrading reaction effluent HPU3P obtains hydrogen-rich gas 2CHPV and upgrading generates oily HPU3P-0P, and the hydroconversion reaction zone HPU3 that at least a portion hydrogen-rich gas 2CHPV returns take the upgrading of lightweight carburetion as target recycles;
Separate upgrading and generate oily HPU3P-OP, obtain gas products and narrow fraction oil product.
While using the present invention to process the second flow scheme of full cut coal tar or the third flow scheme,
The hydrogenation upgrading that separates the hydroconversion reaction zone HPU3 generation take the upgrading of lightweight carburetion as target generates oily HPU3P-OP, the conventional boiling point obtaining is higher than the distillate of 350 ℃, can enter the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and contact with hydrogenation catalyst HPU1-CAT, or enter the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and contact with hydrocracking catalyst HPU21-CAT.
The second flow scheme or the third flow scheme that use the present invention to process full cut coal tar comprise while extracting phenol component process, it is characterized in that: in the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the carbolic oil that the hydrocarbon that is mainly 160～250 ℃ by conventional boiling point forms, carbolic oil is through becoming dephenolize oil containing after alkali aqueous solution extraction step, dephenolize oil enters treating tower, using conventional boiling point be 100～140 ℃ with the segregative hydrocarbon ils of water as interval hydrocarbon introduce treating tower, the low oily quantity for the treatment of tower tower is 5～20% of dephenolize oil, all the other dephenolize oil autofining tower lateral line withdrawal functions, main tower top oil gas be made up of interval hydrocarbon and water vapor leaves to be refined tower top and is separated into water and oil after cooling, the low oil for the treatment of tower tower removes coal tar fractional distillation tower, treating tower side line oil contacts with hydrogenation catalyst HPU3-CAT as the hydroconversion reaction zone HPU3 that after refining, dephenolize oil enters take the upgrading of lightweight carburetion as target as hydrogenating materials.
The present invention processes the second flow scheme of full cut coal tar or the preferred operations condition of the third flow scheme is: the hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～420 ℃, pressure are as 10.0～20.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are as 0.1～2.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 800: 1～2500: 1;
In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, temperature be 350～480 ℃, pressure be 10.0～20.0MPa, hydrogen/stock oil volume ratio be 800: 1～2500: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.03～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under operate; The weight rate SHSW of hydrogen supply hydrocarbon stream SH and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.3～3;
At the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target, be that 300～420 ℃, pressure are that 10.0～20.0MPa, hydrogen/stock oil volume ratio are that 800: 1～2500: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.15～2.0hr in temperature
-1reaction conditions under operate.
Embodiment
Below describe the present invention in detail.
Conventional boiling point of the present invention refers to vapour, the liquid equilibrium temperature of material under a barometric point.Conventional liq hydrocarbon of the present invention refers to the hydro carbons being in a liquid state under normal condition, comprises the hydro carbons that pentane and boiling point thereof are higher.Impurity composition of the present invention refers to the hydrogenation products of non-hydrogen, non-carbon in stock oil, comprises water, hydrogen sulfide, ammonia, hydrogenchloride etc.Proportion of the present invention, unless stated otherwise, refers to the ratio of fluid density and normal pressure under normal pressure, 15.6 ℃ of conditions, 15.6 ℃ of Water Under density.The composition of component of the present invention or concentration or content value, unless stated otherwise, be weight basis value, and weight percent is expressed as % by weight.
Coal tar of the present invention, normally comprise conventional boiling range and be 120～450 ℃ of hydrocarbon components and the conventional boiling point mixture higher than 450 ℃ of hydrocarbon components, conventionally comprise 40～60% conventional boiling range and be the cut (containing double ring arene cut) of 120～330 ℃, to comprise 20～35% conventional boiling range be the cut (containing dicyclo to Fourth Ring aromatic fraction) of 330～450 ℃ and 8～20% conventional boiling range higher than the last running (being coal-tar pitch cut) of 450 ℃.Coal tar of the present invention, refer to the coal-tar products from pyrolysis of coal or coal generating gas or other process, can be from the coalite tar of semi-coking process (pyrolysis temperature is lower than 700 ℃) or coal-tar middle oil (pyrolysis temperature is between 700～950 ℃) or their mixing oil of middle temperature process of coking, conventionally contain coal tar heavy duty oil ingredient.Due to raw coal character and coking or all variations within the specific limits of gas-making process condition, coal tar oil properties also changes within the specific limits.Coal tar oil properties proportion of the present invention is generally 0.89～1.15, and conventionally metal content is that 5～80PPm, sulphur content are 0.1～0.4%, nitrogen content is 0.6～1.6%.Coal tar of the present invention, inorganic water-content is 0.2～5.0% sometimes, sometimes organic oxygen level be 2.5～11%, be especially 3.5～10%, be more particularly 5～10%.According to the present invention, before described coal tar separates, conventionally passed through the process of filtering solid particulate.Coal tar of the present invention, contains phenolic compound conventionally, and before entering hydrogenation process, extraction phenolic compound is wherein such as rudimentary phenol conventionally.Coal tar lightweight fraction oil of the present invention, refers to the coal tar distillate oil that conventional boiling point is generally 60～480 ℃, is generally 60～450 ℃.Coal tar heavy oil of the present invention refers to the main cut being made up of higher than the hydrocarbon component of 450 ℃ conventional boiling point from coal tar, is rich in polycyclic aromatic hydrocarbons, colloid, bituminous matter.
Petroleum naphtha fraction of the present invention refers to the hydro carbons that conventional boiling point is generally 60～190 ℃, is generally 60～180 ℃.Fraction of diesel oil of the present invention refers to the hydro carbons that conventional boiling point is generally 160～390 ℃, is generally 180～370 ℃.
Table 1 Typical Aromatic component and contrast hydride boiling point, condensation point and density summary sheet
Hydrogen supply hydrocarbon SH of the present invention refers to the double ring arene of fractional saturation and the polycyclic aromatic hydrocarbons of fractional saturation.
Table 1 has been listed the part aromatic component and contrast hydride boiling point, condensation point and the density data that in coal tar, exist, for Typical Aromatic component and the variation that contrasts hydride boiling point, condensation point and density are described.
According to the present invention, the full cut of coal tar (specific components that needs separation and Extraction as phenol except) all needs through hydroconversion process, the listed boiling point data hint of table 1: with reference to the conventional boiling point of anthracene (340 ℃) and the conventional boiling point of naphthacene (450 ℃), take 350 ℃ and 450 ℃ as dividing point, about conventional boiling point is that the cut of 350～450 ℃ contains a large amount of three, the aromatic hydrocarbons of Fourth Ring structure, most the concentrating of aromatic hydrocarbons of five rings and more number of rings structures thereof is present in conventional boiling point higher than forming coal-tar pitch cut in the cut of 450 ℃, coal-tar pitch cut is difficult to adopt conventional bed technology to realize long period conventionally, therefore high yield hydrogenation lighting adopt floating bed hydrogenation technical transform it.Therefore following operating principle can be proposed: it is coal-tar pitch cut that conventional boiling point is defined as to coal tar heavy duty oil distillate higher than the cut of 450 ℃, conventional boiling point is defined as to the hydrogen donor precursor of association between the cut of 350～450 ℃, then use the present invention by hydrogen donor precursor hydrocracking for hydrogen supply hydrocarbon, then hydrogen supply hydrocarbon is imported to the hydrogenation lighting reaction process of coal-tar pitch cut, improve the hydrogenation lighting reaction process of coal-tar pitch cut, the novel hydrogenation that forms coal tar transforms combination process.
Conventional boiling point is defined as to the hydrogen donor precursor of association between the coal tar fraction of 350～450 ℃, determines based on following consideration: its hydrotreated product contains a large amount of hydrogen supply hydrocarbon, and cut is converted into the light-end products such as diesel oil must pass through hydrocracking process.
So far, the present invention proposes following " full cut coal tar hydrogenating transform " technological principle: in, the full cut conversion process of coalite tar, it is that the second cut and the conventional boiling point that the carbolic oil of 160～245 ℃, conventional boiling range are 350～450 ℃ lower than the first cut of 350 ℃ of hydrocarbon, conventional boiling range is coal-tar pitch higher than the 3rd cut of 450 ℃ that middle coalite tar is separated into conventional boiling range; From carbolic oil, extract lower boiling phenol, dephenolize oil and the first cut, as light ends, can become clear gusoline through deep hydrofinishing; The second cut that conventional boiling range is 350～450 ℃ of hydrocarbon components is as hydrogen donor precursor, use the present invention is converted into hydrogen supply hydrocarbon, then hydrogen supply hydrocarbon is imported to the hydrogenation lighting reaction process of coal-tar pitch cut, improve the hydrogenation lighting reaction process of coal-tar pitch cut, the hydrogenation lighting reaction of coal-tar pitch cut generate oil can enter the first cut unifining process and or the unifining process of the second cut complete upgrading, the novel hydrogenation that forms coal tar transforms combination process.
Conventional boiling range is the process that 350～450 ℃ of hydrocarbon components are prepared hydrogen supply hydrocarbon, can be Special hydrogenation process, be convenient to the processing that improves to greatest extent hydrogen supply hydrocarbon concentration under top condition, be conventionally applicable to fairly large full cut coal tar, can be also with conventional boiling range lower than the common Unionfining process using of the first cut of 350 ℃ of hydrocarbon, realize the object of simple flow, be conventionally applicable to the full cut coal tar processing of small-scale.
Producing with coal-tar pitch the process that the hydrogenation lighting reaction process of clean fuel oil is close has a lot, herein with the representation of concept of low hydrogen content hydrocarbon ils it, low hydrogen content hydrocarbon ils described herein possesses following characteristics: produce in the hydrogenation lighting reaction process of clean fuel oil at low hydrogen content hydrocarbon ils, the retention rate (improving light-end products productive rate) that the existence of hydrogen supply hydrocarbon has raising pyrolysis molecule reduces solid productive rate simultaneously, shorten the reaction process time, reduce reaction overall temperature rise, improve operational stability texts, therefore low hydrogen content hydrocarbon ils described herein refers to any one suitable low hydrogen content hydrocarbon ils, such as can be hydrogen richness lower than 9% the main logistics being formed higher than the hydrocarbon of 450 ℃ by conventional boiling point, can be selected from coalite tar cut, coal-tar middle oil cut, coal-tar heavy oil cut, petroleum residual oil, petroleum catalytic cracking slurry oil, oil catalytic cracking slurry oil, tar sand basic weight oil, one or more in shale oil.Conventionally,, along with the reduction of hydrogen richness, the aromaticity content in low hydrogen content hydrocarbon ils or gum level or asphalt content increase thereupon.
Scheme normally completes expected degree hydrogenation fractional saturation reaction to being rich in the hydro carbons of double ring arene and/or polycyclic aromatic hydrocarbons is prepared in the industry of hydrogen supply hydrocarbon makes the double ring arene that is converted into fractional saturation of its maximum or the polycyclic aromatic hydrocarbons of fractional saturation, and gained hydrogenation reaction effluent or its sepn process gained oil product can be used as hydrogen supply hydrocarbon stream.As the logistics that is rich in double ring arene and/or polycyclic aromatic hydrocarbons of hydrogen supply hydrocarbon precursor, can be selected from crude oil hot procedure fraction (such as the conventional boiling point of black petroleum products catalytic cracking process is 250～370 ℃ of fractions, the conventional boiling point of petroleum residual oil delayed coking process is 350～450 ℃ of fractions) in one or more, but (common conventional boiling point is 160～480 ℃ to be preferably selected from coal tar distillate, best conventional boiling point is 370～450 ℃), also can be selected from coal tar heavy fractioning hydrogenation converted product, one or more (now forming circulation process) in the sepn process gained distillate of coal tar heavy fractioning hydrogenation converted product.Such as, for middle coalite tar heavy oil (such as conventional boiling point is higher than the middle coalite tar pitch of 450 ℃) produce the hydrogenation lighting reaction process of clean fuel oil, it is industrial that to facilitate available hydrogen supply hydrocarbon predecessor hydrocarbon be exactly the coal tar distillate lower with the boiling point of coal-tar pitch association, now, one of scheme is that in separating, coalite tar obtains the lighting end being mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, the main the hydrocarbon middle cut forming and the last running mainly being formed higher than the hydrocarbon of 450 ℃ by conventional boiling point that are 350～450 ℃ by conventional boiling point, middle cut is as hydrogen supply hydrocarbon predecessor hydrocarbon, last running is as coal-tar pitch, two of scheme is that in separating, coalite tar obtains the front-end volatiles that are mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point and the last running being mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point, and front-end volatiles are as hydrogen supply hydrocarbon predecessor hydrocarbon, and last running is as coal-tar pitch.Because middle coalite tar contains a large amount of phenols, conventionally extract carbolic oil out at tar fractionation process, carbolic oil is separated into crude phenols and dephenolize oil, the further hydrotreatment of dephenolize oil.In the time need to processing the conventional boiling point of coal-tar heavy oil simultaneously and be 230～480 ℃ of cuts (and conventionally described washing oil and or carbolineum), can set it as hydrogen supply hydrocarbon predecessor hydrocarbon and use in the lump.
