CN108970544A - A kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases method - Google Patents

A kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases method Download PDF

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CN108970544A
CN108970544A CN201710426072.6A CN201710426072A CN108970544A CN 108970544 A CN108970544 A CN 108970544A CN 201710426072 A CN201710426072 A CN 201710426072A CN 108970544 A CN108970544 A CN 108970544A
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hydrogenator
liquid
hydrogenation
upstream
hydrogen
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何巨堂
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Luoyang Rui Hua New Energy Technology Development Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/001—Controlling catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B01J8/0085—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction promoting uninterrupted fluid flow, e.g. by filtering out particles in front of the catalyst layer
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/008—Controlling or regulating of liquefaction processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/083—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts in the presence of a solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/086—Characterised by the catalyst used
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
    • B01J2219/00277—Apparatus
    • B01J2219/00351—Means for dispensing and evacuation of reagents
    • B01J2219/00418—Means for dispensing and evacuation of reagents using pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
    • B01J2219/00277—Apparatus
    • B01J2219/00477—Means for pressurising the reaction vessels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/44—Solvents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/70—Catalyst aspects

Abstract

A kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases method, the arrangement of liquid product return line system suitable for direct hydrogenation liquefaction of coal reactor, by increase reflux liquid product down going channel vertical height, simultaneously increase gas-liquid mixed phase reactor feed data feedback channel vertical height, increase the gravity flow motive force of reflux liquid phase product circulation while reducing other motive force quantity of demand；The consumption that circulating pump can reduce power consumption, reduce volume and weight, reduce manufacture difficulty, reduce cost, extend the service life, reducing Seal Oil and flushing oil；When motive force of flowing automatically realizes expected self-recycle amount, dedicated drive circulating pump can be cancelled or cancel the acting operating of normal operating operating condition pump；It may make up the hydrogenator system that reflux liquid phase product circulation and bubbling bed are combined certainly and improve reaction compartment liquid phase fraction, get rid of the limitation of pump machine tool design temperature and be convenient for selecting higher reaction temperature to improve thermal reaction rate and conversion ratio.

Description

A kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases method
Technical field
The present invention relates to a kind of liquid product of gas-liquid material upstream hydrogenator reflux power to increase method, is suitable for coal The arrangement for adding the liquid product return line system of hydrogen direct liquefaction reactor, by increasing reflux liquid product down going channel Vertical height, simultaneously increase gas-liquid mixed phase reactor feed data feedback channel vertical height, increase reflux liquid product follow The gravity flow motive force of ring reduces other motive force quantity of demand simultaneously；Circulating pump can reduce power consumption, reduce volume and weight, drop Low manufacture difficulty, the consumption reduce cost, extend the service life, reducing Seal Oil and flushing oil；Motive force of flowing automatically realizes expected gravity flow When internal circulating load, dedicated drive circulating pump can be cancelled or cancel the acting operating of normal operating operating condition pump；It may make up and produced from reflux liquid phase Object circulation improves reaction compartment liquid phase fraction with the hydrogenator system that bubbling bed is combined, and gets rid of pump machine tool design temperature limit It makes and is convenient for selecting higher reaction temperature to improve thermal reaction rate and conversion ratio.
Background technique
Gas-liquid material up flow type direct hydrogenation liquefaction of coal reactor of the present invention, can be any one suitable form The gas-liquid material up flow type direct hydrogenation liquefaction of coal reactor for having liquid product to flow back can be the reaction of up flow type boiling bed hydrogenation Device can be up flow type floating bed hydrogenation reactor such as bubbling bed hydrogenator, forced circulation floating bed hydrogenation reactor, interior The internal recycle suspension bed hydroprocessing reactor of portion's setting guide shell.
It is of the present invention to have liquid product reflux, refer to a certain gas-liquid in direct hydrogenation liquefaction of coal reaction system At least partly liquid product RKLDP for expecting up flow type direct hydrogenation liquefaction of coal reactor RK is back in reactor RK and/or returns It flow in the direct hydrogenation liquefaction of coal reactor RJ of the upstream reactor RK, then with process Flow of Goods and Materials to isolating liquid product The separating step of RKLDP completes a reflux cycle.
The liquid product reflow method of known gas-liquid material up flow type direct hydrogenation liquefaction of coal reactor has H-OIL hydrogen oily Shielding circulating pump forced circulation method that technique, LC-FINING technique use, to use hydrogen charging be that the injection of power gas sucks Supercharge method, use liquid feedstock be power liquid injection suck supercharge method, it might even be possible to be using gas-liquid mixed phase material be power The injection of material sucks supercharge method, wherein common method is using expensive shielding circulating pump forced circulation method.
