CN105419866A - Method for hydro-conversion of hydrocarbon by using thermal high-pressure separation oil pressure pump - Google Patents
Method for hydro-conversion of hydrocarbon by using thermal high-pressure separation oil pressure pump Download PDFInfo
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- CN105419866A CN105419866A CN201510746198.2A CN201510746198A CN105419866A CN 105419866 A CN105419866 A CN 105419866A CN 201510746198 A CN201510746198 A CN 201510746198A CN 105419866 A CN105419866 A CN 105419866A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
Abstract
The invention discloses a method for hydro-conversion of a hydrocarbon by using a thermal high-pressure separation oil pressure pump. The method is particularly suitable for hydrocarbon hydrogenation processes requiring pressurization of the oil phase of a thermal high-pressure separator, such as a hydro-conversion process of anthracene oil. The method includes the processes that a reaction product R1P of a hydro-conversion process R1 of a raw material hydrocarbon F1 is separated by a thermal high-pressure separator S1 into thermal high-pressure separation gas S1V and thermal high-pressure separation oil S1L, and at least one part S1L1 of the thermal high-pressure separation oil S1L is directly fed into the pressure pump P without a decompression procedure, is pressurized and then returns to the hydro-conversion process R1 or enters a hydrogenation procedure R2 of other pressurization operations. The method has the huge advantages that investment and hydrogen loss can be reduced; power consumption can be lowered; and the operation safety can be improved.
Description
Technical field
The present invention relates to a kind of hydrocarbon hydrogenating conversion process using hot high score oil force (forcing) pump, be particularly suitable for the hydrocarbon hydrogenation process such as carbolineum hydroconversion process that high pressure hot separator oil phase needs pressurization, the reaction product R1P of raw material hydrocarbon F1 hydroconversion process R1 is separated into hot high score gas S1V and hot high score fluid body S1L at high pressure hot separator S1, and hot high score oil S1L1 directly enters without pressure reduction and to return hydroconversion process R1 after topping-up pump P pressurizes and or enter the hydrogenation process R2 of other pressurized operation at least partially.
Background technology
The present invention relates to and use high pressure hot separator and the hydrocarbon hydroconversion process of hot high score oil require pressure treatment, such as use high pressure hot separator and the carbolineum hydroconversion process of hot high score oil require pressurization.
The hydrogenation process of carbolineum Hydrogenation fine-quality diesel oil cut, comprises unifining process and hydrocracking process usually.
Cold high score flow process is not selected in the sepn process of carbolineum unifining process reaction effluent R1P usually, this is because the hydrofining of carbolineum generates the density of density close to water of oil, if carbolineum unifining process reaction effluent note wash-down water, be cooled to 40 ~ 50 DEG C after directly enter in cold high pressure separator and carry out Oil, Water, Gas separation, oil-water separation is very poor.
Hot high score flow process is selected in the sepn process of carbolineum unifining process reaction effluent usually, the high pressure hot separator S1 that first carbolineum unifining process reaction effluent enters thermal high separate part THPS be separated into primarily of the hot high score oil S1L of high boiling point, high-density hydrocarbon composition and on volume primarily of the hot high score gas S1V comprising lower boiling, low density hydrocarbon of hydrogen composition; At cold anticyclone separate part HPS, hot high score gas S1V notes wash-down water, be cooled to 40 ~ 50 DEG C after enter in cold high pressure separator S2 and carry out Oil, Water, Gas separation, due to density and the water of cold high score oil density difference comparatively greatly, oil-water separation is fine.Now, if hot high score oil enters the higher hydrocracking process of working pressure just need pressurization.