The major objective of producing the hydrogenation modification step of hydrogen supply hydrocarbon is to improve the content of " hydrogen supply hydrocarbon " in hydrogen supply hydrocarbon stream, such as improving the content of cycloalkyl benzene class, bicyclic alkyl benzene class component, contain a large amount of twin nuclei aromatic hydrocarbons, tricyclic structure aromatic hydrocarbons and Fourth Ring and above this fact of structure aromatic hydrocarbons thereof based on coal tar, coal tar hydrogenating modifying process is an incomplete saturation history of an aromatic hydrogenation aromatic hydrogenation appropriateness saturation history in other words conj.or perhaps.
About the hydrogenation modification process of producing hydrogen supply hydrocarbon, there is the Technology of the thick oily hydrogenation production coal liquefaction solvent oil of multiple gelatin liquefaction to use for reference, its reactor types can be fixed bed, ebullated bed, adverse current bed etc., catalyzer mostly is high reactivity carried catalyst.
Characteristic of the present invention is below described.
The hydrogenation lightening method of a kind of low hydrogen content heavy oil that uses hydrogen supply hydrocarbon of the present invention, comprises the steps:
Heavy oil streams HDS is mainly made up of higher than the hydrocarbon component HD of 450 ℃ conventional boiling point, and heavy oil streams HDS is selected from one or more in following material:
1. coalite tar heavy oil fraction;
2. coal-tar middle oil heavy oil fraction;
3. coal-tar heavy oil heavy oil fraction;
4. petroleum base heavy oil thermal course of processing gained heavy oil fraction product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;
5. shale oil basic weight oil hot procedure gained heavy oil fraction product;
6. tar sand basic weight oil hot procedure gained heavy oil fraction product;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, under hydrogen and catalyzer existence condition, the hydrogenation lighting reaction HPU21R that heavy oil streams HDS comprises hydrocracking reaction, at least a portion hydrocarbon component HD completes hydrocracking reaction and obtains reaction effluent HPU21P, it is characterized in that the hydrogen supply hydrocarbon stream SHS that contains hydrogen supply hydrocarbon SH enters hydroconversion reaction zone HPU21, in hydrogenation reaction HPU21R process, hydrogen supply hydrocarbon SH contacts with hydrocarbon component HD;
Described hydrogen supply hydrocarbon SH refer to fractional saturation double ring arene and or the polycyclic aromatic hydrocarbons of fractional saturation; In logistics SHS, gum level is lower than 10 % by weight, and asphalt content is lower than 1 % by weight; In logistics SHS, in hydrogen supply hydrocarbon SH weight and logistics SHS, the ratio of conventional liquid hydrocarbon component gross weight exceeds in heavy oil streams HDS the ratio at least 3% of conventional liquid hydrocarbon component gross weight in hydrogen supply hydrocarbon SH weight and heavy oil streams HDS; In logistics SHS, conventional liquid hydrocarbon component protium weight in average content exceeds the protium weight content at least 2% of heavy oil streams HDS;
Hydrogen supply hydrocarbon stream SHS is prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target from processing hydrogen supply hydrocarbon precursor logistics SHSBF's with hydrogen supply hydrocarbon; In logistics SHS, hydrogen supply hydrocarbon SH weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight; In the weight rate SHSW of hydrogen supply hydrocarbon stream SHS and heavy oil streams HDS, conventional boiling point is higher than the ratio K=SHSW/HDW of the weight rate HDW of the hydrocarbon component HD of 450 ℃, K=0.1～10.
It is middle coalite tar heavy oil and hydrogen supply hydrocarbon precursor logistics SHSBF is the processing of combining of middle coalite tar lighting end that the present invention is particularly suitable for heavy oil streams HDS, it is characterized in that: hydrogen richness is mainly made up of higher than the hydrocarbon component HD of 450 ℃ conventional boiling point lower than the heavy oil streams HDS of 8 % by weight; Heavy oil streams HDS is selected from one or both in following material:
1. coalite tar heavy oil fraction;
2. coal-tar middle oil heavy oil fraction;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor HPU21-SB, charging autoreactor HPU21-SB bottom enters, temperature be 300～500 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 500: 1～4000: 1, hydrogenation catalyst HPU21-CAT add weight be HDS weight 0.01～5.0%, volume space velocity is 0.1～10.0hr
-1reaction conditions under, complete the hydrogenation lighting reaction that comprises hydrocracking reaction and obtain hydrogenation lighting reaction effluent HPU21P, flow out on reaction effluent HPU21P autoreactor HPU21-SB top;
Hydrogen supply hydrocarbon stream SHS is prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target from processing hydrogen supply hydrocarbon precursor logistics SHSBF's with hydrogen supply hydrocarbon; In logistics SHS, hydrogen supply hydrocarbon SH weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight; In the weight rate SHSW of hydrogen supply hydrocarbon stream SHS and heavy oil streams HDS, conventional boiling point is higher than the ratio K=SHSW/HDW of the weight rate HDW of the hydrocarbon component HD of 450 ℃, K=0.2～5;
Hydrogen supply hydrocarbon precursor logistics SHSBF is selected from one or more in following logistics:
1. be mainly the logistics of the coalite tar fractions consisting of 350～450 ℃ by conventional boiling point;
2. be mainly the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ by conventional boiling point;
3. be mainly the logistics of the coal-tar heavy oil fractions consisting of 230～450 ℃ by conventional boiling point;
4. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coalite tar fractions consisting of 350～450 ℃ of cuts by comprising conventional boiling point;
5. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ of cuts by comprising conventional boiling point;
6. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coalite tar fractions consisting of 350～450 ℃ of cuts by the conventional boiling point after dephenolize;
7. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ of cuts by the conventional boiling point after dephenolize.
When hydrogen supply hydrocarbon precursor logistics SHSBF of the present invention is the middle coalite tar cut of 350～450 ℃, the selection of hydrogen supply hydrocarbon stream SHS is: at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS hydrogen supply hydrocarbon processed hydrogenation reaction HPU1R forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar, at least a portion hydrocarbon component MF completes hydrogenation modification reaction and obtains hydrogenation reaction effluent HPU1P, and the hydrogen supply hydrocarbon stream SHS obtaining based on hydrogenation reaction effluent HPU1P is selected from one or several of following logistics:
1. reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
2. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1-HSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
3. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1 mono-HSO is as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21, and the hot high score oil of at least a portion HPU1-HSO step-down, degassed rear gained liquid HPU1-HSOA enter hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
4. reaction effluent HPU1P enters cold anticyclone sepn process HPU1--CS and is separated into cold high score oil HPU1-CSO and cold high score gas HPU1-CSV, the cold high score oil of at least a portion HPU1-CSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
5. separating reaction effluent HPU1P obtains hydrogenated oil HPU1P0 and hydrogen-rich gas; In hydrogenated oil HPU1P0 fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
6. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion mainly by conventional boiling point be 350～450 ℃ be rich in logistics that hydrogen supply hydrocarbon component forms as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS.
When hydrogen supply hydrocarbon precursor logistics SHSBF of the present invention is the middle coalite tar cut of 60～450 ℃, the selection of hydrogen supply hydrocarbon stream SHS is: at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from containing of coal tar conventional boiling point be that the logistics LMFS of 60～450 ℃ of hydrocarbon LMF completes deep hydrofinishing reaction HPU1R and is converted into hydrogenation reaction effluent HPU1P, conventional boiling point is that the hydrocarbon of 60～350 ℃ is converted into petroleum naphtha and diesel component, conventional boiling point is that the hydrocarbon of 350～450 ℃ is converted into the hydrogenation tail oil that is rich in hydrogen supply hydrocarbon SH, the hydrogen supply hydrocarbon stream SHS obtaining based on hydrogenation reaction effluent HPU1P is selected from one or several of following logistics:
1. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1-HSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
2. the intermediate reaction effluent HPU1MP that is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon enters thermal high sepn process HPU1M-HS and is separated into hot high score oil HPU1M-HSO and hot high score gas HPU1MP-HSV, the hot high score oil of at least a portion HPU1M-HSO is as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21, after the degassed rear gained degas oil HPU1M-HSOA of the hot high score oil HPU1M-HSO step-down of at least a portion mixes with heavy oil streams HDS, enters hydroconversion reaction zone HPU21;
3. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
4. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion mainly by conventional boiling point be 350～450 ℃ be rich in logistics that hydrogen supply hydrocarbon component forms as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS.
When hydrogen supply hydrocarbon precursor logistics SHSBF of the present invention is the middle coalite tar cut of 60～450 ℃, at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from coal tar be mainly that the hydrogenation modification that logistics LMFS that 60～450 ℃ of hydrocarbon LMF forms carries out reacts HPU1R by conventional boiling point, can select to produce to greatest extent hydrogen supply hydrocarbon is target.
Heavy oil streams HDS of the present invention mainly by conventional boiling point higher than 450 ℃ hydrogen richness while forming lower than the coal tar heavy fractioning HD of 6.5 % by weight, turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight, temperature be 320～480 ℃, pressure be 10.0～20.0MPa, hydrogen/stock oil volume ratio be 1000: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.1～2.0%, volume space velocity is 0.2～5.0hr
-1reaction conditions under operate; In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.3～3.
When the hydroconversion reaction zone HPU3 of setting of the present invention take the upgrading of lightweight carburetion as target, the first mode of operation is:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst PU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
When the hydroconversion reaction zone HPU3 of setting of the present invention take the upgrading of lightweight carburetion as target, the second mode of operation is:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21P0 and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21P0 and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
When the hydroconversion reaction zone HPU3 of setting of the present invention take the upgrading of lightweight carburetion as target, the third mode of operation is:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that the hydrocarbon that at least a portion is mainly 350～450 ℃ by conventional boiling point forms removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target; The logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
When the present invention arranges hydrogenation upgrading cascade reaction district HPU22, be characterised in that:
The hydrogenation reaction effluent HPU21P that turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight enters the hot high score fluid body HPU21P-HSL that hot high-pressure separator HPU21P-HS is separated into hot high score gas HPU21P-HSV and contains solid particulate, and hot high-pressure separator HPU21P-HS is to operate under 350～500 ℃, the pressure condition that is 6.0～28.0MPa in temperature; The main oil product being made up of higher than the hydrocarbon of 450 ℃ conventional boiling point that heat of dissociation high score fluid body HPU21P-HSL obtains enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and contacts with catalyzer HPU21-CAT;
Hot high score gas HPU21P-HSV enters hydrogenation upgrading cascade reaction district HPU22, the main liquid hydrocarbon being made up of lower than the hydrocarbon of 450 ℃ conventional boiling point that heat of dissociation high score oil HPU21P-HSL obtains enters hydrogenation upgrading cascade reaction district HPU22, the main logistics LFS being made up of lower than the hydrocarbon LF of 350C conventional boiling point from coal tar existing enters hydrogenation upgrading cascade reaction district HPU22, hydrogenation upgrading cascade reaction district HPU22 operational condition is: temperature is 280～440 ℃, pressure is 6.0～28.0MPa, hydrogen/stock oil volume ratio is 300: 1～3000: 1, hydrogenation catalyst HPU22-CAT volume space velocity is 0.05～5.0hr
-1, complete hydrogenation upgrading cascade reaction and obtain hydrogenation upgrading cascade reaction effluent HPU22P,
At the separate part HPU22P-S of hydrogenation upgrading cascade reaction effluent HPU22P, separate hydrogenation upgrading cascade reaction effluent HPU22P and obtain hydrogen-rich gas HPU22PH and hydrogenated oil HPU22PO, at least a portion hydrogen-rich gas HPU22PH returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
At hydrogenated oil HPU22PO separate part HPU22PO-FS, separate hydrogenated oil HPU22PO and obtain gas and narrow fraction oil product.
When the present invention arranges hydrogenation upgrading cascade reaction district HPU22, at hydrogenated oil HPU22PO separate part HPU22PO-FS, separate the main oil product being formed higher than the hydrocarbon of 350 ℃ by conventional boiling point that hydrogenated oil HPU22PO obtains, enter the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and catalyzer HPU21-CAT and contact or enter the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and contact with catalyzer HPU1-CAT.
The hydrogenation upgrading cascade reaction district HPU22 that the present invention arranges should use ebullated bed reactor or suspended-bed reactor, with the raw material that adapts to contain tiny solid particle.
For simple flow, the hydroconversion reaction zone HPU1 that the present invention can be prepared as target with hydrogen supply hydrocarbon by heavy oil lighting generation oil introducing separation completes upgrading object, and its first flow process is:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1P0 and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separation hydrogenated oil HPU1PO obtains being rich in the logistics of hydrogen supply hydrocarbon component, and what at least a portion was mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target.
For simple flow, the hydroconversion reaction zone HPU1 that the present invention can be prepared as target with hydrogen supply hydrocarbon by heavy oil lighting generation oil introducing separation completes upgrading object, and its second flow process is:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separation hydrogenated oil HPU1PO obtains being rich in the logistics of hydrogen supply hydrocarbon component, and what at least a portion was mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21P0 and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target.