In order to simplify above-mentioned liquid product reflux cycle system, reduces and invest, reduce operating cost, simplifying operation, or In order to reduce circulating pump pump case diameter, reduce power consumption, the present invention proposes the gas-liquid material up flow type coal hydrogenation for having liquid product to flow back Direct liquefaction reactor raises method for arranging, the liquid product return line system suitable for direct hydrogenation liquefaction of coal reactor Arrangement, by increasing the vertical height of reflux liquid product down going channel, increasing the reactor feed of gas-liquid mixed phase simultaneously The vertical height of data feedback channel increases the motive force of liquid product reflux cycle process, and liquid product reflux can be effectively reduced The pressurization value of the driving equipment of cyclic process, effect are:
1. the pressurization value of the driving equipment of liquid product reflux cycle process is effectively reduced, circulating pump can be reduced and be applied to The lift for recycling liquid material can reduce impeller of pump revolving speed under the premise of pump configuration is certain, reduce impeller, pump chamber overcurrent cavity The erosion rate on surface can extend the service life；
2. the pressurization value of the driving equipment of liquid product reflux cycle process is effectively reduced, circulating pump can be reduced and be applied to The lift for recycling liquid material, can reduce the power of the shield electric machine of circulating pump, under the premise of impeller of pump revolving speed is certain, can subtract Small impeller of pump diameter reduces the fluid end of circulating pump and the equipment volume of power end and weight, is conducive to reduce manufacture difficulty, reduce Cost is conducive to reduce pump housing vibration, convenient for arrangement；At this point, even circulating pump is only mainly used as go into operation pump, stop work pump, pipeline Flushing pump；
3. the pressurization value of the driving equipment of liquid product reflux cycle process is effectively reduced, the shielding of circulating pump can be reduced The power consumption of motor, the especially power consumption of normal operation operating condition；Circulating pump can reduce power of motor and acting calorific value, reduce The consumption of Seal Oil and flushing oil；
4. the motive force provided by value of raising when upper hydrogenator basis meets the reflux of anticipated number liquid product When the motive force numerical value of circulatory system whole, for example expensive circulating pump of dedicated driving equipment can be cancelled, for processing capacity For 2~3 reactors that the direct hydrogenation liquefaction of coal process of 2,000,000 tons/year of raw coal uses, every reactor saves 1 circulation About 0.35~0.40 hundred million yuan/platform set of the investment of pump, it is overall to save about 0.70~1.20 hundred million yuan, and Seal Oil, flushing oil can be saved Consumption caused by huge cost；
5. the vertical height of the data feedback channel of the reactor feed of increased gas-liquid mixed phase of the invention (as needed can also be with Increase catheter channel area), while being also a premixing reaction section, conducive to the mixture homogeneity for improving reactor feedstocks, benefit In raising reaction efficiency；
6. increasing the method for gravity flow motive force, method progress " the gas-liquid material up flow type coal for increasing skirt height is generallyd use Add hydrogen direct liquefaction reactor raises arrangement ", " gas-liquid material up flow type coal can also be carried out using the method for increasing height of foundation Add hydrogen direct liquefaction reactor raises arrangement ", or low level topography, ditch are used using the method for reducing mixing point absolute altitude Slot；It is of the present invention since gas-liquid material up flow type direct hydrogenation liquefaction of coal reactor RK is usually heavier and uses skirt The gas-liquid material up flow type direct hydrogenation liquefaction of coal reactor for having liquid product to flow back raises arrangement, refers to intentional by gas The bottom feed inlet absolute altitude of liquid material up flow type direct hydrogenation liquefaction of coal reactor RK improves；
Increase stressed method 7. can be superimposed using hydrogen injection formula Venturi tube or use oil liquid injecting type venturi Pipe increases stressed method or increases stressed method using miscible fluids Jet Ejector Venturi；
8. may make up the hydrogenator system of a certain amount of liquid product gravity flow systemic circulation of reactor, pump can be got rid of Machine Design limits and selects harsher reaction condition, and the safety of reaction system can be improved；
Built-in collection can be considered in the hydrogenator system of reflux liquid product gravity flow systemic circulation, the structure type of reactor The delivery line of the reflux liquid product of liquid cup, the preferably horizontal plane on the top of reactor, close liquid collecting cup bottom discharging mouth are attached Closely, using suitable discharge pipe arrangement (bottom level discharge, suck-back pipe be inserted into) will reflux liquid product from reactor device The side of wall exports, and rises the influence of stream flow to reduce to liquid collecting cup lower part, reduces the abrasion to drain tube wall, instead Device inner structure form is answered, the inner structure form of common reactor has been different from；
It is combined by the gravity flow systemic circulation of a certain amount of liquid product with bubbling bed short-circuit cycle in device 9. reactor may make up A kind of novel simple hydrogenator system of structure, by " lightweight liquid possessed by bubbling bed short-circuit cycle in reactor Expect the residence time is short, the heavy liquid material residence time it is long " selective reaction advantage, " will be exported with hot liquid product systemic circulation Reactor inlet raw material is distributed in reaction heat carrying ", " increase reactor cross section flow velocity prevent solids particles precipitate " the advantages of, group It closes and uses；
10. can by downstream reactor RK bottom opening absolute altitude, arrangement to be higher than upstream reactor RJ bottom opening absolute altitude certain Such as 20~40 meters of height, to realize the circulating pump RKPUMP of downstream reactor RK, outlet liquid is pressed into downstream reactor RK Differential pressure requirements, with will export liquid indentation upstream reactor RJ differential pressure requirements it is relatively consistent, so as to realize 1 Circulating pump reasonably conveys product liquid phegma to 2 or more reactors simultaneously, can significant simple flow, reduction throwing Money improves technological operation flexibility.
The difference in height for increasing Liquid product recycle pipeline such as raises skirt or the basis of equipment, is a kind of conventional engineering skill Art, still, a kind of liquid product reflux power of gas-liquid material upstream hydrogenator of the invention increase method, technical effect It is huge be it is surprising, unexpected, due to have liquid product flow back gas-liquid material up flow type direct hydrogenation liquefaction of coal reaction Device system has already appeared about 40 years, within very long so far 40 years time, does not occur being same as report of the invention, because This, the present invention has creativeness outstanding.
Therefore, an object of the present disclosure is to propose a kind of liquid product reflux power of gas-liquid material upstream hydrogenator Increase method.
Second purpose of the invention is to propose that a kind of liquid product of gas-liquid material upstream direct hydrogenation liquefaction of coal reactor returns Mobilization force increases method.
Third purpose of the present invention is to propose that a kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases Method significantly reduces the lift that circulating pump is applied to circulation liquid material.
4th purpose of the invention is to propose that a kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases Method, superposition increase stressed method using hydrogen injection or increase stressed method using oil liquid injection or use miscible fluids Injection increases stressed method.
5th purpose of the invention is to propose that a kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases Method, constitutes the hydrogenator system of a certain amount of liquid product gravity flow systemic circulation of reactor, and the machinery that can get rid of pump is set Meter limits and selects harsher reaction condition, and the safety of reaction system can be improved.
6th purpose of the invention is to propose that a kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases Method constitutes a kind of novel knot being combined by the gravity flow systemic circulation of a certain amount of liquid product with bubbling bed short-circuit cycle in device The simple hydrogenator system of structure.