Carbolineum unifining process, in order to reduce density of aromatic hydrocarbon and the organonitrogen concentration of stock oil, hydrofining can be adopted to generate the method for oil circulation dilution, in order to reduce the thermosteresis that turning oil working cycle is formed, reasonable manner adopts thermal cycling oil, namely use hot high score oil as thinning oil, as a kind of anthracene oil hydrogenation method that number of patent application is 200910187908.7, number of patent application is the method for hydrogen cracking of a kind of deep drawing anthracene oil of 200910187922.7, like this in order to return the higher operating upstream unit of working pressure, just need the pressurization of hot high score oil.
The hydrocarbon hydroconversion process that the present invention relates to, feature is that its reaction product R1P is separated into hot high score gas S1V and hot high score fluid body S1L at high pressure hot separator S1, just can enter hydroconversion process R1 at least partially and or enter the hydrogenation process R2 of other pressurized operation after the pressurization of hot high score oil require.
The method for hydrogen cracking that the method that number of patent application is a kind of producing light fuel oil by hydrogenating anthracene oil of 200910187909.1, number of patent application are the carbolineum of 200910187906.8, number of patent application are the method for a kind of producing lightweight fuel oil by hydrogenation of deep drawn anthracene oil of 200910187923.1, do not describe carbolineum hydrofining reaction product separation method in detail, do not illustrate that high score oil returns the pressure method of carbolineum hydrofining reaction process yet.
Current carbolineum hydrogenation unit, the mode that the hot high score oil of unifining process reaction effluent R1P enters the hydrogenation process of high top pressure operation has:
1. the hot high score oil of carbolineum hydrofining reaction product separation gained directly enters the hydrocracking process of working pressure lower than unifining process; Its shortcoming is, in order to ensure the working pressure of hot high score oil hydrocracking reaction process, the pressure of carbolineum hydrofining reaction process must be improved, namely in order to improve the working pressure of hot high score oil, the working pressure that improve whole carbolineum hydrofining high-pressure process causes construction investment to increase considerably, lose more than gain, along with the increase of unit scale, the increase of construction investment volume is surprising;
2. enter light pressure separator after the step-down of carbolineum hydrofining reaction product separation gained hot high score oil and be separated into heat low point of gas and heat low point of oil, heat low point of oil enters carbolineum unifining process R1 and or enters hot high score oil hydrocracking process R2 after force (forcing) pump supercharging.
The method for hydrogen cracking that a kind of anthracene oil hydrogenation method that number of patent application is 200910187908.7, number of patent application are a kind of deep drawing anthracene oil of 200910187922.7, all use thermal low-pressure separators, cause a large amount of material consumptions, energy consumption and once invest increase on the one hand, cause potential safety hazard on the one hand, be embodied in following shortcoming:
1. hydrogen loss is dissolved: enter after the step-down of hot high score oil and carry out gas-liquid separation in heat low point of device and obtain heat low point of gas and heat low point of oil, major part dissolving hydrogen gasification in high score oil enters in low point of gas and forms hydrogen loss, even if the separated purification Posterior circle of hydrogen adds hydrogenation process in heat low point of gas, also will increase energy consumption, form hydrogen loss;
2. the hot high score oil pressure loss of energy: enter the heat low point of device mineralization pressure loss of energy after the step-down of hot high score oil, such as working pressure is that the hot high score oil of 16.5MPa reduces pressure to enter working pressure be heat low point of device Amplitude of Hypotensive of 2.5MPa is 14.0MPa, and the oily pump pressure process of low point of heat exists huge power consumption;
3. high-power high lift pump and corollary system thereof are invested huge;
4. the handoff procedure poor stability of high-power high lift pump, maintenance cost is high.
In order to solve this problem, the object of the invention is to propose a kind of hydrocarbon hydrogenating conversion process using hot high score oil force (forcing) pump, thermal low-pressure separators is not set, the feed surge tank of special hot high score oil force (forcing) pump is not set yet, be particularly suitable for the hydrocarbon hydrogenation process such as carbolineum hydroconversion process that high pressure hot separator liquid phase needs pressurization, the reaction product R1P of raw material hydrocarbon F1 hydroconversion process R1 is separated into hot high score gas S1L and hot high score fluid body S1L at high pressure hot separator S1, hot high score oil S1L1 directly enters without pressure reduction and to return hydroconversion process R1 after topping-up pump P pressurizes and or enter the hydrogenation process of other pressurized operation at least partially.