When hydrogen supply hydrocarbon precursor logistics SHSBF is the middle coalite tar cut of 350～450 ℃, for simple flow, the first flow process of the present invention is:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P, and at least a portion reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics HPU3-F1 that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
When hydrogen supply hydrocarbon precursor logistics SHSBF is the middle coalite tar cut of 350～450 ℃, for simple flow, the second flow process of the present invention is:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from coal tar be mainly that logistics MFS that 350～450 ℃ of hydrocarbon MF forms completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P by conventional boiling point, at least a portion reaction effluent HPU1P is used as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that the hydrocarbon that at least a portion is mainly 350～450 ℃ by conventional boiling point forms removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target; The logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
When hydrogen supply hydrocarbon precursor logistics SHSBF is the middle coalite tar cut of 350～450 ℃, for simple flow, the third flow process of the present invention is:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P, and at least a portion reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21P0 and hydrogen-rich gas; In hydrogenated oil HPU21P0 fractionation part, separate hydrogenated oil HPU21P0 and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
The present invention arranges hydrocracking reaction process HPU4 and processes while being prepared as the separating obtained oil product HPU1PO-DO being made up of higher than 350 ℃ of hydrocarbon conventional boiling point of hydrogenated oil HPU1PO of hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon, for simple flow, the present invention is characterised in that:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate hydrogenated oil HPU1PO and obtain gas, narrow fraction oil product, the logistics that is rich in hydrogen supply hydrocarbon component that part is mainly made up of higher than 350 ℃ of hydrocarbon conventional boiling point is as hydrogen supply hydrocarbon stream SHS; The oil product HPU1PO-DO that part is mainly made up of higher than 350 ℃ of hydrocarbon conventional boiling point goes hydrocracking reaction process HPU4 to be converted into hydrocracking reaction effluent HPU4P, and hydrocracking reaction effluent HPU4P mixes with one or several in following logistics:
1. be prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon;
2. the hydrogenation upgrading cascade reaction effluent HPU22P existing;
3. the hydrogenation reaction effluent HPU3P of the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target existing.
In the middle of existing, the hydroconversion reaction zone HPU21 that the present invention turns to target with heavy oil lightweight when turning oil system, it is characterized in that:
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, the main heavy oil streams HDS being made up of higher than the coal tar heavy fractioning HD of 450 ℃ conventional boiling point enters the first reaction zone HPU211, temperature be 300～500 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 500: 1～4000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.05～5%, volume space velocity is 0.2～5.0hr
-1reaction conditions under, complete shallow degree hydrocracking reaction and obtain intermediate reaction effluent HPU211P; The intermediate reaction effluent HPU211P1 of first part is separated into intermediate gas and middle hydrocarbon ils, and middle hydrocarbon ils returns to the first reaction zone HPU211 as middle circulation hydrocarbon ils and contacts with hydrogenation catalyst HPU211-CAT; The second reaction zone HPU212 that second section intermediate reaction effluent HPU211P2 and intermediate gas enter hydroconversion reaction zone HPU21 carries out overhydrocracking reaction and obtains hydrogenation reaction effluent HPU212P, and reaction effluent HPU212P is as the hydrogenation reaction effluent HPU21P that turns to the hydroconversion reaction zone of target with heavy oil lightweight; The ratio K=HPU211P1W/HPU211P2W of the weight rate HPU211P1W of the intermediate reaction effluent HPU211P1 of first part and the weight rate HPU211P2W of second section intermediate reaction effluent HPU211P2, conventionally K=0.5～2.
When the present invention exists two-way hydrogen supply hydrocarbon stream, the first flow scheme is:
There is two-way hydrogen supply hydrocarbon precursor material: lightweight hydrogen supply hydrocarbon precursor SHB1 and heavy hydrogen supply hydrocarbon precursor SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 obtains hydrogenation reaction effluent HPU11P through aromatic hydrogenation fractional saturation process HPU11, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, hydrogenation reaction effluent HPU11P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 obtains hydrogenation reaction effluent HPU12P through aromatic hydrogenation fractional saturation process HPU12, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, hydrogenation reaction effluent HPU12P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD.
When the present invention exists two-way hydrogen supply hydrocarbon stream, the second flow scheme is:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 is the distillate HPU11PSP of 60～350 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU11 gained hydrogenation reaction effluent HPU11P, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1; Distillate HPU11PSP enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 is the distillate HPU12PSP of 350～450 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU12 gained hydrogenation reaction effluent HPU12P, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1; Distillate HPU12PSP enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD.
When the present invention exists two-way hydrogen supply hydrocarbon stream, the third flow scheme is:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 obtains hydrogenation reaction effluent HPU11P through aromatic hydrogenation fractional saturation process HPU11, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 obtains hydrogenation reaction effluent HPU12P through aromatic hydrogenation fractional saturation process HPU12, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～20.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
There is the first reaction zone HPU211 and the second reaction zone HPU212 of serial operation in the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, coal tar heavy oil HDS enters the first reaction zone HPU211, SHB1 transforms the reaction effluent HPU11P obtaining and enters the first reaction zone HPU211 hydrogen supply hydrocarbon is contacted with coal-tar hydrocarbon component HD or its intermediate product, obtains the first reaction zone HPU211 reaction effluent HPU211P; Reaction effluent HPU211P enters the second hydroconversion reaction zone HPU212, SHB2 transforms the reaction effluent HPU12P obtaining and enters the second hydroconversion reaction zone HPU212 hydrogen supply hydrocarbon is contacted with the intermediate product of coal-tar hydrocarbon component HD, and second reaction zone HPU212 service temperature is compared with at least 10 ℃ of the first reaction zone HPU211 service temperature height.
When the present invention exists two-way hydrogen supply hydrocarbon stream, the 4th kind of flow scheme is:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, the distillate HPU11PSP that SHB1 is 60～350C through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU11 gained hydrogenation reaction effluent HPU11P, aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 is the distillate HPU12PSP of 350～450 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU12 gained hydrogenation reaction effluent HPU12P, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
There is the first reaction zone HPU211 and the second reaction zone HPU212 of serial operation in the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, coal-tar hydrocarbon component HD enters the first reaction zone HPU211, SHB1 transforms the distillate HPU11PSP obtaining and enters the first reaction zone HPU211 hydrogen supply hydrocarbon is contacted with coal-tar hydrocarbon component HD or its intermediate product, obtains the first reaction zone HPU211 reaction effluent HPU211P; Reaction effluent HPU211P enters the second hydroconversion reaction zone HPU212, SHB2 transforms the distillate HPU12PSP obtaining and enters the second hydroconversion reaction zone HPU212 hydrogen supply hydrocarbon is contacted with the intermediate product of coal-tar hydrocarbon component HD, and second reaction zone HPU212 service temperature is compared with at least 15 ℃ of the first reaction zone HPU211 service temperature height.
The first flow scheme that the present invention processes full cut coal tar is:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the lighting end LMFS being mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point and the last running HS being mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point, last running HS is as heavy oil streams HDS, and lighting end LMFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB completes deep hydrofinishing reactive moieties at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and obtains hydrogenation reaction effluent HPUlP, the hydroconversion reaction zone HPUl that is prepared as target take hydrogen supply hydrocarbon in temperature as 200～440 ℃, pressure are as 6.0～28.0MPa, HPU21-CAT volume space velocity are as 0.05～10.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, in hydrogenation reaction effluent HPUlP, full cut diesel-fuel cetane number is higher than 24;
Separate the distillate HPU1P-FHO that hydrogenation reaction effluent HPUlP obtains gas, the main distillate HPU1P-FLO being made up of lower than the hydrocarbon of 350 ℃ conventional boiling point and is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point, at least a portion distillate HPUlP-FHO enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight after mixing with heavy oil streams HDS as logistics SHS, and in logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, temperature be 350～500 ℃, pressure be 3.0～28.0MPa, hydrogen/stock oil volume ratio be 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under, carry out hydrogenation lighting reaction and obtain hydrogenation lighting reaction effluent HPU21P; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDw of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.2～5; Hydrogenation lighting reaction effluent HPU21P enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21 mono-HPV and contains solid particulate, hot high score gas HPU2-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU2-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to hydroconversion reaction zone HPU21 and recycles;
The hot high score fluid of fractionation body HPU21-HPL and or cold high score fluid body HPU2-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight; Outer oil extraction WPY penetration depth hydrofining reaction part HPUl contacts with its Hydrobon catalyst, and outer oil extraction WPY completes hydrogenation upgrading reaction, and the hydrogenation upgrading reaction effluent obtaining enters in hydrogenation reaction effluent HPUlP.
The first flow scheme that the present invention processes full cut coal tar comprises while extracting phenol component process, it is characterized in that:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the carbolic oil that the hydrocarbon that is mainly 160～250 ℃ by conventional boiling point forms, carbolic oil is through becoming dephenolize oil containing after alkali aqueous solution extraction step, dephenolize oil enters treating tower, using conventional boiling point be 100～140 ℃ with the segregative hydrocarbon ils of water as interval hydrocarbon introduce treating tower, the low oily quantity for the treatment of tower tower is 5～20% of dephenolize oil, all the other dephenolizes oil autofining tower lateral line withdrawal functions, the tower top oil gas mainly be made up of interval hydrocarbon and water vapor leaves to be refined tower top and is separated into water and oil after cooling; The low oil for the treatment of tower tower removes coal tar fractional distillation tower; Treating tower side line oil enters hydrogenation reaction part HPUl as dephenolize oil after refining as hydrogenating materials and contacts with its hydrogenation catalyst.
The preferred operational condition of the first flow scheme that the present invention processes full cut coal tar is:
The hydroconversion reaction zone HPUl that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～420 ℃, pressure are as 10.0～25.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are as 0.1～2.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 800: 1～2500: 1, in hydrogenation reaction effluent HPU1P, full cut diesel-fuel cetane number is higher than 28;
In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight;
Turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight, temperature be 350～480 ℃, pressure be 10.0～25.0MPa, hydrogen/stock oil volume ratio be 800: 1～2500: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under operate, in the whole hydrocarbon feeds of hydroconversion reaction zone HPU21, conventional boiling point is greater than 40 % by weight higher than the cracking rate of the hydrocarbon component of 450 ℃.
When the present invention processes the first flow scheme of full cut coal tar, the weight rate SHW of hydrogen supply hydrocarbon SH and the ratio K=SHW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, conventionally K=0.3～3.
The second flow scheme that the present invention processes full cut coal tar is:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, the first cut LFS that in separation, coalite tar obtains mainly be made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, the second cut MFS and the main last running HS being formed higher than the hydrocarbon of 450 ℃ by conventional boiling point that mainly the hydrocarbon that is 350～450 ℃ by conventional boiling point forms, last running HS is as heavy oil streams HDS, and the second cut MFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB is converted into hydrogenation reaction effluent HPU1P at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, and hydroconversion reaction zone HPU1 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
At least a portion hydrogenation reaction effluent HPU1P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight as logistics SHS after mixing with heavy oil streams HDS, and in logistics SHS, hydrogen supply hydrocarbon SH weight accounts in logistics SHS conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
The hydroconversion reaction zone HPU21 that turns to target take heavy oil lightweight in temperature as 350～500 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio add as 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT weight as HD weight 0.01～2%, volume space velocity is as 0.1～10.0hr
-1reaction conditions under complete hydrogenation lighting reaction and obtain hydrogenation reaction effluent HPU21P; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.1～10; At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor, charging autoreactor bottom enters, and flow out on hydrogenation lighting reaction effluent HPU21P autoreactor top;
Reaction effluent HPU21P enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21-HPV and contains solid particulate, hot high score gas HPU21-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU21-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
The hot high score fluid of fractionation body HPU21-HPL and or cold high score fluid body HPU21-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight;
The hydroconversion reaction zone HPU3 of oil extraction WPY hydrogenation upgrading reaction zone take the upgrading of lightweight carburetion as target is outside that 260～440 ℃, pressure are that 6.0～28.0MPa, hydrogen/stock oil volume ratio are that 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.05～5.0hr in temperature
-1reaction conditions under, outer oil extraction WPY and the first cut LFS that combines processing complete the reaction of hydrogenation upgrading system, obtain hydrogenation upgrading reaction effluent HPU3P;
At the separate part HPU3P-HS of hydrogenation upgrading reaction effluent, separation hydrogenation upgrading reaction effluent HPU3P obtains hydrogen-rich gas HPU3P-HSV and upgrading generates oily HPU3P-0P, and the hydroconversion reaction zone HPU3 that at least a portion hydrogen-rich gas HPU3P-HSV returns take the upgrading of lightweight carburetion as target recycles;
Separate upgrading and generate oily HPU3P-0P, obtain gas products and narrow fraction oil product.