7th purpose of the invention is to propose that a kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases Method, by downstream reactor RK bottom opening absolute altitude, arrangement is higher than upstream reactor RJ bottom opening absolute altitude certain altitude, in fact Existing 1 circulating pump reasonably conveys product liquid phegma to 2 or more reactors simultaneously.
Summary of the invention
A kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases method, it is characterised in that packet Containing following steps:
Hydrogenator R1X, hydrogenator R1X are used in the first hydrogenation process R1 of processing feedstock hydrocarbon R1F Including at least a gas-liquid material upstream hydrogenator R1K, when hydrogenator R1X quantity more than 1 and is serial operation pass When being, on the basis of just being flowed to by the process of raw material R1F, other reactors are located at the upstream or downstream of hydrogenator R1E；
1. in the first hydrogenation process R1, there are hydrogen, hydrocarbon liquid phase simultaneously there may be the mixed phase objects of solid particle Under the conditions of material, the raw material R1F at least containing carbon and protium enters the first hydrogenation process R1 progress first plus hydrogen is anti- R1R is answered to obtain the first hydrogenation reaction product BASE-R1P；
Raw material R1F is made of liquid hydrocarbon feeds R1FL and solid particulate materials R1FS that may be present；
The object of solid particle may be contained simultaneously containing hydrogen, hydrocarbon liquid phase based on the first hydrogenation reaction product BASE-R1P Material is used as the first hydrogenation reaction effluent R1P；
In first hydrogenation process R1, there are hydrogen, hydrocarbon liquid phase, there may be solid particles simultaneously；
First hydrogenation reaction R1R, the hydrofining reaction comprising at least part liquid material R1FL may be comprising at least The heat from hydrogenation cracking reaction of a part of liquid material R1FL may include at least part solid material R1FS's that may be present Heat from hydrogenation cracking reaction；
First hydrogenation process R1 may use catalyst R1C；
First hydrogenation reaction product BASE-R1P, for the mixed phase of solid particle may be contained simultaneously containing hydrogen, hydrocarbon liquid phase Material；
First hydrogenation reaction effluent R1P is for being discharged the first hydrogenation reaction product BASE-R1P, to contain hydrogen gas, liquid Hydrocarbon simultaneously may the mixed phase material containing solid particle；
First hydrogenation reaction effluent R1P occurs in the form of 1 tunnel or 2 tunnels or multichannel material；
2. gas-liquid material upstream hydrogenator R1K, setting top liquid trap LD；
Gas-liquid material upstream hydrogenator R1K includes lower section, that is, up flow type hydroconversion reaction zone Q1 and upper section, that is, Disengagement zone Q2； Upper section, that is, Disengagement zone Q2 is made of top liquid trap LD and reactor R1K shell upper section；
In up flow type hydroconversion reaction zone, Q1 obtains product R1KP；
In Disengagement zone Q2, a part of liquid phase isolated in R1KP obtains liquid product phegma R1KP-LR and net product R1KP-MP；
Liquid product phegma R1KP-SLR, be back in reactor R1K and/or be back to the upstream reactor R1K adds hydrogen In reactor R1X, a reflux cycle then is completed with process Flow of Goods and Materials to separate section R1KP-S；
3. along absolute altitude and direct hydrogenation liquefaction of coal reactor R1K on gas-liquid material upstream hydrogenator R1K, liquid trap LD The elevation difference of elevation of bottom is RH；
The down going channel WP of liquid product phegma R1KP-SLR passes through downwards the bottom hydrogenator R1K feed inlet N1 At least the 0.60 of RH times of downlink after absolute altitude, flows up into hydrogenator R1K after then mixing with hydrogen logistics H100 In the hydrogenator of upstream that is interior or entering hydrogenator R1K.
The present invention, in general, the 3. down going channel WP of liquid product phegma R1KP-SLR, passes through downwards hydrogenator At least 20 meters of downlink after the feed inlet N1 absolute altitude of the bottom R1K, then to upstream after mixing point KM is mixed with hydrogen logistics H100 In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K；Using raising hydrogenation reaction Method for arranging of the bottom the device R1K feed inlet N1 relative to ground elevation where hydrogenator R1K.
The present invention, in general, the 3. down going channel WP of liquid product phegma R1KP-SLR, passes through downwards hydrogenator At least 20 meters of downlink after the feed inlet N1 absolute altitude of the bottom R1K, then to upstream after mixing point KM is mixed with hydrogen logistics H100 In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K；Using reduction mixing point KM Method for arranging relative to ground elevation where hydrogenator R1K.
The present invention, generally, 3. the down going channel WP of liquid product phegma R1KP-SLR, passes through downwards hydrogenator 15~100 meters of downlink after the feed inlet N1 absolute altitude of the bottom R1K, then to upstream after mixing point KM is mixed with hydrogen logistics H100 In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K.
The present invention, preferably, 3. the down going channel WP of liquid product phegma R1KP-SLR, passes through downwards hydrogenator 25~40 meters of downlink after the feed inlet N1 absolute altitude of the bottom R1K, then to upstream after mixing point KM is mixed with hydrogen logistics H100 In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K.
The present invention can use circulating pump simultaneously, and 3. liquid product phegma R1KP-SLR is by circulation force (forcing) pump boosting The upstream of hydrogenator R1K is flowed up into hydrogenator R1K or entered after mixing afterwards with hydrogen logistics H100 Hydrogenator in.
The present invention, can simultaneously using gas swab, 3. liquid product phegma R1KP-SLR by gas swab QC increasing Enter in hydrogenator R1K after pressure or enter in the hydrogenator of upstream of hydrogenator R1K, gas swab QC is used Power gas be reaction feed gas.
The present invention, can simultaneously using gas swab, 3. liquid product phegma R1KP-SLR by gas swab QC increasing Enter in hydrogenator R1K after pressure or enter in the hydrogenator of upstream of hydrogenator R1K, gas swab QC is used Power gas be reaction feed hydrogen rich gas gas.