Summary of the invention
A kind of hydrocarbon hydrogenating conversion process using hot high score oil force (forcing) pump of the present invention, is characterized in that:
1. at the first hydroconversion process R1, under hydrogen and hydrogenation catalyst existence condition, raw material hydrocarbon HDS completes the first hydroconversion reactions and is converted into the first hydrogenation reaction product R1P;
2. at thermal high sepn process THPS, in high pressure hot separator S1, first hydrogenation reaction product R1P is separated into hot high score gas S1V and hot high score oil S1L, high pressure hot separator S1 internal space comprises the epimere space S 1-U possessing gas-liquid separating function and the hypomere space S 1-D being used as hot high score oil cushioning pocket, hot high score oil S1L1 enters after topping-up pump P pressurizes at least partially becomes supercharging hot high score oil S1L1P, at least partially supercharging hot high score oil S1L1P return the first hydroconversion process R1 and or enter the second hydroconversion process R2 of the hot high score oil of processing; The residual heat high score oil S1L2 that recovery may exist;
3. at cold anticyclone sepn process HPS, in cold high pressure separator S2, heat of dissociation high score gas S1V obtains cold high score oil S2L and primarily of the cold high score gas S2V of hydrogen composition on volume, and cold high score gas S2V returns the first hydroconversion process R1 and recycles at least partially.
Hydrocarbon hydrogenating conversion process of the present invention, hydrocarbon feed HDS can be selected from one or more in following materials:
1. coalite tar or its distillate or its hot procedure gained oil product;
2. coal-tar middle oil or its distillate or its hot procedure gained oil product;
3. coal-tar heavy oil or its distillate or its hot procedure gained oil product;
4. coal liquefaction gained liquefied coal coil or its distillate or its hot procedure gained oil product;
5. shale oil or its distillate or its hot procedure gained oil product;
6. tar sand basic weight oil or its hot procedure gained oil product;
7. petroleum base wax oil thermal cracking tars;
8. petroleum based heavy fuel oils hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;
9. other polycyclic aromatic hydrocarbons concentration higher than 10%, aromatic hydrocarbons total content higher than 40% hydrocarbon ils.
Hydrocarbon hydrogenating conversion process of the present invention, operational condition is generally:
1. the operational condition of the first hydroconversion process R1 is: temperature is 170 ~ 460 DEG C, pressure is 4.0 ~ 28.0MPa, hydrogen/stock oil volume ratio is 50 ~ 5000, hydrogenation catalyst R1-CAT volume space velocity is 0.05 ~ 5.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 100 ~ 400 DEG C, pressure is 3.6 ~ 27.6MPa.
Hydrocarbon hydrogenating conversion process of the present invention, operational condition is generally:
1. the operational condition of the first hydroconversion process R1 is: temperature is 230 ~ 420 DEG C, pressure is 12.0 ~ 20.0MPa, hydrogen/stock oil volume ratio is 50 ~ 2500, hydrogenation catalyst R1-CAT volume space velocity is 0.15 ~ 2.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 200 ~ 370 DEG C, pressure is 11.6 ~ 19.6MPa.
Hydrocarbon hydrogenating conversion process of the present invention, operational condition is preferably:
1. the operational condition of the first hydroconversion process R1 is: temperature is 250 ~ 400 DEG C, pressure is 15.0 ~ 18.0MPa, hydrogen/stock oil volume ratio is 50 ~ 2500, hydrogenation catalyst R1-CAT volume space velocity is 0.15 ~ 2.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 300 ~ 370 DEG C, pressure is 14.6 ~ 17.6MPa.