The third flow scheme that the present invention processes full cut coal tar is:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the lighting end LMFS being mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point and the last running HS being mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point, last running HS is as heavy oil streams HDS, and lighting end LMFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB is converted into hydrogenation reaction effluent HPU1P through the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, and hydroconversion reaction zone HPU1 is that 200～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
At least a portion hydrogenation reaction effluent HPU1P enters hydroconversion reaction zone HPU21 as logistics SHS after mixing with heavy oil streams HDS, in logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
Hydroconversion reaction zone HPU21 temperature be 300～550 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under, carry out hydrogenation lighting reaction and obtain hydrogenation lighting reaction effluent HPU21P; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.1～10; At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor, charging autoreactor bottom enters, and flow out on hydrogenation lighting reaction effluent HPU21P autoreactor top;
The reaction effluent HPU21P that turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21-HPV and contains solid particulate, hot high score gas HPU21-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU21-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
The hot high score fluid of fractionation body HPU21-HPL and or cold high score fluid body HPU21-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight;
Outer oil extraction WPY hydrogenation upgrading reaction zone HPU3 is that 260～440 ℃, pressure are that 6.0～28.0MPa, hydrogen/stock oil volume ratio are that 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.05～5.0hr in temperature
-1reaction conditions under, outer oil extraction WPY completes hydrogenation upgrading system reaction, obtains hydrogenation upgrading reaction effluent HPU3P;
At the separate part HPU3P-HS of hydrogenation upgrading reaction effluent, separation hydrogenation upgrading reaction effluent HPU3P obtains hydrogen-rich gas 2CHPV and upgrading generates oily HPU3P-0P, and the hydroconversion reaction zone HPU3 that at least a portion hydrogen-rich gas 2CHPV returns take the upgrading of lightweight carburetion as target recycles;
Separate upgrading and generate oily HPU3P-0P, obtain gas products and narrow fraction oil product.
While using the present invention to process the second flow scheme of full cut coal tar or the third flow scheme,
The hydrogenation upgrading that separates the hydroconversion reaction zone HPU3 generation take the upgrading of lightweight carburetion as target generates oily HPU3P-0P, the conventional boiling point obtaining is higher than the distillate of 350 ℃, can enter the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and contact with hydrogenation catalyst HPU1-CAT, or enter the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and contact with hydrocracking catalyst HPU21-CAT.
The second flow scheme or the third flow scheme that use the present invention to process full cut coal tar comprise while extracting phenol component process, it is characterized in that: in the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the carbolic oil that the hydrocarbon that is mainly 160～250 ℃ by conventional boiling point forms, carbolic oil is through becoming dephenolize oil containing after alkali aqueous solution extraction step, dephenolize oil enters treating tower, using conventional boiling point be 100～140 ℃ with the segregative hydrocarbon ils of water as interval hydrocarbon introduce treating tower, the low oily quantity for the treatment of tower tower is 5～20% of dephenolize oil, all the other dephenolize oil autofining tower lateral line withdrawal functions, main tower top oil gas be made up of interval hydrocarbon and water vapor leaves to be refined tower top and is separated into water and oil after cooling, the low oil for the treatment of tower tower removes coal tar fractional distillation tower, treating tower side line oil contacts with hydrogenation catalyst HPU3-CAT as the hydroconversion reaction zone HPU3 that after refining, dephenolize oil enters take the upgrading of lightweight carburetion as target as hydrogenating materials.
The present invention processes the second flow scheme of full cut coal tar or the preferred operations condition of the third flow scheme is: the hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～420 ℃, pressure are as 10.0～20.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are as 0.1～2.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 800: 1～2500: 1;
In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, temperature be 350～480 ℃, pressure be 10.0～20.0MPa, hydrogen/stock oil volume ratio be 800: 1～2500: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.03～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under operate; The weight rate SHSW of hydrogen supply hydrocarbon stream SH and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.3～3;
At the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target, be that 300～420 ℃, pressure are that 10.0～20.0MPa, hydrogen/stock oil volume ratio are that 800: 1～2500: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.15～2.0hr in temperature
-1reaction conditions under operate.
Below describe each step of the present invention in detail.
Describe the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight of the present invention in detail below in conjunction with coalite tar.
The main logistics HDS being made up of higher than the coalite tar last running HD of 450 ℃ conventional boiling point enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, carry out heavy oil lighting hydrogenation reaction and obtain hydrogenation reaction effluent HPU21P, it is characterized in that the logistics SHS that contains hydrogen supply hydrocarbon SH enters hydroconversion reaction zone HPU21 hydrogen supply hydrocarbon SH is contacted with coal tar heavy fractioning HD.
The logistics SHS that contains hydrogen supply hydrocarbon SH enters hydroconversion reaction zone HPU21 makes hydrogen supply hydrocarbon SH unrestricted with the mode that coal tar heavy fractioning HD contacts, for the two is fully mixed, the logistics SHS that contains hydrogen supply hydrocarbon SH conventionally completes with coal tar heavy fractioning HD and contact (mixing) and enter afterwards hydroconversion reaction zone HPU21, can be employing one or more modes below:
1. first kind of way, the hydrogenation reaction effluent that comprises hydrogen supply hydrocarbon directly completes and contacts (as abundant mixing) and enter afterwards hydroconversion reaction zone HPU21 with coal-tar pitch logistics HDS;
2. the second way, the hydrogenation reaction effluent that comprises hydrogen supply hydrocarbon is separated into gas G and liquid L under condition of high voltage, liquid L completes and contact (as abundant mixing or after mixing stop certain hour) and enters afterwards hydroconversion reaction zone HPU21 with the coal-tar pitch logistics HDS after pressurization, gas G also enters hydroconversion reaction zone HPU21;
3. the third mode, the hydrogenation reaction effluent that comprises hydrogen supply hydrocarbon completes to contact with the coal-tar pitch logistics HDS after pressurization and forms mixture, then under condition of high voltage, mixture separation is gas G and liquid L, liquid L enters hydroconversion reaction zone HPU21 after stopping certain hour, and gas G also enters hydroconversion reaction zone HPU21;
4. the 4th kind of mode, the hydrogenation reaction effluent that comprises hydrogen supply hydrocarbon is separated into gas G and liquid L under condition of high voltage, liquid L step-down, degassed rear gained liquid LA and coal-tar pitch logistics HDS complete and contact (as abundant mixing) and enter hydroconversion reaction zone HPU21 through pressurization afterwards, and gas G also enters hydroconversion reaction zone HPU21;
5. the 5th kind of mode, separates the hydrogenation reaction effluent that comprises hydrogen supply hydrocarbon and obtains the narrow fraction oil product that comprises hydrogen supply hydrocarbon, and narrow fraction oil product and coal-tar pitch logistics HDS complete and contact (as abundant mixing) and pass through afterwards to pressurize and enter hydroconversion reaction zone HPU21.
Hydroconversion reaction zone HPU21, the reactor assembly technology of its use can be one or more in suspended-bed reactor (comprising pump circulation suspended-bed reactor) systems technology, ebullated bed reactor systems technology, adverse current bed reactor system technology, number of reactors can be one or several, and number of reactors is generally 1～3.
The present invention recommends reactor assembly utilization suspended-bed reactor (the comprising pump circulation suspended-bed reactor) systems technology of hydroconversion reaction zone HPU21, number of reactors is generally 1～2, contains a large amount of bituminous matters, colloid and a certain amount of ash feature of grading to adapt to coalite tar pitch.
The present invention recommends reactor assembly utilization suspended-bed reactor (the comprising pump circulation suspended-bed reactor) systems technology of hydroconversion reaction zone HPU21, the hydrogenation catalyst that hydroconversion reaction zone HPU2 uses can be any suitable catalyzer and related system technology thereof, such as being the method that patent application 201010217358.1 is recorded, comprise catalyzer, operational condition, operation scheme, certainly concrete numerical value needs in conjunction with test or the corresponding adjustment of the condition of production.
Described hydrogenation modification reactive moieties HPU21, the hydrogenation catalyst HPU21-CAT of use can be the combination of one or two or more hydrogenation catalyst.
The coal-tar pitch hydrogenation lighting reaction that hydroconversion reaction zone HPU21 of the present invention occurs, refer at hydrogen, the lighting reaction process of the consumption hydrogen that under suitable hydrogenation catalyst HPU21-CAT and hydrogen supply hydrocarbon existence condition, coal-tar pitch occurs, its minimum reaction depth should possess MIN industrial significance: the cracking reaction and the hydrogenation reaction that coal-tar pitch HDS are completed expection, this hydrogenation reaction degree of depth should be determined according to the cracking degree of hydrocarbon component structure and expection in coal-tar pitch HDS, the cracking rate X of coal-tar pitch is less than with the conventional boiling point generating the hydrocarbon weight ratio that conventional boiling point in the hydrocarbon weight of 450 ℃ and coal-tar pitch HDS is greater than 450 ℃ and represents, X is generally 0.25～0.95, be generally 0.55～0.85, when transformation efficiency is too high, can increase gas yield.
Described hydroconversion reaction zone HPU21, because of the difference of the difference of feedstock property (metal content, carbon residue content, sulphur content, nitrogen content, aromaticity content, boiling range, proportion) and hydrogenation reaction (hydrogenating desulfurization, hydrodenitrification, hydrogenation are saturated, the hydrocracking etc.) degree of depth, the variation range of its operational condition is very wide, should determine according to concrete process condition.
Any supplementary sulphur can be added to hydroconversion reaction zone HPU21 as required, to guarantee that the necessary minimum concentration of hydrogen sulfide of reaction process is such as 500PPm (v) or 1000PPm (v), to guarantee that the necessary hydrogen sulfide sectional pressure of catalyzer is not less than minimum must value.Described supplementary sulphur can be the material without undesirable action to hydroconversion process that sulfide hydrogen maybe can be converted into hydrogen sulfide, such as hydrogen sulfide containing gas or oil product, or contacts rear dithiocarbonic anhydride or the Methyl disulfide etc. that generates hydrogen sulfide with high-temperature hydrogen.In the time that hydrogen supply hydrocarbon provides with hydrogenation reaction effluent form, if hydrogen sulfide quantity wherein meets the needs of hydroconversion reaction zone HPU2, can not re-use sulfur supplementary agent.
Below describe the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon in detail.
According to the present invention, the logistics SHS that contains hydrogen supply hydrocarbon SH is the logistics that transforms gained hydrogenation reaction effluent HPU1P from the hydrogen supply hydrocarbon precursor logistics SHSBF that is rich in double ring arene and/or polycyclic aromatic hydrocarbons at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon; The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon conventionally in temperature as 280～440 ℃, pressure are as 6.0～20.0MPa, hydrogenation catalyst HPU1-CAT volume space velocity are as 0.05～10.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1.
The aromatic hydrogenation fractional saturation reaction that is prepared as the hydroconversion reaction zone HPU1 generation of target with hydrogen supply hydrocarbon of the present invention, refer to the reaction process that is rich in the consumption hydrogen that the hydrocarbon material SHSBF of double ring arene and/or polycyclic aromatic hydrocarbons occurs under hydrogen and suitable hydrogenation catalyst HPU1-CAT (aromatic hydrogenation fractional saturation catalyzer) existence condition, its minimum reaction depth should possess MIN industrial significance: the aromatic hydrogenation fractional saturation that completes expection to being rich in the hydrocarbon material SHSBF of double ring arene and/or polycyclic aromatic hydrocarbons, this hydrogenation reaction degree of depth should be determined according to the aromatic hydrocarbons fractional saturation degree of aromatic component structure and expection in SHSBF, conventional boiling point in hydrogenation reaction effluent HPU1P be in the hydrocarbon-fraction of 350～480 ℃ hydrogen supply hydrocarbon weight concentration value SHN expect more high better, SHN is greater than 6 % by weight conventionally, generally be greater than 10 % by weight.
The described hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, because of the difference of feedstock property (metal content, oxygen level content, olefin(e) centent, sulphur content, nitrogen content, aromaticity content, boiling range, proportion) and the difference of hydrogenation reaction (hydrogenation deoxidation, hydrogenating desulfurization, hydrodenitrification, the hydrogenation fractional saturation) degree of depth, the variation range of its operational condition is very wide, should determine according to concrete process condition.
The described hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the hydrogenation catalyst HPU1-CAT using can be the series combination of one or two or more Hydrobon catalyst and load in mixture, can be the special-purpose catalyst for concrete raw material, can be also Hydrobon catalyst and the combination thereof with functions such as hydrodemetallation (HDM) or hydrogenation deoxidation or hydrogenating desulfurization or hydrodenitrification or hydrogenation are saturated that the unifining process of suitable refining of petroleum heavy gas oil type or wax oil type uses.The aromatic hydrogenation fractional saturation of the thick oily production coal liquefaction solvent oil of gelatin liquefaction catalyzer for reaction process, coal tar lighting end deep hydrofinishing catalyzer are normally operable.
The described hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon; the hydrogenation catalyst HPU1-CAT using; at least comprise hydrocatalyst for saturating arylhydrocarbon, conventionally also comprise Hydrodemetalation catalyst (flow process position be positioned at hydrocatalyst for saturating arylhydrocarbon bed before).
Any supplementary sulphur can be added as required to the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, to guarantee that the necessary minimum concentration of hydrogen sulfide of reactive moieties is such as 500PPm (v) or 1000PPm (v), to guarantee that the necessary hydrogen sulfide sectional pressure of catalyzer is not less than minimum must value.Described supplementary sulphur can be the material without undesirable action to hydroconversion process that sulfide hydrogen maybe can be converted into hydrogen sulfide, such as hydrogen sulfide containing gas or oil product, or contacts rear dithiocarbonic anhydride or the Methyl disulfide etc. that generates hydrogen sulfide with high-temperature hydrogen.