The present invention can use Liquid siphon simultaneously, and 3. liquid product phegma R1KP-SLR increases by Liquid siphon LC Enter in hydrogenator R1K after pressure or enter in the hydrogenator of upstream of hydrogenator R1K, Liquid siphon LC is used Power fluid be reaction feed liquid.
Self-running liquid product circulation may be implemented in the present invention, and 3. liquid product phegma R1KP-SLR enters by direct current In hydrogenator R1K or enter in the hydrogenator of upstream of hydrogenator R1K, that is to say, that the process is without using increasing Press equipment.
The present invention, the first hydrogenation process R1 can be selected from a kind or 2 kinds or several of following hydrogenation process Combination:
1. the adding using expanded bed of the logistics containing oil product obtained by middle coalite tar or its distillate or its hot procedure Hydrogen process；Hot procedure is selected from coking or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；
2. the logistics containing oil product obtained by high temperature coal-tar or its distillate or its hot procedure adds hydrogen using expanded bed Process；
3. the hydrogenation process using expanded bed of the logistics containing oil product obtained by shale oil or its distillate or its hot procedure；
4. the hydrogenation process using expanded bed of ethylene cracking tar；
5. the hydrogenation process using expanded bed of the logistics containing oil product obtained by petroleum based heavy fuel oils or its hot procedure；
6. the hydrogenation process using expanded bed of the logistics containing oil product obtained by tar sand base weight oil or its hot procedure；
7. direct hydrogenation liquefaction of coal liquefaction process uses the hydrogenation process of expanded bed, including using the coal of hydrogen supply dissolvent oil to add Hydrogen direct liquefaction liquefaction process, coal refines process to oil altogether, coal faces hydrogen thermosol liquefaction process；
8. the hydrogenation process using expanded bed of liquefaction oil obtained by direct hydrogenation liquefaction of coal liquefaction process；
9. hydrocarbon ils of other aromatic hydrocarbons weight contents higher than 40%, organic nitrogen weight content higher than 0.10% uses expanded bed Hydrogenation process.
The present invention, the first hydrogenation process R1, existing solid particle can 1 kinds or several in following:
1. semicoke particle obtained by direct hydrogenation liquefaction of coal process；
2. catalyst granules；
3. iron rust particle；
4. particles of inorganic material；
5. coking of coal process generate into the solid particle in coal tar；
6. the product solid particle from hydro carbons thermal condensation process；
7. the solid particle from shale；
8. the solid particle from oil-sand；
9. other particles being present in one-stage hydrogenation reaction product BASE-ARP.
The present invention, the first hydrogenation process R1, the expanded bed reactor, mode of operation can be selected from following a kind Or several combination:
1. suspension bed, that is, slurry bed system；
2. ebullated bed；
3. slight expanded-bed.
The present invention, in general, the 1. operating condition of the first hydroconversion process R1 are as follows: temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen/feedstock oil volume ratio are 50~5000.
The present invention, generally, the 1. operating condition of the first hydroconversion process R1 are as follows: temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen/feedstock oil volume ratio are 300~1000, hydrogenation catalyst R1-CAT volume space velocity be 0.05~ 5.0hr-1。
The present invention, the cylinder-shaped length of cylindrical shell sections of hydrogenator R1K, generally 10~45 meters.
Detailed description of the invention
Fig. 1 is that a kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases the 1st kind of method The principle process schematic diagram of embodiment, in direct hydrogenation liquefaction of coal reactor R, reactor comprising setting top liquid trap LD Withdrawing fluid product LDP delivery line 31, device exteenal reflux product liquid down-comer 35, the mixing point KK5 with coal slurry raw material MJ, coal slurry Mixing point KM, M100 and hot hydrogen for conveying house keeper 65, M100 and hot hydrogen H100 of the mixture M 100 of MJ and circulating liquid LDP The rising of the mixture F100 of gas H100 conveys house keeper 71, and program reactor R elevation of bottom is elevated " BH+H0 ", wherein BH The absolute altitude of mixing point KM (reactor feed becomes gas-liquid mixed phase material) absolute altitude of injection hydrogen is higher by for reactor R elevation of bottom Difference, H0 is the absolute altitude that hot hydrogen H100 Pipe installing requires, for the absolute altitude is both with respect to local ground elevation.
Elevation difference on liquid trap LD as shown in Figure 1 along absolute altitude and direct hydrogenation liquefaction of coal reactor R elevation of bottom is RH。
As shown in Figure 1, direct hydrogenation liquefaction of coal reactor R, can be the First of direct hydrogenation liquefaction of coal reaction process Or the direct hydrogenation liquefaction of coal reactor in last or middle position.
As shown in Figure 1, combined feed of the mixture F100 as reactor R, upstream is by being converted into product after reaction compartment RP enters liquid trap LD and the gas-liquid separation zone of reactor head wall composition is separated into circulating liquid LDP and the net product of mixed phase Reactor R is discharged through piping P100 in RP100, the net product RP100 of mixed phase, and usual pipeline P100 is inserted into mono- depthkeeping of liquid trap LD Degree.
As shown in Figure 1, as an example, the direct hydrogenation liquefaction of coal reactor R comprising setting top liquid trap LD, Along being RH with the difference of reactor R elevation of bottom on liquid trap LD, RH is 26 meters, and reactor R elevation of bottom is determined as " 30 meters + 10.5 meters ", wherein BH is 30 meters, and H0 is 10.5 meters, the tedge 71 for the gas-liquid two-phase state for being 30 meters due to there is height, Increase reflux purpose of the liquid product from mobilization force is realized, liquid material declines material averag density 650kg/m in pipeline 353, and Material averag density is 265kg/m in tedge 713, therefore 30 meters of height differences to decline the instantaneous quiet of pipeline 35 and tedge 71 It is 650kg/m that state pressure difference, which has reached averag density,317.8 meters of liquid-column height of liquid material, due to the presence of this motive force, follow The quantity of ring liquid LDP can achieve 1.1~1.2 times of coal slurry raw material MJ quantity.It is anti-with conventional bubbling bed Coal Liquefaction It answers device to compare, forms the up flow type bubbling bed reactor under self-recycle liquid and the common existence condition of fresh feed, increase The liquid phase ratio of reaction compartment, improves the space utilization rate of reactor.