The gangway pressure reduction of topping-up pump P of the present invention: be usually less than 3.0MPa, be generally less than 1.0MPa.
Hydrocarbon hydrogenating conversion process of the present invention, the residence time of the charging high score oil S1L of topping-up pump P: be generally 15 ~ 120 minutes, be generally 15 ~ 60 minutes.
Hydrocarbon hydrogenating conversion process of the present invention, topping-up pump P-structure form is canned-motor pump.
Hydrocarbon hydrogenating conversion process of the present invention, the partial boost that usual topping-up pump P exports hot high score oil S1L1PR returns in high pressure hot separator S1 as topping-up pump P phegma.
Hydrocarbon hydrogenating conversion process of the present invention, usual hot high score oil S1L1 directly enters topping-up pump P without depressurization step.
Embodiment
A kind of hydrocarbon hydrogenating conversion process using hot high score oil force (forcing) pump of the present invention, is characterized in that:
1. at the first hydroconversion process R1, under hydrogen and hydrogenation catalyst existence condition, raw material hydrocarbon HDS completes the first hydroconversion reactions and is converted into the first hydrogenation reaction product R1P;
2. at thermal high sepn process THPS, in high pressure hot separator S1, first hydrogenation reaction product R1P is separated into hot high score gas S1V and hot high score oil S1L, high pressure hot separator S1 internal space comprises the epimere space S 1-U possessing gas-liquid separating function and the hypomere space S 1-D being used as hot high score oil cushioning pocket, hot high score oil S1L1 enters after topping-up pump P pressurizes at least partially becomes supercharging hot high score oil S1L1P, at least partially supercharging hot high score oil S1L1P return the first hydroconversion process R1 and or enter the second hydroconversion process R2 of the hot high score oil of processing; The residual heat high score oil S1L2 that recovery may exist;
3. at cold anticyclone sepn process HPS, in cold high pressure separator S2, heat of dissociation high score gas S1V obtains cold high score oil S2L and primarily of the cold high score gas S2V of hydrogen composition on volume, and cold high score gas S2V returns the first hydroconversion process R1 and recycles at least partially.
Hydrocarbon hydrogenating conversion process of the present invention, hydrocarbon feed HDS can be selected from one or more in following materials:
1. coalite tar or its distillate or its hot procedure gained oil product;
2. coal-tar middle oil or its distillate or its hot procedure gained oil product;
3. coal-tar heavy oil or its distillate or its hot procedure gained oil product;
4. coal liquefaction gained liquefied coal coil or its distillate or its hot procedure gained oil product;
5. shale oil or its distillate or its hot procedure gained oil product;
6. tar sand basic weight oil or its hot procedure gained oil product;
7. petroleum base wax oil thermal cracking tars;
8. petroleum based heavy fuel oils hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;
9. other polycyclic aromatic hydrocarbons concentration higher than 10%, aromatic hydrocarbons total content higher than 40% hydrocarbon ils.
Hydrocarbon hydrogenating conversion process of the present invention, operational condition is generally:
1. the operational condition of the first hydroconversion process R1 is: temperature is 170 ~ 460 DEG C, pressure is 4.0 ~ 28.0MPa, hydrogen/stock oil volume ratio is 50 ~ 5000, hydrogenation catalyst R1-CAT volume space velocity is 0.05 ~ 5.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 100 ~ 400 DEG C, pressure is 3.6 ~ 27.6MPa.
Hydrocarbon hydrogenating conversion process of the present invention, operational condition is generally:
1. the operational condition of the first hydroconversion process R1 is: temperature is 230 ~ 420 DEG C, pressure is 12.0 ~ 20.0MPa, hydrogen/stock oil volume ratio is 50 ~ 2500, hydrogenation catalyst R1-CAT volume space velocity is 0.15 ~ 2.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 200 ~ 370 DEG C, pressure is 11.6 ~ 19.6MPa.