When the present invention is applied to the coal-tar pitch hydrogenation lighting process of coalite tar, its major advantage is:
1. can shorten the reaction process time, improve catalyst efficiency;
The retention rate that 2. can improve pyrolysis molecule reduces solid productive rate simultaneously, improves light-end products productive rate, saves solid-liquid separation power consumption;
3. can reduce reaction overall temperature rise;
4. can improve operational stability, prolong operation cycle;
5. the present invention is suitable for new device or existing plant modification;
6. be suitable for large-scale processing device.
Turn to conventional boiling point in the hydrogenation reaction product HPU21P of hydroconversion reaction zone HPU21 of target with heavy oil lightweight and conventionally enter the hydroconversion reaction zone HPU21 that turns to target with the heavy oil lightweight cracking that circulates higher than the distillate of 450 ℃ or 480 ℃.
Turn to benzoline that conventional boiling point in the hydrogenation reaction product HPU21P of hydroconversion reaction zone HPU21 of target is less than 450 ℃ or 480 ℃ conventionally enters hydrogenation upgrading process (HPU3 or HPU1 or HPU22) and produces the products such as gas, liquefied gas, petroleum naphtha, diesel component with heavy oil lightweight.
Below describe the rule of the high pressure separation process of hydrogenation reaction effluent of the present invention in detail.
The high pressure separation process of hydrogenation reaction effluent all comprises cold high pressure separator, when hydrocarbon ils density in hydrogenation reaction effluent large (such as approaching with water-mass density) or viscosity large or be difficult to separate or contain solid particulate with emulsifying water (such as parrot coal body is better in comparatively high temps current downflow, poor fluidity at a lower temperature) time, also need setting operation temperature to be generally the high pressure hot separator of 150～450 ℃, now hydrogenation reaction effluent enters high pressure hot separator and be separated into the hot high score gas gas (may contain solid particulate) being mainly made up of hydrogen and a main hot high score fluid body being made up of conventional liq hydrocarbon and the solid that may exist on volume, hot high score gas enters the cold high pressure separator that service temperature is generally 20～80 ℃ and is separated into cold high score oil and cold high score gas, because a large amount of high boiling components enter in hot high score fluid body, realize following target: cold high score oil density diminishes or viscosity diminishes or be easy to separate with water or parrot coal body has better mobility and is easy to discharge system.The high pressure separation process of hydrogenation reaction effluent arranges high pressure hot separator, also possesses the advantage that reduces calorific loss, because hot high score fluid body can be avoided the use air cooler of hot high score gas experience or the process that cools of water cooler.The hydrogenation process that hot part high score fluid body can be returned to upstream recycles, to improve the total raw material character of hydrogenation process that receives this turning oil, or to this turning oil hydrogenation that circulates.
Before hydrogenation reaction effluent or hot high score gas enter cold anticyclone separate part, conventionally first reduce temperature (being generally and reactive moieties charging heat exchange) to approximately 220～100 ℃ (these temperature should higher than sulphur hydrogenation ammonia Tc in this hydrogenation reaction effluent gas phase), then conventionally inject wherein washing water and form water filling back end hydrogenation reaction effluent, washing water for absorbing ammonia and issuable other impurity as hydrogenchloride etc., and the inevitable absorbing hydrogen sulphide of the aqueous solution after absorbing ammonia.At cold anticyclone separate part, described water filling back end hydrogenation reaction effluent is separated into: the cold high score gas being mainly made up of hydrogen on volume, cold high score oil, the main cold high score water that be made up of water and that be dissolved with hydrogen sulfide, ammonia being mainly made up of conventional liq hydrocarbon and dissolved hydrogen.Described cold high score water, wherein the content of ammonia is generally 0.5～15% (w), is preferably 1～8% (w).An object of note washing water is ammonia and the hydrogen sulfide absorbing in hydrogenation reaction effluent, prevents from forming sulphur hydrogenation ammonia or many sulphur ammonia Crystallization Plugging heat exchanger channel, increases system pressure drop.The injection rate of described washing water, should determine according to following principle: on the one hand, washing water are divided into vapour phase water and liquid phase water after injecting hydrogenation reaction effluent, and the liquid phase water yield must be greater than zero, is preferably 30% or more of washing water total amount; Again on the one hand, washing water, for absorbing the ammonia of hydrogenation reaction effluent, prevent that the ammonia concentration of high score gas is too high, reduce catalyst activity, conventionally the ammonia volumetric concentration of high score gas is more low better, is generally not more than 200PPm (v), is preferably not more than 50PPm (v).Described cold high pressure separator working pressure is that hydrogenation reaction partial pressure deducts true pressure and falls, and the difference of cold anticyclone separate part working pressure and hydrogenation reaction pressure is unsuitable too low or too high, is generally 0.35～3.2MPa, is generally 0.5～1.5MPa.The hydrogen volume concentration value of described cold high score gas, should not be too low (causing device working pressure to rise), generally should be not less than 70% (v), should be not less than 80% (v), preferably be not less than 85% (v).As previously mentioned at least a portion, be generally 85～100% cold high score gas and return in hydrogenation reaction part and recycle, so that the necessary amounts of hydrogen of hydrogenation reaction part and hydrogen concentration to be provided; In order to improve plant investment efficiency, must guarantee that recycle hydrogen concentration is not less than aforesaid low limit value,, distribute according to concrete feedstock property, reaction conditions, product for this reason, can get rid of methane, ethane that the described cold high score gas of a part produces to get rid of reaction.For the cold high score gas of discharge, can adopt conventional membrane separation process or pressure swing adsorption technique or oil wash technique to realize hydrogen and separate with non-hydrogen component, and the hydrogen reclaiming is used as to new hydrogen.
New hydrogen enters and adds hydrogen partial to supplement the hydrogen that adds hydrogen partial consumption, and new hydrogen hydrogen concentration is more high better, generally should not be lower than 95% (v), be preferably not less than 99% (v).All new hydrogen can be introduced to arbitrary hydrogenation reaction part.
Embodiment mono-
The present embodiment take the character of the blue charcoal energy generation device of the large-scale upright furnace by-product of Anshan Research Inst. of Heat Energy, China Iron & Steel Group and metallurgical furnace limited liability company of Huanggang Huaxing if the coalite tar of table 2 is as example explanation the present invention.
Be processed as example with 500,000 tons/year of coalite tars, fractionation coalite tar obtains conventional boiling point coal tar lighting end lower than 482 ℃ higher than the coal-based heavy oil of 482 ℃ and conventional boiling point of approximately 7.5 ten thousand tons/year.
Conventional boiling point enters coal tar lighting end unifining process HPU1 lower than the coal tar lighting end of 482 ℃, hydrogenation unit processing condition in table 3 to table 7, separate hydrofining generation oil and obtain gas, liquefied gas, petroleum naphtha, hydrofining diesel oil, 9.07 ten thousand tons/year of hydrofining tail oils (wherein conventional boiling point is 6.3 ten thousand tons/year higher than the cut of 350 ℃), all hydrofining tail oils remove floating bed hydrocracking device as hydrogen supply dissolvent oil.
In the present embodiment, hydrofining tail oil and coal-tar pitch are mixed into floating bed hydrocracking mixing raw material F100, the method that hydrocracking process of suspended bed adopts patent application 201010217358.1 to record is suspension bed (or bubbling bed or the slurry state bed) hydrocracking reaction that coal tar heavy cut carries out heterogeneous catalyst, and step is as follows:
A, oil, catalyzer, vulcanizer step with slurry: the powdered catalyst particle (composite hydrogenation catalyst that a certain amount of ingredients oil (having removed turning oil and/or the floating bed hydrocracking mixing raw material F100 of catalyzer), granularity is less than to 100 μ m, wherein high-activity component metal is 1: 1000 to 1: 10 with the mass ratio of low activity component metals) and vulcanizing agent together with under the agitation condition of 80 ℃～200 ℃, mix and make oil-catalyst slurry, control the solids concn of oil-catalyst slurry in 20～45% scopes;
B, (hydrogenation reaction resultant is through atmospheric tower fractionation gained heavy oil of the normal end with the turning oil that contains catalyzer for oil-catalyst slurry and all the other floating bed hydrocracking mixing raw material F100, account for 4/5ths quantity) mix as compound, compound boosts through feedstock pump, mixed hydrogen, after intensification, enter suspension bed (or bubbling bed or slurry state bed) hydrogenator and carry out hydrocracking reaction, the add-on of catalyzer is to control the metal of active ingredient and coal tar raw material mass ratio as 0.1: 100 to 4: 100, reactor reaction effluent is through high-temperature separator, after low-temperature separator, obtain liquid-solid phase height point oil mixt stream and hydrogen-rich gas two parts.Hydrogen-rich gas is as recycle hydrogen.A liquid-solid phase height point oil mixt is flowed through after atmospheric tower fractionation, obtain being less than 370 ℃ of benzolines, at the bottom of tower, obtain the heavy oil of the normal end (being greater than in 370 ℃ of distillates) that contains catalyzer, wherein heavy oil of most of (about 4/5ths) normal end is recycled directly to and in floating bed hydrogenation reactor, further carries out hydrogenation lighting reaction as turning oil, the heavy oil of the normal end of all the other small portions (about 1/5th) adopts the method for filtering or distill to carry out solid-liquid separation, after separation, obtain catalyst residue and floating bed hydrogenation heavy distillate, the partial solvent that the reaction raw materials of this part heavy distillate or direct and suspension bed mixes or prepares as oil-catalyst slurry, circulation enters in suspension bed or bubbling bed hydrogenator further carries out hydrogenation lighting reaction, and the catalyzer of deviating from gets rid of outward or regenerates, wherein 320～480 ℃ of floating bed hydrogenation temperature of reaction, reaction pressure 8～19MPa, volume space velocity 0.3～3.0h
-1, hydrogen to oil volume ratio 500～2000, catalyzer is the powdered granule coal tar hydrogenation catalyst of supporting compound many metal active constituents, wherein the mass ratio of high-activity component metal and low activity component metals is 1: 1000 to 1: 10, add-on is that activity component metal amount and coal tar raw material mass ratio are 0.1: 100 to 4: 100, the tail oil major part that contains catalyzer that hydrogenation reaction product separates after lightweight oil direct cycles to reactor, small part tail oil carries out being recycled to reactor after Removal of catalyst processing, further lighting, heavy oil all or maximum circulation, realize the object that coal tar maximum is produced lightweight oil and catalyst recycling, greatly improve the utilising efficiency of raw material and catalyzer,
In suspension bed or bubbling bed hydrogenation reaction product, conventional boiling point is less than the benzoline of 370 ℃ and enters special hydrogenation upgrading process HPU3 and produce the products such as gas, liquefied gas, petroleum naphtha, diesel component.
Embodiment bis-
Based on embodiment mono-, in suspension bed or bubbling bed hydrogenation reaction product, be less than 370 ℃ of benzolines and enter dead oil unifining process HPU1 and combine processing, produce gas, liquefied gas, petroleum naphtha, diesel component, hydrofining tail oil etc.In suspension bed or bubbling bed hydrogenation reaction product, conventional boiling point is greater than the distillate of 370 ℃ and enters suspension bed or the bubbling bed hydrogenation process HPU21 cracking that circulates.
Compared with embodiment mono-, the upgrading course of processing and dead oil unifining process HPU1 that floating bed hydrocracking generates oily lightweight oil have realized merging, have simplified flow process.
Embodiment tri-
Based on embodiment bis-, improve floating bed hydrocracking and generate oily lightweight oil final boiling point, be that in suspension bed or bubbling bed hydrogenation reaction product, conventional boiling point is less than the benzoline of 450 ℃ and enters foregoing dead oil unifining process HPU1 and combine processing, produce gas, liquefied gas, petroleum naphtha, diesel component, hydrofining tail oil etc.
Compared with embodiment bis-, improve the hydrogenation load of unifining process HPU1, improve solvent oil ratio in hydrocracking process of suspended bed HPU21 stock oil, alleviate the hydrogenation load of hydrocracking process of suspended bed.
Embodiment tetra-
Based on embodiment tri-, refining partial hydrogenation tail oil (approximately 3～40,000 tons/year) is sent into the diesel component that hydrofining tail oil hydrocracking process HPU4 (being different from hydrocracking process of suspended bed HPU21) production cetane value is greater than 45, HPU4 per pass conversion 60～70 % by weight, at least a portion HPU4 hydrocracking generates oily wax oil component (conventional boiling point is higher than 350 ℃ of components) and returns to HPU4 and contact with hydrocracking catalyst.Combined separation after HPU4 reaction effluent mixes with unifining process HPU1 reaction effluent.
Compared with embodiment tri-, increase hydrofining tail oil hydrocracking process HPU4, alleviate the hydrocracking load of hydrocracking process of suspended bed HPU21, reduce solvent oil ratio in floating bed hydrocracking stock oil.
Embodiment five
Based on embodiment mono-, it is the carbolic oil of 165～245 ℃ that fractionation coalite tar obtains conventional boiling point, and carbolic oil is separated into sodium phenolate solution and dephenolize oil after alkali aqueous solution extraction, after the dehydration of dephenolize oil, removing impurities as the stock oil of unifining process HPU1.
Although only enumerate five embodiment herein, be enough to show effect of the present invention.