Fig. 2 is that a kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases the 2nd kind of method The principle process schematic diagram of embodiment, the difference is that, superposition is sprayed logical using raw material coal slurry MJ with scheme described in Fig. 1 The method that Venturi tube KK5 increases the draft to circulation liquid material LDP is crossed, increases Liquid product recycle power, increases product liquid Loop number further increases the liquid phase ratio of reaction compartment, further improves the space utilization rate of reactor；Such as Fig. 2 Shown, coal slurry raw material MJ and the mixture M 100 of circulation liquid material LDP are conveyed through pipeline 65.
Fig. 3 is that a kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases the 3rd kind of method The principle process schematic diagram of embodiment, the difference is that, superposition is ejected through using raw hydrogen with scheme described in Fig. 2 The method that Venturi tube KK3 increases the draft to circulation liquid material LDP, increases Liquid product recycle power, increases product liquid and follows Number of rings amount further increases the liquid phase ratio of reaction compartment, further improves the space utilization rate of reactor；Such as Fig. 3 institute Show, the circulation liquid material LDP9 that raw hydrogen H100 and pipeline 33 convey, becomes mixture M 200 through pipeline by Venturi tube KK3 63 conveyings, convey after converging with the material in pipeline 65 through pipeline 71.
Fig. 4 is that a kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases the 4th kind of method The principle process schematic diagram of embodiment, the difference is that, superposition uses circulating pump PUMP increase pair with scheme described in Fig. 1 The method for recycling the draft of liquid material LDP increases Liquid product recycle power, increases Liquid product recycle quantity, further increases The liquid phase ratio of reaction compartment, further improves the space utilization rate of reactor；Or circulating pump PUMP lift is reduced, Under the premise of circulation revolution speed is constant, for centrifugal pump of single stage type, it is reduced significantly impeller of pump diameter, reduces pump case volume, reduced high Press pump manufacture difficulty；As shown in figure 4, the mixed material comprising coal slurry raw material MJ and raw hydrogen H100, with pump PUMP outlet It is conveyed after the circulation liquid material LDP mixing of road P01 conveying through pipeline 71.
Fig. 5 is that a kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases the 5th kind of method The principle process schematic diagram of embodiment, the difference is that, superposition is increased using circulating pump PUMP with scheme described in Fig. 2, Fig. 4 Add the method for the draft to circulation liquid material LDP, raw material coal slurry MJ to be ejected through Venturi tube KK5 to increase to circulation liquid material LDP's The method of draft increases Liquid product recycle power, increases Liquid product recycle quantity, further increases the liquid of reaction compartment Phase ratio further improves the space utilization rate of reactor；Or circulating pump lift is reduced, before circulation revolution speed is constant It puts, for centrifugal pump of single stage type, is reduced significantly impeller of pump diameter, reduces pump case volume, reduce high-pressure pump manufacture difficulty.
As shown in figure 5, the circulation liquid material LDP of pump PUMP outlet conduit P01 conveying, is ejected through text by raw material coal slurry MJ Venturi KK5 increases the draft to circulation liquid material LDP, and obtained mixture M 100 is conveyed through pipeline 65.
Fig. 6 is that a kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases the 6th kind of method The principle process schematic diagram of embodiment, with scheme described in Fig. 2 the difference is that, the circulating liquid LDP inside reactor R The arrangement of delivery line 31 is that the side wall on the top of reactor R is drawn.
Fig. 7 is that a kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases the 7th kind of method The principle process schematic diagram of embodiment, with scheme described in Fig. 2 the difference is that, by the straight of at least part tedge 71 Diameter expands, and reduces flow velocity to reduce the pressure drop of the flow process of tedge 71, increases Liquid product recycle power, increases liquid Product circulation quantity.
Specific embodiment
The present invention described in detail below.
Pressure of the present invention, refers to absolute pressure.
Concentration of component of the present invention is weight concentration i.e. mass concentration when not specified.
Characteristic of the invention is described below.
A kind of liquid product reflux power of gas-liquid material of the invention upstream hydrogenator increases method, it is characterised in that packet Containing following steps:
Hydrogenator R1X, hydrogenator R1X are used in the first hydrogenation process R1 of processing feedstock hydrocarbon R1F Including at least a gas-liquid material upstream hydrogenator R1K, when hydrogenator R1X quantity more than 1 and is serial operation pass When being, on the basis of just being flowed to by the process of raw material R1F, other reactors are located at the upstream or downstream of hydrogenator R1E；
1. in the first hydrogenation process R1, there are hydrogen, hydrocarbon liquid phase simultaneously there may be the mixed phase objects of solid particle Under the conditions of material, the raw material R1F at least containing carbon and protium enters the first hydrogenation process R1 progress first plus hydrogen is anti- R1R is answered to obtain the first hydrogenation reaction product BASE-R1P；
Raw material R1F is made of liquid hydrocarbon feeds R1FL and solid particulate materials R1FS that may be present；
The object of solid particle may be contained simultaneously containing hydrogen, hydrocarbon liquid phase based on the first hydrogenation reaction product BASE-R1P Material is used as the first hydrogenation reaction effluent R1P；
In first hydrogenation process R1, there are hydrogen, hydrocarbon liquid phase, there may be solid particles simultaneously；
First hydrogenation reaction R1R, the hydrofining reaction comprising at least part liquid material R1FL may be comprising at least The heat from hydrogenation cracking reaction of a part of liquid material R1FL may include at least part solid material R1FS's that may be present Heat from hydrogenation cracking reaction；
First hydrogenation process R1 may use catalyst R1C；
First hydrogenation reaction product BASE-R1P, for the mixed phase of solid particle may be contained simultaneously containing hydrogen, hydrocarbon liquid phase Material；
First hydrogenation reaction effluent R1P is for being discharged the first hydrogenation reaction product BASE-R1P, to contain hydrogen gas, liquid Hydrocarbon simultaneously may the mixed phase material containing solid particle；
First hydrogenation reaction effluent R1P occurs in the form of 1 tunnel or 2 tunnels or multichannel material；
2. gas-liquid material upstream hydrogenator R1K, setting top liquid trap LD；
Gas-liquid material upstream hydrogenator R1K includes lower section, that is, up flow type hydroconversion reaction zone Q1 and upper section, that is, Disengagement zone Q2； Upper section, that is, Disengagement zone Q2 is made of top liquid trap LD and reactor R1K shell upper section；
In up flow type hydroconversion reaction zone, Q1 obtains product R1KP；
In Disengagement zone Q2, a part of liquid phase isolated in R1KP obtains liquid product phegma R1KP-LR and net product R1KP-MP；
Liquid product phegma R1KP-SLR, be back in reactor R1K and/or be back to the upstream reactor R1K adds hydrogen In reactor R1X, a reflux cycle then is completed with process Flow of Goods and Materials to separate section R1KP-S；
3. along absolute altitude and direct hydrogenation liquefaction of coal reactor R1K on gas-liquid material upstream hydrogenator R1K, liquid trap LD The elevation difference of elevation of bottom is RH；
The down going channel WP of liquid product phegma R1KP-SLR passes through downwards the bottom hydrogenator R1K feed inlet N1 At least the 0.60 of RH times of downlink after absolute altitude, flows up into hydrogenator R1K after then mixing with hydrogen logistics H100 In the hydrogenator of upstream that is interior or entering hydrogenator R1K.
The present invention, in general, the 3. down going channel WP of liquid product phegma R1KP-SLR, passes through downwards hydrogenator At least 20 meters of downlink after the feed inlet N1 absolute altitude of the bottom R1K, then to upstream after mixing point KM is mixed with hydrogen logistics H100 In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K；Using raising hydrogenation reaction Method for arranging of the bottom the device R1K feed inlet N1 relative to ground elevation where hydrogenator R1K.
The present invention, in general, the 3. down going channel WP of liquid product phegma R1KP-SLR, passes through downwards hydrogenator At least 20 meters of downlink after the feed inlet N1 absolute altitude of the bottom R1K, then to upstream after mixing point KM is mixed with hydrogen logistics H100 In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K；Using reduction mixing point KM Method for arranging relative to ground elevation where hydrogenator R1K.
The present invention, generally, 3. the down going channel WP of liquid product phegma R1KP-SLR, passes through downwards hydrogenator 15~100 meters of downlink after the feed inlet N1 absolute altitude of the bottom R1K, then to upstream after mixing point KM is mixed with hydrogen logistics H100 In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K.
The present invention, preferably, 3. the down going channel WP of liquid product phegma R1KP-SLR, passes through downwards hydrogenator 25~40 meters of downlink after the feed inlet N1 absolute altitude of the bottom R1K, then to upstream after mixing point KM is mixed with hydrogen logistics H100 In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K.
The present invention can use circulating pump simultaneously, and 3. liquid product phegma R1KP-SLR is by circulation force (forcing) pump boosting The upstream of hydrogenator R1K is flowed up into hydrogenator R1K or entered after mixing afterwards with hydrogen logistics H100 Hydrogenator in.
The present invention, can simultaneously using gas swab, 3. liquid product phegma R1KP-SLR by gas swab QC increasing Enter in hydrogenator R1K after pressure or enter in the hydrogenator of upstream of hydrogenator R1K, gas swab QC is used Power gas be reaction feed gas.
The present invention, can simultaneously using gas swab, 3. liquid product phegma R1KP-SLR by gas swab QC increasing Enter in hydrogenator R1K after pressure or enter in the hydrogenator of upstream of hydrogenator R1K, gas swab QC is used Power gas be reaction feed hydrogen rich gas gas.
The present invention can use Liquid siphon simultaneously, and 3. liquid product phegma R1KP-SLR increases by Liquid siphon LC Enter in hydrogenator R1K after pressure or enter in the hydrogenator of upstream of hydrogenator R1K, Liquid siphon LC is used Power fluid be reaction feed liquid.
Self-running liquid product circulation may be implemented in the present invention, and 3. liquid product phegma R1KP-SLR enters by direct current In hydrogenator R1K or enter in the hydrogenator of upstream of hydrogenator R1K, that is to say, that the process is without using increasing Press equipment.
The present invention, the first hydrogenation process R1 can be selected from a kind or 2 kinds or several of following hydrogenation process Combination:
1. the adding using expanded bed of the logistics containing oil product obtained by middle coalite tar or its distillate or its hot procedure Hydrogen process；Hot procedure is selected from coking or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；
2. the logistics containing oil product obtained by high temperature coal-tar or its distillate or its hot procedure adds hydrogen using expanded bed Process；
3. the hydrogenation process using expanded bed of the logistics containing oil product obtained by shale oil or its distillate or its hot procedure；
4. the hydrogenation process using expanded bed of ethylene cracking tar；
5. the hydrogenation process using expanded bed of the logistics containing oil product obtained by petroleum based heavy fuel oils or its hot procedure；
6. the hydrogenation process using expanded bed of the logistics containing oil product obtained by tar sand base weight oil or its hot procedure；
7. direct hydrogenation liquefaction of coal liquefaction process uses the hydrogenation process of expanded bed, including using the coal of hydrogen supply dissolvent oil to add Hydrogen direct liquefaction liquefaction process, coal refines process to oil altogether, coal faces hydrogen thermosol liquefaction process；
8. the hydrogenation process using expanded bed of liquefaction oil obtained by direct hydrogenation liquefaction of coal liquefaction process；
9. hydrocarbon ils of other aromatic hydrocarbons weight contents higher than 40%, organic nitrogen weight content higher than 0.10% uses expanded bed Hydrogenation process.