The anhydrous coal tar main character of table 2
| Project | Coal tar | Coal tar hydrogenating charging |
| Cut | Full cut | A：B=3／4(v／v) |
| Density (20 ℃), kg/m 3 | 1.0981 | 0.9822 |
| Boiling range, ℃ | ? | ? |
| IBP／10％ | 142 | 165／222 |
| 30％／50％ | ? | 289／332 |
| 70％／90％ | 85%: 482 | 366／407 |
| 95％／EBP | ? | 430／524 |
| Sulphur, % | 0.14 | 0.13 |
| Nitrogen, % | 1.06 | 0.7659 |
| C／H | 84.86／9.07 | 83.37／9.16 |
| Condensation point, ℃ | ? | 10 |
| Viscosity (100 ℃), mm/s 2 | ? | 3.467 |
| Carbon residue, % | 5.11 | 0.47 |
| Acid number, mgKOH/g | ? | 0 |
| Heavy metal/ppm | ? | ? |
| Fe | 66.28 | 40.47 |
| Na | 0.63 | 0.37 |
| Ni | 0.0483 | 0.0143 |
| V | 0.0282 | 0.0252 |
| Project | Full cut | Hydrogenation charging |
| Mass spectrum composition, m% | ? | ? |
| Colloid | ? | 37.4 |
| Paraffinic hydrocarbons | ? | 10.1 |
| Naphthenic hydrocarbon | ? | 8.2 |
| Monocycle/dicyclo | ? | 3.2／1.0 |
| Three rings/Fourth Ring | ? | 2.0／1.4 |
| Five rings/six ring | ? | 0.5／0.1 |
| Aromatic hydrocarbons | ? | 44.3 |
| Monocycle/dicyclo | ? | 10.4／17.3 |
| Three rings/Fourth Ring | ? | 9.6／4.4 |
| Five rings/thiophene | ? | 0.0／2.2 |
| Do not identify | ? | 0.4 |
? table 3 coal tar hydrorefining processing condition
| Raw material | Coal tar < 480 ℃ of cuts |
| Reaction stagnation pressure, MPa | 15.8 |
| Hydrogen to oil volume ratio | 1200∶1 |
| Protective material | D |
| Protective material volume space velocity/h -1 | 2.0 |
| Finishing agent average reaction temperature/℃ | 380 |
| Finishing agent volume space velocity/h -1 | 0.5 |
Table 4 coal tar hydrorefining product distributes
| Generate the water yield, m% | 5.57 |
| Liquid yield, % | 97.06 |
| Treated oil density (20 ℃)/g.cm -3 | 0.8673 |
| Treated oil nitrogen content/μ g.g -1 | 10.0 |
| Treated oil product distributes, % | ? |
| H 2S／NH 3 | 0.14／0.93 |
| C 1／C 2 | 0.16／0.15 |
| C 3／C 4 | 0.24／0.09 |
| < 160 ℃ (petroleum naphtha) | 13.78 |
| 160 ℃-330 ℃ (diesel oil) | 61.95 |
| > 330 ℃ (hydrogenation tail oil) | 21.33 |
| Chemical hydrogen consumption, % | 4.34 |
? table 5 coal tar hydrorefining naphtha fraction character
| Cut scope/℃ | <160 |
| Density (20 ℃)/g.cm -3 | 0.775 |
| Boiling range/℃ | ? |
| IBP／10％／30％／50％ | 75／98／107／114 |
| 70％／90％／95％／EBP | 125／142／150／174 |
| Sulphur/μ g.g -1 | 9.1 |
| Nitrogen/μ g.g -1 | 1.0 |
| Octane value (RON) | 67 |
| Composition, % | ? |
| Paraffinic hydrocarbons | 11.96 |
| Naphthenic hydrocarbon | 79.09 |
| Aromatic hydrocarbons | 8.91 |
| Latent (the C8)/% of virtue | 65.06 |
Table 6 coal tar hydrorefining diesel oil distillate character
| Cut scope, ℃ | 160-330 |
| Density/g.cm -3(20℃) | 0.8913 |
| Boiling range/℃ | ? |
| IBP／10％／30％／50％ | 193／220／246／269 |
| 70％／90％／95％／EBP | 289／314／322／329 |
| Sulphur/μ g.g -1 | 9.8 |
| Nitrogen/μ g.g -1 | 2.0 |
| Flash-point/℃ (remaining silent) | 89 |
| Condensation point/℃ | -28 |
| Cold filter clogging temperature/℃ | -19 |
| Carbon residue (10%), % | 0.02 |
| Cetane value (actual measurement) | 31 |
| Aromatic hydrocarbons, % | 38.1 |
| Monocycle/dicyclo/tri-ring | 31.8／6.1／0.2 |
table 7 coal tar hydrorefining tail oil character
| Cut scope/℃ | >330 |
| Density (20 ℃)/g.cm-3 | 0.8991 |
| Boiling range/℃ | ? |
| IBP／10％／30％／50％ | 247／329／356／379 |
| 70％／90％／95％／EBP | 403／435／457／529 |
| Sulphur/μ g.g -1 | 12.9 |
| Nitrogen/μ g.g -1 | 14.5 |
| Condensation point/℃ | 28 |
| Aromatic hydrocarbons, % | 28.3 |
| Monocycle | 13.5 |
| Dicyclo | 8.5 |
| Three rings | 2.1 |
| Fourth Ring | 1.0 |
Claims (35)
1. a hydrogenation lightening method that uses the low hydrogen content heavy oil of hydrogen supply hydrocarbon, comprises the steps:
Heavy oil streams HDS is mainly made up of higher than the hydrocarbon component HD of 450 ℃ conventional boiling point, and heavy oil streams HDS is selected from one or more in following material:
1. coalite tar heavy oil fraction;
2. coal-tar middle oil heavy oil fraction;
3. coal-tar heavy oil heavy oil fraction;
4. petroleum base heavy oil thermal course of processing gained heavy oil fraction product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;
5. shale oil basic weight oil hot procedure gained heavy oil fraction product;
6. tar sand basic weight oil hot procedure gained heavy oil fraction product;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, under hydrogen and catalyzer existence condition, the hydrogenation lighting reaction HPU21R that heavy oil streams HDS comprises hydrocracking reaction, at least a portion hydrocarbon component HD completes hydrocracking reaction and obtains reaction effluent HPU21P, it is characterized in that the hydrogen supply hydrocarbon stream SHS that contains hydrogen supply hydrocarbon SH enters hydroconversion reaction zone HPU21, in hydrogenation reaction HPU21R process, hydrogen supply hydrocarbon SH contacts with hydrocarbon component HD;
Described hydrogen supply hydrocarbon SH refer to fractional saturation double ring arene and or the polycyclic aromatic hydrocarbons of fractional saturation; In logistics SHS, gum level is lower than 10 % by weight, and asphalt content is lower than 1 % by weight; In logistics SHS, in hydrogen supply hydrocarbon SH weight and logistics SHS, the ratio of conventional liquid hydrocarbon component gross weight exceeds in heavy oil streams HDS the ratio at least 3% of conventional liquid hydrocarbon component gross weight in hydrogen supply hydrocarbon SH weight and heavy oil streams HDS; In logistics SHS, conventional liquid hydrocarbon component protium weight in average content exceeds the protium weight content at least 2% of heavy oil streams HDS;
Hydrogen supply hydrocarbon stream SHS is prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target from processing hydrogen supply hydrocarbon precursor logistics SHSBF's with hydrogen supply hydrocarbon; In logistics SHS, hydrogen supply hydrocarbon SH weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight; In the weight rate SHSW of hydrogen supply hydrocarbon stream SHS and heavy oil streams HDS, conventional boiling point is higher than the ratio K=SHSW/HDW of the weight rate HDW of the hydrocarbon component HD of 450 ℃, K=0.1～10.
2. method according to claim 1, is characterized in that:
Hydrogen richness is mainly made up of higher than the hydrocarbon component HD of 450 ℃ conventional boiling point lower than the heavy oil streams HDS of 8 % by weight; Heavy oil streams HDS is selected from one or both in following material:
1. coalite tar heavy oil fraction;
2. coal-tar middle oil heavy oil fraction;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor HPU21-SB, charging autoreactor HPU21-SB bottom enters, temperature be 300～500 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 500: 1～4000: 1, hydrogenation catalyst HPU21-CAT add weight be HDS weight 0.01～5.0%, volume space velocity is 0.1～10.0hr
-1reaction conditions under, complete the hydrogenation lighting reaction that comprises hydrocracking reaction and obtain hydrogenation lighting reaction effluent HPU21P, flow out on reaction effluent HPU21P autoreactor HPU21-SB top;
Hydrogen supply hydrocarbon stream SHS is prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target from processing hydrogen supply hydrocarbon precursor logistics SHSBF's with hydrogen supply hydrocarbon; In logistics SHS, hydrogen supply hydrocarbon SH weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight; In the weight rate SHSW of hydrogen supply hydrocarbon stream SHS and heavy oil streams HDS, conventional boiling point is higher than the ratio K=SHSW/HDW of the weight rate HDW of the hydrocarbon component HD of 450 ℃, K=0.2～5;
Hydrogen supply hydrocarbon precursor logistics SHSBF is selected from one or more in following logistics:
1. be mainly the logistics of the coalite tar fractions consisting of 350～450 ℃ by conventional boiling point;
2. be mainly the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ by conventional boiling point;
3. be mainly the logistics of the coal-tar heavy oil fractions consisting of 230～450 ℃ by conventional boiling point;
4. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coalite tar fractions consisting of 350～450 ℃ of cuts by comprising conventional boiling point;
5. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ of cuts by comprising conventional boiling point;
6. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coalite tar fractions consisting of 350～450 ℃ of cuts by the conventional boiling point after dephenolize;
7. be mainly that 120～350 ℃ of cuts and conventional boiling point are the logistics of the coal-tar middle oil fractions consisting of 350～450 ℃ of cuts by the conventional boiling point after dephenolize.
3. method according to claim 2, is characterized in that:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS hydrogen supply hydrocarbon processed hydrogenation reaction HPU1R forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar, at least a portion hydrocarbon component MF completes hydrogenation modification reaction and obtains hydrogenation reaction effluent HPU1P, and the hydrogen supply hydrocarbon stream SHS obtaining based on hydrogenation reaction effluent HPU1P is selected from one or several of following logistics:
1. reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
2. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1-HSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
3. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1-HS0 is as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21, and the hot high score oil of at least a portion HPU1-HSO step-down, degassed rear gained liquid HPU1-HSOA enter hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
4. reaction effluent HPU1P enters cold anticyclone sepn process HPU1-CS and is separated into cold high score oil HPU1-CSO and cold high score gas HPU1-CSV, the cold high score oil of at least a portion HPU1-CSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
5. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
6. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion mainly by conventional boiling point be 350～450 ℃ be rich in logistics that hydrogen supply hydrocarbon component forms as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS.
4. method according to claim 2, is characterized in that:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from containing of coal tar conventional boiling point be that the logistics LMFS of 60～450 ℃ of hydrocarbon LMF completes deep hydrofinishing reaction HPU1R and is converted into hydrogenation reaction effluent HPU1P, conventional boiling point is that the hydrocarbon of 60～350 ℃ is converted into petroleum naphtha and diesel component, conventional boiling point is that the hydrocarbon of 350～450 ℃ is converted into the hydrogenation tail oil that is rich in hydrogen supply hydrocarbon SH, and the hydrogen supply hydrocarbon stream SHS obtaining based on hydrogenation reaction effluent HPU1P is selected from one or several of following logistics:
1. reaction effluent HPU1P enters thermal high sepn process HPU1-HS and is separated into hot high score oil HPU1-HSO and hot high score gas HPU1-HSV, the hot high score oil of at least a portion HPU1-HSO is as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
2. the intermediate reaction effluent HPU1MP that is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon enters thermal high sepn process HPU1M-HS and is separated into hot high score oil HPU1M-HSO and hot high score gas HPU1MP-HSV, the hot high score oil of at least a portion HPU1M-HSO is as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21, after the degassed rear gained degas oil HPU1M-HSOA of the hot high score oil HPU1M-HSO step-down of at least a portion mixes with heavy oil streams HDS, enters hydroconversion reaction zone HPU21;
3. separating reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS, and hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS;
4. separating reaction effluent HPU1P obtains hydrogenated oil HPU1P0 and hydrogen-rich gas; In hydrogenated oil HPU1P0 fractionation part, separate the logistics that hydrogenated oil HPU1PO obtains being rich in hydrogen supply hydrocarbon component, at least a portion mainly by conventional boiling point be 350～450 ℃ be rich in logistics that hydrogen supply hydrocarbon component forms as hydrogen supply hydrocarbon stream SHS, hydrogen supply hydrocarbon stream SHS enters hydroconversion reaction zone HPU21 after mixing with heavy oil streams HDS.
5. method according to claim 4, is characterized in that:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from coal tar be mainly that the hydrogenation modification that logistics LMFS that 60～450 ℃ of hydrocarbon LMF forms carries out reacts HPU1R by conventional boiling point, to produce to greatest extent hydrogen supply hydrocarbon as target.