The present invention, the first hydrogenation process R1, existing solid particle can 1 kinds or several in following:
1. semicoke particle obtained by direct hydrogenation liquefaction of coal process；
2. catalyst granules；
3. iron rust particle；
4. particles of inorganic material；
5. coking of coal process generate into the solid particle in coal tar；
6. the product solid particle from hydro carbons thermal condensation process；
7. the solid particle from shale；
8. the solid particle from oil-sand；
9. other particles being present in one-stage hydrogenation reaction product BASE-ARP.
The present invention, the first hydrogenation process R1, the expanded bed reactor, mode of operation can be selected from following a kind Or several combination:
1. suspension bed, that is, slurry bed system；
2. ebullated bed；
3. slight expanded-bed.
The present invention, in general, the 1. operating condition of the first hydroconversion process R1 are as follows: temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen/feedstock oil volume ratio are 50~5000.
The present invention, generally, the 1. operating condition of the first hydroconversion process R1 are as follows: temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen/feedstock oil volume ratio are 300~1000, hydrogenation catalyst R1-CAT volume space velocity be 0.05~ 5.0hr-1。
The present invention, the cylinder-shaped length of cylindrical shell sections of hydrogenator R1K, generally 10~45 meters.

Claims (17)

1. a kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases method, it is characterised in that include following step It is rapid:
Hydrogenator R1X is used in the first hydrogenation process R1 of processing feedstock hydrocarbon R1F, hydrogenator R1X is at least Comprising a gas-liquid material upstream hydrogenator R1K, when hydrogenator R1X quantity is more than 1 and is serial operation relationship, On the basis of just being flowed to by the process of raw material R1F, other reactors are located at the upstream or downstream of hydrogenator R1E；
1. in the first hydrogenation process R1, there are hydrogen, hydrocarbon liquid phase simultaneously there may be the mixed phase material items of solid particle Under part, the raw material R1F at least containing carbon and protium enters the first hydrogenation process R1 and carries out the first hydrogenation reaction R1R Obtain the first hydrogenation reaction product BASE-R1P；
Raw material R1F is made of liquid hydrocarbon feeds R1FL and solid particulate materials R1FS that may be present；
May be used simultaneously containing the material of solid particle containing hydrogen, hydrocarbon liquid phase based on the first hydrogenation reaction product BASE-R1P Make the first hydrogenation reaction effluent R1P；
In first hydrogenation process R1, there are hydrogen, hydrocarbon liquid phase, there may be solid particles simultaneously；
First hydrogenation reaction R1R, the hydrofining reaction comprising at least part liquid material R1FL may include at least one Divide the heat from hydrogenation cracking reaction of liquid material R1FL, hydrogen may be added comprising at least part solid material R1FS that may be present Heat cracking reaction；
First hydrogenation process R1 may use catalyst R1C；
First hydrogenation reaction product BASE-R1P, for containing hydrogen, hydrocarbon liquid phase simultaneously may the mixed phase material containing solid particle；
First hydrogenation reaction effluent R1P is same containing hydrogen, hydrocarbon liquid phase for the first hydrogenation reaction product BASE-R1P to be discharged Shi Keneng contains the mixed phase material of solid particle；
First hydrogenation reaction effluent R1P occurs in the form of 1 tunnel or 2 tunnels or multichannel material；
2. gas-liquid material upstream hydrogenator R1K, setting top liquid trap LD；
Gas-liquid material upstream hydrogenator R1K includes lower section, that is, up flow type hydroconversion reaction zone Q1 and upper section, that is, Disengagement zone Q2；Upper section That is Disengagement zone Q2 is made of top liquid trap LD and reactor R1K shell upper section；
In up flow type hydroconversion reaction zone, Q1 obtains product R1KP；
In Disengagement zone Q2, isolates a part of liquid phase in R1KP and obtain liquid product phegma R1KP-LR and net product R1KP- MP；
Liquid product phegma R1KP-SLR, is back in reactor R1K and/or is back to the hydrogenation reaction of the upstream reactor R1K In device R1X, a reflux cycle then is completed with process Flow of Goods and Materials to separate section R1KP-S；
3. along absolute altitude and the bottom direct hydrogenation liquefaction of coal reactor R1K on gas-liquid material upstream hydrogenator R1K, liquid trap LD The elevation difference of absolute altitude is RH；
The down going channel WP of liquid product phegma R1KP-SLR passes through downwards the bottom hydrogenator R1K feed inlet N1 absolute altitude At least the 0.60 of RH times of downlink afterwards, flowed up into after then being mixed with hydrogen logistics H100 in hydrogenator R1K or Into in the hydrogenator of the upstream of hydrogenator R1K.
2. method according to claim 1, it is characterised in that:
3. the down going channel WP of liquid product phegma R1KP-SLR is marked by the bottom hydrogenator R1K feed inlet N1 downwards Then at least 20 meters of downlink after height flow up into hydrogenator after mixing point KM is mixed with hydrogen logistics H100 In R1K or enter in the hydrogenator of upstream of hydrogenator R1K；Using raising the bottom hydrogenator R1K feed inlet Method for arranging of the N1 relative to ground elevation where hydrogenator R1K.
3. method according to claim 1, it is characterised in that:
3. the down going channel WP of liquid product phegma R1KP-SLR is marked by the bottom hydrogenator R1K feed inlet N1 downwards Then at least 20 meters of downlink after height flow up into hydrogenator after mixing point KM is mixed with hydrogen logistics H100 In R1K or enter in the hydrogenator of upstream of hydrogenator R1K；Using reduction mixing point KM relative to hydrogenator The method for arranging of ground elevation where R1K.
4. method according to claim 1, it is characterised in that:
3. the down going channel WP of liquid product phegma R1KP-SLR is marked by the bottom hydrogenator R1K feed inlet N1 downwards Then 15~100 meters of downlink after height flow up into hydrogenator after mixing point KM is mixed with hydrogen logistics H100 In R1K or enter in the hydrogenator of upstream of hydrogenator R1K.
5. method according to claim 1, it is characterised in that:
3. the down going channel WP of liquid product phegma R1KP-SLR is marked by the bottom hydrogenator R1K feed inlet N1 downwards Then 25~40 meters of downlink after height flow up into hydrogenator after mixing point KM is mixed with hydrogen logistics H100 In R1K or enter in the hydrogenator of upstream of hydrogenator R1K.
6. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
3. liquid product phegma R1KP-SLR mixed after circulation force (forcing) pump boosting with hydrogen logistics H100 after to upstream In the dynamic hydrogenator interior or into the upstream of hydrogenator R1K into hydrogenator R1K.
7. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
3. liquid product phegma R1KP-SLR enters in hydrogenator R1K after gas swab QC pressurization or enters plus hydrogen In the hydrogenator of the upstream of reactor R1K, the power gas that gas swab QC is used is reaction feed gas.
8. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
3. liquid product phegma R1KP-SLR enters in hydrogenator R1K after gas swab QC pressurization or enters plus hydrogen In the hydrogenator of the upstream of reactor R1K, the power gas that gas swab QC is used is reaction feed hydrogen rich gas gas.
9. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
3. liquid product phegma R1KP-SLR enters in hydrogenator R1K after Liquid siphon LC pressurization or enters plus hydrogen In the hydrogenator of the upstream of reactor R1K, the power fluid that Liquid siphon LC is used is reaction feed liquid.
10. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
3. liquid product phegma R1KP-SLR enters in hydrogenator R1K or enters hydrogenator R1K's by direct current In the hydrogenator of upstream.
11. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
3. liquid product phegma R1KP-SLR enters in hydrogenator R1K or enters hydrogenator R1K's by direct current In the hydrogenator of upstream, which does not use supercharging equipment.
12. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
(1) first hydrogenation process R1, a kind or 2 kinds or several of the combination selected from following hydrogenation process:
1. the logistics containing oil product obtained by middle coalite tar or its distillate or its hot procedure adds hydrogen mistake using expanded bed Journey；Hot procedure is selected from coking or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；
2. the hydrogenation process using expanded bed of the logistics containing oil product obtained by high temperature coal-tar or its distillate or its hot procedure；
3. the hydrogenation process using expanded bed of the logistics containing oil product obtained by shale oil or its distillate or its hot procedure；
4. the hydrogenation process using expanded bed of ethylene cracking tar；
5. the hydrogenation process using expanded bed of the logistics containing oil product obtained by petroleum based heavy fuel oils or its hot procedure；
6. the hydrogenation process using expanded bed of the logistics containing oil product obtained by tar sand base weight oil or its hot procedure；
7. direct hydrogenation liquefaction of coal liquefaction process uses the hydrogenation process of expanded bed, including using the coal hydrogenation of hydrogen supply dissolvent oil straight Connect liquefaction liquefaction process, oil coal refines process altogether, coal faces hydrogen thermosol liquefaction process；
8. the hydrogenation process using expanded bed of liquefaction oil obtained by direct hydrogenation liquefaction of coal liquefaction process；
9. other aromatic hydrocarbons weight contents are higher than the adding using expanded bed of hydrocarbon ils of 40%, the organic nitrogen weight content higher than 0.10% Hydrogen process.
13. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
(1) first hydrogenation process R1, a kind or several in following of existing solid particle:
1. semicoke particle obtained by direct hydrogenation liquefaction of coal process；
2. catalyst granules；
3. iron rust particle；
4. particles of inorganic material；
5. coking of coal process generate into the solid particle in coal tar；
6. the product solid particle from hydro carbons thermal condensation process；
7. the solid particle from shale；
8. the solid particle from oil-sand；
9. other particles being present in one-stage hydrogenation reaction product BASE-ARP.
14. according to claim 1 or 2 or 3 or 4 or 5 the methods, it is characterised in that:
(1) first hydrogenation process R1, the expanded bed reactor, mode of operation are selected from a kind or several following of combination:
1. suspension bed, that is, slurry bed system；
2. ebullated bed；
3. slight expanded-bed.
15. hydrocarbon hydrogenating conversion process according to claim 2, it is characterised in that:
1. the operating condition of the first hydroconversion process R1 are as follows: temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen Gas/feedstock oil volume ratio is 50~5000.
16. hydrocarbon hydrogenating conversion process according to claim 2, it is characterised in that:
1. the operating condition of the first hydroconversion process R1 are as follows: temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen Gas/feedstock oil volume ratio is 300~1000, hydrogenation catalyst R1-CAT volume space velocity is 0.05~5.0hr-1。
17. hydrocarbon hydrogenating conversion process according to claim 2, it is characterised in that:
The cylinder-shaped length of cylindrical shell sections of hydrogenator R1K is 10~45 meters.
CN201710426072.6A 2017-06-02 2017-06-02 A kind of liquid product reflux power of gas-liquid material upstream hydrogenator increases method Withdrawn CN108970544A (en)

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Publication number Priority date Publication date Assignee Title
CA1196877A (en) * 1981-12-21 1985-11-19 Michael C. Chervenak Coal hydrogenation process having increased solids retention in ebullated bed reactor
CN1258561A (en) * 1999-12-30 2000-07-05 清华大学 Circular tri-phase gas-liquid-solid reactor
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CN104968915A (en) * 2012-08-13 2015-10-07 巴布科克和威尔科克斯能量产生集团公司 Rapid startup heat recovery steam generator
CN105273747A (en) * 2015-11-18 2016-01-27 北京中科诚毅科技发展有限公司 Temperature control measure for slurry bed hydrogenation reactor and design method and application thereof
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Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1196877A (en) * 1981-12-21 1985-11-19 Michael C. Chervenak Coal hydrogenation process having increased solids retention in ebullated bed reactor
CN1258561A (en) * 1999-12-30 2000-07-05 清华大学 Circular tri-phase gas-liquid-solid reactor
CN201190150Y (en) * 2008-03-31 2009-02-04 汉能科技有限公司 Outer circulation reactor
CN104968915A (en) * 2012-08-13 2015-10-07 巴布科克和威尔科克斯能量产生集团公司 Rapid startup heat recovery steam generator
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Application publication date: 20181211