6. according to the method described in claim 3 or 4 or 5, it is characterized in that:
Heavy oil streams HDS mainly by conventional boiling point higher than 450 ℃ hydrogen richness form lower than the coal tar heavy fractioning HD of 6.5 % by weight;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, temperature be 320～480 ℃, pressure be 10.0～20.0MPa, hydrogen/stock oil volume ratio be 1000: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.1～2.0%, volume space velocity is 0.2～5.0hr
-1reaction conditions under operate; In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.3～3.
7. method according to claim 2, is characterized in that:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst PU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
8. method according to claim 2, is characterized in that:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
9. method according to claim 2, is characterized in that:
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that the hydrocarbon that at least a portion is mainly 350～450 ℃ by conventional boiling point forms removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target; The logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation upgrading reaction and obtain hydrogenation reaction effluent HPU3P.
10. method according to claim 2, is characterized in that:
The hydrogenation reaction effluent HPU21P that turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight enters the hot high score fluid body HPU21P-HSL that hot high-pressure separator HPU21P-HS is separated into hot high score gas HPU21P-HSV and contains solid particulate, and hot high-pressure separator HPU21P-HS is to operate under 350～500 ℃, the pressure condition that is 6.0～28.0MPa in temperature; The main oil product being made up of higher than the hydrocarbon of 450 ℃ conventional boiling point that heat of dissociation high score fluid body HPU21P-HSL obtains enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and contacts with catalyzer HPU21-CAT;
Hot high score gas HPU21P-HSV enters hydrogenation upgrading cascade reaction district HPU22, the main liquid hydrocarbon being made up of lower than the hydrocarbon of 450 ℃ conventional boiling point that heat of dissociation high score oil HPU21P-HSL obtains enters hydrogenation upgrading cascade reaction district HPU22, the main logistics LFS being made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar existing enters hydrogenation upgrading cascade reaction district HPU22, hydrogenation upgrading cascade reaction district HPU22 operational condition is: temperature is 280～440 ℃, pressure is 6.0～28.0MPa, hydrogen/stock oil volume ratio is 300: 1～3000: 1, hydrogenation catalyst HPU22-CAT volume space velocity is 0.05～5.0hr
-1, complete hydrogenation upgrading cascade reaction and obtain hydrogenation upgrading cascade reaction effluent HPU22P,
At the separate part HPU22P-S of hydrogenation upgrading cascade reaction effluent HPU22P, separate hydrogenation upgrading cascade reaction effluent HPU22P and obtain hydrogen-rich gas HPU22PH and hydrogenated oil HPU22PO, at least a portion hydrogen-rich gas HPU22PH returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
At hydrogenated oil HPU22PO separate part HPU22PO-FS, separate hydrogenated oil HPU22PO and obtain gas and narrow fraction oil product.
11. methods according to claim 10, is characterized in that:
At hydrogenated oil HPU22P0 separate part HPU22P0-FS, separate the main oil product being formed higher than the hydrocarbon of 350 ℃ by conventional boiling point that hydrogenated oil HPU22P0 obtains and enter the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and contact with catalyzer HPU21-CAT.
12. methods according to claim 10, is characterized in that:
At hydrogenated oil HPU22P0 separate part HPU22P0-FS, separate the main oil product being formed higher than the hydrocarbon of 350 ℃ by conventional boiling point that hydrogenated oil HPU22P0 obtains and enter the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and contact with catalyzer HPU1-CAT.
13. methods according to claim 10, is characterized in that:
Hydrogenation upgrading cascade reaction district HPU22 uses ebullated bed reactor or suspended-bed reactor.
14. methods according to claim 2, is characterized in that:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separation hydrogenated oil HPU1PO obtains being rich in the logistics of hydrogen supply hydrocarbon component, and what at least a portion was mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target.
15. methods according to claim 2, is characterized in that:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separation hydrogenated oil HPU1PO obtains being rich in the logistics of hydrogen supply hydrocarbon component, and what at least a portion was mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point is rich in the logistics of hydrogen supply hydrocarbon component as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21P0 and hydrogen-rich gas; In hydrogenated oil HPU21P0 fractionation part, separate hydrogenated oil HPU21P0 and obtain narrow fraction oil product, the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target.
16. methods according to claim 2, is characterized in that:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P, and at least a portion reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics HPU3-F1 that at least a portion is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
17. methods according to claim 2, is characterized in that:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, from coal tar be mainly that logistics MFS that 350～450 ℃ of hydrocarbon MF forms completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P by conventional boiling point, at least a portion reaction effluent HPU1P is used as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21PO and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, and the logistics that the hydrocarbon that at least a portion is mainly 350～450 ℃ by conventional boiling point forms removes to be prepared as with hydrogen supply hydrocarbon the hydroconversion reaction zone HPU1 of target; The logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
18. methods according to claim 2, is characterized in that:
At the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, the logistics MFS forming from the hydrocarbon MF that is mainly 350～450 ℃ by conventional boiling point of coal tar completes hydrogenation modification reaction HPU1R and obtains reaction effluent HPU1P, and at least a portion reaction effluent HPU1P is as hydrogen supply hydrocarbon stream SHS;
The reaction effluent HPU21P that separation turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight obtains hydrogenated oil HPU21PO and hydrogen-rich gas; In hydrogenated oil HPU21PO fractionation part, separate hydrogenated oil HPU21P0 and obtain narrow fraction oil product, the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target is removed in the logistics that at least a portion is mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point, and the logistics that at least a portion is mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point removes to turn to heavy oil lightweight the hydroconversion reaction zone HPU21 of target;
Hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target in temperature as 260～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under operate, main logistics LFS be made up of lower than the hydrocarbon LF of 350 ℃ conventional boiling point from coal tar of logistics HPU3-F1 and existence carries out hydrogenation upgrading and reacts and obtain hydrogenation reaction effluent HPU3P.
19. methods according to claim 2, is characterized in that:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～440 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio is as 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity as 0.05～5.0hr
-1reaction conditions under complete hydrogenation modification reaction and obtain hydrogenation reaction effluent HPU1P;
The reaction effluent HPU1P that separation is prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon obtains hydrogenated oil HPU1PO and hydrogen-rich gas; In hydrogenated oil HPU1PO fractionation part, separate hydrogenated oil HPU1PO and obtain gas, narrow fraction oil product, the logistics that is rich in hydrogen supply hydrocarbon component that part is mainly made up of higher than 350 ℃ of hydrocarbon conventional boiling point is as hydrogen supply hydrocarbon stream SHS; The oil product HPU1PO-DO that part is mainly made up of higher than 350 ℃ of hydrocarbon conventional boiling point goes hydrocracking reaction process HPU4 to be converted into hydrocracking reaction effluent HPU4P, and hydrocracking reaction effluent HPU4P mixes with one or several in following logistics:
1. be prepared as the hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon;
2. the hydrogenation upgrading cascade reaction effluent HPU22P existing;
3. the hydrogenation reaction effluent HPU3P of the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target existing.
20. methods according to claim 1, there is middle turning oil system in the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, it is characterized in that:
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, the main heavy oil streams HDS being made up of higher than the coal tar heavy fractioning HD of 450 ℃ conventional boiling point enters the first reaction zone HPU211, temperature be 300～500 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 500: 1～4000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.05～5%, volume space velocity is 0.2～5.0hr
-1reaction conditions under, complete shallow degree hydrocracking reaction and obtain intermediate reaction effluent HPU211P; The intermediate reaction effluent HPU211P1 of first part is separated into intermediate gas and middle hydrocarbon ils, and middle hydrocarbon ils returns to the first reaction zone HPU211 as middle circulation hydrocarbon ils and contacts with hydrogenation catalyst HPU211-CAT; The second reaction zone HPU212 that second section intermediate reaction effluent HPU211P2 and intermediate gas enter hydroconversion reaction zone HPU21 carries out overhydrocracking reaction and obtains hydrogenation reaction effluent HPU212P, and reaction effluent HPU212P is as the hydrogenation reaction effluent HPU21P that turns to the hydroconversion reaction zone of target with heavy oil lightweight.
21. methods according to claim 20, it is characterized in that: the weight rate HPU211P1W of the intermediate reaction effluent HPU211P1 of first part, with the ratio K=HPU211P1W/HPU211P2W of the weight rate HPU211P2W of second section intermediate reaction effluent HPU211P2, K=0.5～2.
22. methods according to claim 2, is characterized in that:
There is two-way hydrogen supply hydrocarbon precursor material: lightweight hydrogen supply hydrocarbon precursor SHB1 and heavy hydrogen supply hydrocarbon precursor SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 obtains hydrogenation reaction effluent HPU11P through aromatic hydrogenation fractional saturation process HPU11, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, hydrogenation reaction effluent HPU11P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 obtains hydrogenation reaction effluent HPU12P through aromatic hydrogenation fractional saturation process HPU12, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, hydrogenation reaction effluent HPU12P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD.
23. methods according to claim 2, is characterized in that:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 is the distillate HPU11PSP of 60～350 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU11 gained hydrogenation reaction effluent HPU11P, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1; Distillate HPU11PSP enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 is the distillate HPU12PSP of 350～450 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU12 gained hydrogenation reaction effluent HPU12P, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1; Distillate HPU12PSP enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight makes hydrogen supply hydrocarbon contact with coal-tar hydrocarbon component HD.
24. methods according to claim 2, is characterized in that:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 obtains hydrogenation reaction effluent HPU11P through aromatic hydrogenation fractional saturation process HPU11, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 obtains hydrogenation reaction effluent HPU12P through aromatic hydrogenation fractional saturation process HPU12, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～20.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
There is the first reaction zone HPU211 and the second reaction zone HPU212 of serial operation in the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, coal tar heavy oil HDS enters the first reaction zone HPU211, SHB1 transforms the reaction effluent HPU11P obtaining and enters the first reaction zone HPU211 hydrogen supply hydrocarbon is contacted with coal-tar hydrocarbon component HD or its intermediate product, obtains the first reaction zone HPU211 reaction effluent HPU211P; Reaction effluent HPU211P enters the second hydroconversion reaction zone HPU212, SHB2 transforms the reaction effluent HPU12P obtaining and enters the second hydroconversion reaction zone HPU212 hydrogen supply hydrocarbon is contacted with the intermediate product of coal-tar hydrocarbon component HD, and second reaction zone HPU212 service temperature is compared with at least 10 ℃ of the first reaction zone HPU211 service temperature height.
25. methods according to claim 2, is characterized in that:
There is two-way hydrogen supply hydrocarbon precursor material SHB1 and SHB2, SHB1 is mainly the fractions consisting of 60～350 ℃ by conventional boiling point, SHB1 is the distillate HPU11PSP of 60～350 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU11 gained hydrogenation reaction effluent HPU11P, and aromatic hydrogenation fractional saturation process HPU11 is that 200～420 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
SHB2 is mainly the fractions consisting of 350～450 ℃ by conventional boiling point, SHB2 is the distillate HPU12PSP of 350～450 ℃ through the conventional boiling point of sepn process gained of aromatic hydrogenation fractional saturation process HPU12 gained hydrogenation reaction effluent HPU12P, and aromatic hydrogenation fractional saturation process HPU12 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.03～5.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
There is the first reaction zone HPU211 and the second reaction zone HPU212 of serial operation in the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, coal-tar hydrocarbon component HD enters the first reaction zone HPU211, SHB1 transforms the distillate HPU11PSP obtaining and enters the first reaction zone HPU211 hydrogen supply hydrocarbon is contacted with coal-tar hydrocarbon component HD or its intermediate product, obtains the first reaction zone HPU211 reaction effluent HPU211P; Reaction effluent HPU211P enters the second hydroconversion reaction zone HPU212, SHB2 transforms the distillate HPU12PSP obtaining and enters the second hydroconversion reaction zone HPU212 hydrogen supply hydrocarbon is contacted with the intermediate product of coal-tar hydrocarbon component HD, and second reaction zone HPU212 service temperature is compared with at least 15 ℃ of the first reaction zone HPU211 service temperature height.
26. methods according to claim 1, is characterized in that:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the lighting end LMFS being mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point and the last running HS being mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point, last running HS is as heavy oil streams HDS, and lighting end LMFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB completes deep hydrofinishing reactive moieties at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and obtains hydrogenation reaction effluent HPU1P, the hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 200～440 ℃, pressure are as 6.0～28.0MPa, HPU21-CAT volume space velocity are as 0.05～10.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1, in hydrogenation reaction effluent HPU1P, full cut diesel-fuel cetane number is higher than 24;
Separate the distillate HPU1P-FHO that hydrogenation reaction effluent HPU1P obtains gas, the main distillate HPU1P-FLO being made up of lower than the hydrocarbon of 350 ℃ conventional boiling point and is mainly made up of higher than the hydrocarbon of 350 ℃ conventional boiling point, at least a portion distillate HPU1P-FHO enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight after mixing with heavy oil streams HDS as logistics SHS, and in logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, temperature be 350～500 ℃, pressure be 3.0～28.0MPa, hydrogen/stock oil volume ratio be 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under, carry out hydrogenation lighting reaction and obtain hydrogenation lighting reaction effluent HPU21P; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.2～5; Hydrogenation lighting reaction effluent HPU21P enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21-HPV and contains solid particulate, hot high score gas HPU21-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU21-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to hydroconversion reaction zone HPU21 and recycles;
The hot high score fluid of fractionation body HPU21-HPL and/or cold high score fluid body HPU21-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight; Outer oil extraction WPY penetration depth hydrofining reaction part HPU1 contacts with its Hydrobon catalyst, and outer oil extraction WPY completes hydrogenation upgrading reaction, and the hydrogenation upgrading reaction effluent obtaining enters in hydrogenation reaction effluent HPU1P.
27. methods according to claim 26, is characterized in that:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the carbolic oil that the hydrocarbon that is mainly 160～250 ℃ by conventional boiling point forms, carbolic oil is through becoming dephenolize oil containing after alkali aqueous solution extraction step, dephenolize oil enters treating tower, using conventional boiling point be 100～140 ℃ with the segregative hydrocarbon ils of water as interval hydrocarbon introduce treating tower, the low oily quantity for the treatment of tower tower is 5～20% of dephenolize oil, all the other dephenolizes oil autofining tower lateral line withdrawal functions, the tower top oil gas mainly be made up of interval hydrocarbon and water vapor leaves to be refined tower top and is separated into water and oil after cooling; The low oil for the treatment of tower tower removes coal tar fractional distillation tower; Treating tower side line oil enters hydrogenation reaction part HPU1 as dephenolize oil after refining as hydrogenating materials and contacts with its hydrogenation catalyst.
28. according to the method described in claim 26 or 27, it is characterized in that:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～420 ℃, pressure are as 10.0～25.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are as 0.1～2.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 800: 1～2500: 1, in hydrogenation reaction effluent HPU1P, full cut diesel-fuel cetane number is higher than 28;
In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight;
Turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight, temperature be 350～480 ℃, pressure be 10.0～25.0MPa, hydrogen/stock oil volume ratio be 800: 1～2500: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under operate, in the whole hydrocarbon feeds of hydroconversion reaction zone HPU21, conventional boiling point is greater than 40 % by weight higher than the cracking rate of the hydrocarbon component of 450 ℃.
29. methods according to claim 28, is characterized in that:
The weight rate SHW of hydrogen supply hydrocarbon SH and the ratio K=SHW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.3～3.
30. methods according to claim 1, is characterized in that:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, the first cut LFS that in separation, coalite tar obtains mainly be made up of lower than the hydrocarbon of 350 ℃ conventional boiling point, the second cut MFS and the main last running HS being formed higher than the hydrocarbon of 450 ℃ by conventional boiling point that mainly the hydrocarbon that is 350～450 ℃ by conventional boiling point forms, last running HS is as heavy oil streams HDS, and the second cut MFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB is converted into hydrogenation reaction effluent HPU1P at the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, and hydroconversion reaction zone HPU1 is that 250～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hT in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
At least a portion hydrogenation reaction effluent HPU1P enters the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight as logistics SHS after mixing with heavy oil streams HDS, and in logistics SHS, hydrogen supply hydrocarbon SH weight accounts in logistics SHS conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
The hydroconversion reaction zone HPU21 that turns to target take heavy oil lightweight in temperature as 350～500 ℃, pressure as 6.0～28.0MPa, hydrogen/stock oil volume ratio add as 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT weight as HD weight 0.01～2%, volume space velocity is as 0.1～10.0hr
-1reaction conditions under complete hydrogenation lighting reaction and obtain hydrogenation reaction effluent HPU21P; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.1～10; At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor, charging autoreactor bottom enters, and flow out on hydrogenation lighting reaction effluent HPU21P autoreactor top;
Reaction effluent HPU21P enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21-HPV and contains solid particulate, hot high score gas HPU21-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU21-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
The hot high score fluid of fractionation body HPU21-HPL and/or cold high score fluid body HPU21-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight;
The hydroconversion reaction zone HPU3 of oil extraction WPY hydrogenation upgrading reaction zone take the upgrading of lightweight carburetion as target is outside that 260～440 ℃, pressure are that 6.0～28.0MPa, hydrogen/stock oil volume ratio are that 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.05～5.0hr in temperature
-1reaction conditions under, outer oil extraction WPY and the first cut LFS that combines processing complete the reaction of hydrogenation upgrading system, obtain hydrogenation upgrading reaction effluent HPU3P;
At the separate part HPU3P-HS of hydrogenation upgrading reaction effluent, separation hydrogenation upgrading reaction effluent HPU3P obtains hydrogen-rich gas HPU3P-HSV and upgrading generates oily HPU3P-OP, and the hydroconversion reaction zone HPU3 that at least a portion hydrogen-rich gas HPU3P-HSV returns take the upgrading of lightweight carburetion as target recycles;
Separate upgrading and generate oily HPU3P-0P, obtain gas products and narrow fraction oil product.
31. methods according to claim 1, is characterized in that:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the lighting end LMFS being mainly made up of lower than the hydrocarbon of 450 ℃ conventional boiling point and the last running HS being mainly made up of higher than the hydrocarbon of 450 ℃ conventional boiling point, last running HS is as heavy oil streams HDS, and lighting end LMFS is as hydrogen supply hydrocarbon precursor material SHB;
SHB is converted into hydrogenation reaction effluent HPU1P through the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon, and hydroconversion reaction zone HPU1 is that 200～440 ℃, pressure are that 6.0～28.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are 0.05～10.0hr in temperature
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 300: 1～3000: 1;
At least a portion hydrogenation reaction effluent HPU1P enters hydroconversion reaction zone HPU21 as logistics SHS after mixing with heavy oil streams HDS, in logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 6 % by weight;
Hydroconversion reaction zone HPU21 temperature be 300～550 ℃, pressure be 6.0～28.0MPa, hydrogen/stock oil volume ratio be 300: 1～3000: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.01～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under, carry out hydrogenation lighting reaction and obtain hydrogenation lighting reaction effluent HPU21P; The weight rate SHSW of hydrogen supply hydrocarbon stream SHS and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.1～10; At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, use suspended-bed reactor, charging autoreactor bottom enters, and flow out on hydrogenation lighting reaction effluent HPU21P autoreactor top;
The reaction effluent HPU21P that turns to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight enters the hot high score fluid body HPU21-HPL that hot high-pressure separator HPU21-HPS is separated into hot high score gas HPU21-HPV and contains solid particulate, hot high score gas HPU21-HPV enters cold conditions high-pressure separator HPU21-CPS and is separated into cold high score gas HPU21-CPV and cold high score fluid body HPU21-CPL, and the cold high score gas of at least a portion HPU21-CPV returns to the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and recycles;
The hot high score fluid of fractionation body HPU21-HPL and or cold high score fluid body HPU21-CPL, the oil product obtaining is divided into and enters the turning oil and the outer oil extraction WPY that turn to the hydroconversion reaction zone HPU21 of target with heavy oil lightweight;
Outer oil extraction WPY hydrogenation upgrading reaction zone HPU3 is that 260～440 ℃, pressure are that 6.0～28.0MPa, hydrogen/stock oil volume ratio are that 300: 1～3000: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.05～5.0hr in temperature
-1reaction conditions under, outer oil extraction WPY completes hydrogenation upgrading system reaction, obtains hydrogenation upgrading reaction effluent HPU3P;
At the separate part HPU3P-HS of hydrogenation upgrading reaction effluent, separation hydrogenation upgrading reaction effluent HPU3P obtains hydrogen-rich gas 2CHPV and upgrading generates oily HPU3P-OP, and the hydroconversion reaction zone HPU3 that at least a portion hydrogen-rich gas 2CHPV returns take the upgrading of lightweight carburetion as target recycles;
Separate upgrading and generate oily HPU3P-0P, obtain gas products and narrow fraction oil product.
32. according to the method described in claim 30 or 31, it is characterized in that:
Separate the hydrogenation upgrading that hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target produces and generate oily HPU3P-0P, the conventional boiling point obtaining enters higher than the distillate of 350 ℃ the hydroconversion reaction zone HPU1 that is prepared as target with hydrogen supply hydrocarbon and contacts with hydrogenation catalyst HPU1-CAT.
33. according to the method described in claim 30 or 31, it is characterized in that:
Separate the hydrogenation upgrading that hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target produces and generate oily HPU3P-0P, the conventional boiling point obtaining enters higher than the distillate of 350 ℃ the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight and contacts with hydrocracking catalyst HPU21-CAT.
34. according to the method described in claim 30 or 31, it is characterized in that:
In the coal tar fractional distillation part that uses coal tar fractional distillation tower, in separation, coalite tar obtains the carbolic oil that the hydrocarbon that is mainly 160～250 ℃ by conventional boiling point forms, carbolic oil is through becoming dephenolize oil containing after alkali aqueous solution extraction step, dephenolize oil enters treating tower, using conventional boiling point be 100～140 ℃ with the segregative hydrocarbon ils of water as interval hydrocarbon introduce treating tower, the low oily quantity for the treatment of tower tower is 5～20% of dephenolize oil, all the other dephenolizes oil autofining tower lateral line withdrawal functions, the tower top oil gas mainly be made up of interval hydrocarbon and water vapor leaves to be refined tower top and is separated into water and oil after cooling; The low oil for the treatment of tower tower removes coal tar fractional distillation tower; Treating tower side line oil contacts with hydrogenation catalyst HPU3-CAT as the hydroconversion reaction zone HPU3 that after refining, dephenolize oil enters take the upgrading of lightweight carburetion as target as hydrogenating materials.
35. according to the method described in claim 30 or 31, it is characterized in that:
The hydroconversion reaction zone HPU1 that is prepared as target take hydrogen supply hydrocarbon in temperature as 250～420 ℃, pressure are as 10.0～20.0MPa, hydrogenation catalyst HPU21-CAT volume space velocity are as 0.1～2.0hr
-1, hydrogen/stock oil volume ratio is to operate under the reaction conditions of 800: 1～2500: 1;
In logistics SHS, hydrogen supply function hydrocarbon component S H weight accounts for conventional liquid hydrocarbon component gross weight ratio higher than 10 % by weight;
At the hydroconversion reaction zone HPU21 that turns to target with heavy oil lightweight, temperature be 350～480 ℃, pressure be 10.0～20.0MPa, hydrogen/stock oil volume ratio be 800: 1～2500: 1, hydrogenation catalyst HPU21-CAT add weight be HD weight 0.03～2%, volume space velocity is 0.1～10.0hr
-1reaction conditions under operate; The weight rate SHSW of hydrogen supply hydrocarbon stream SH and the ratio K=SHSW/HDW of conventional boiling point higher than the weight rate HDW of the coal tar heavy fractioning HD of 450 ℃, K=0.3～3;
At the hydroconversion reaction zone HPU3 take the upgrading of lightweight carburetion as target, be that 300～420 ℃, pressure are that 10.0～20.0MPa, hydrogen/stock oil volume ratio are that 800: 1～2500: 1, hydrogenation catalyst HPU3-CAT volume space velocity are 0.15～2.0hr in temperature
-1reaction conditions under operate.
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| CN103773441B (en) * | 2012-10-24 | 2015-09-30 | 中国石油化工股份有限公司 | A kind of ebullated bed liquid-phase hydrogenatin treatment process |
| CN104927914A (en) * | 2014-03-23 | 2015-09-23 | 何巨堂 | Higher aromatic hydrogenation method with low-hydrogen-oil-ratio pre-hydrogenation process with hydrogen-donor hydrocarbon |
| CN104194832A (en) * | 2014-08-08 | 2014-12-10 | 何巨堂 | Low-quality hydrocarbon hydrogenation method containing middle hydrogenated oil circulation step |
| CN105754648B (en) * | 2016-04-22 | 2018-02-27 | 神雾科技集团股份有限公司 | Coal tar processing method and its system |
| CN106635160B (en) * | 2016-12-06 | 2019-01-22 | 胜帮科技股份有限公司 | A kind of coal and coal tar mixed hydrogenation system and technique |
| CN106635159B (en) * | 2016-12-06 | 2019-04-05 | 胜帮科技股份有限公司 | A kind of coal tar suspension bed hydrogenation system of high solids content and technique |
| CN109762598A (en) * | 2018-03-11 | 2019-05-17 | 洛阳瑞华新能源技术发展有限公司 | The combined method of the hydrocarbon material up flow type heat from hydrogenation cracking process of series connection hydrogen supply hydrocarbon |
| CN110938461A (en) * | 2018-09-23 | 2020-03-31 | 何巨堂 | Suspension bed hydrogenation modification method of coal tar containing coal pitch |
| CN110964561A (en) * | 2018-09-28 | 2020-04-07 | 何巨堂 | Method for combining high aromatic hydrocarbon suspension bed hydrogenation and solvent method needle coke raw material extraction process |
| CN109609186A (en) * | 2018-12-29 | 2019-04-12 | 洛阳瑞华新能源技术发展有限公司 | The combined method of upper heat from hydrogenation cracking process and long distillate hydrocarbon ils fractional distillation process |
| CN111826188B (en) * | 2020-07-07 | 2021-09-07 | 鞍钢化学科技有限公司 | Raw material asphalt for carbon-based new material and production process thereof |
| CN113416569A (en) * | 2021-06-29 | 2021-09-21 | 胜帮科技股份有限公司 | Hydrogenation device and method for pulverized coal pyrolysis tar combined bed |
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