Hydrocarbon hydrogenating conversion process of the present invention, operational condition is preferably:
1. the operational condition of the first hydroconversion process R1 is: temperature is 250 ~ 400 DEG C, pressure is 15.0 ~ 18.0MPa, hydrogen/stock oil volume ratio is 50 ~ 2500, hydrogenation catalyst R1-CAT volume space velocity is 0.15 ~ 2.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 300 ~ 370 DEG C, pressure is 14.6 ~ 17.6MPa.
The gangway pressure reduction of topping-up pump P of the present invention: be usually less than 3.0MPa, be generally less than 1.0MPa.
Hydrocarbon hydrogenating conversion process of the present invention, the residence time of the charging high score oil S1L of topping-up pump P: be generally 15 ~ 120 minutes, be generally 15 ~ 60 minutes.
Hydrocarbon hydrogenating conversion process of the present invention, topping-up pump P-structure form is canned-motor pump.
Hydrocarbon hydrogenating conversion process of the present invention, the partial boost that usual topping-up pump P exports hot high score oil S1L1PR returns in high pressure hot separator S1 as topping-up pump P phegma.
Hydrocarbon hydrogenating conversion process of the present invention, usual hot high score oil S1L1 directly enters topping-up pump P without depressurization step.
Hot high score oil force (forcing) pump P of the present invention, can be the reliable pump of any one performance safety, can be centrifugal pump or positive-displacement pump, such as canned-motor pump, surge pump; If latter stage at plant running initial stage, the pressure difference of hot high score oil force (forcing) pump P changed greatly, hot high score oil force (forcing) pump P pump group can configure frequency variable speed-adjusting mechanism to save the overcurrent flow of power consumption and stable pump.
The combination of high pressure hot separator S1 of the present invention and hot high score oil force (forcing) pump P, simplify device structure, optimize technological operation, as compared to using the technique of thermal low-pressure separators and heat low point of oily force (forcing) pump, major advantage shows as:
1. dissolving hydrogen loss is avoided;
2. avoid insignificant Pressure Drop, avoid insignificant huge power consumption;
3. low head pump and corollary system less investment thereof;
4. the handoff procedure security of low head pump is high, and maintenance cost is low.
The present invention is suitable for new device or existing apparatus transformation.
Claims (12)
1. use a hydrocarbon hydrogenating conversion process for hot high score oil force (forcing) pump, it is characterized in that:
1. at the first hydroconversion process R1, under hydrogen and hydrogenation catalyst existence condition, raw material hydrocarbon HDS completes the first hydroconversion reactions and is converted into the first hydrogenation reaction product R1P;
2. at thermal high sepn process THPS, in high pressure hot separator S1, first hydrogenation reaction product R1P is separated into hot high score gas S1V and hot high score oil S1L, high pressure hot separator S1 internal space comprises the epimere space S 1-U possessing gas-liquid separating function and the hypomere space S 1-D being used as hot high score oil cushioning pocket, hot high score oil S1L1 enters after topping-up pump P pressurizes at least partially becomes supercharging hot high score oil S1L1P, at least partially supercharging hot high score oil S1L1P return the first hydroconversion process R1 and or enter the second hydroconversion process R2 of the hot high score oil of processing; The residual heat high score oil S1L2 that recovery may exist;
3. at cold anticyclone sepn process HPS, in cold high pressure separator S2, heat of dissociation high score gas S1V obtains cold high score oil S2L and primarily of the cold high score gas S2V of hydrogen composition on volume, and cold high score gas S2V returns the first hydroconversion process R1 and recycles at least partially.
2. hydrocarbon hydrogenating conversion process according to claim 1, is characterized in that one or more that hydrocarbon feed HDS is selected from following materials:
1. coalite tar or its distillate or its hot procedure gained oil product;
2. coal-tar middle oil or its distillate or its hot procedure gained oil product;
3. coal-tar heavy oil or its distillate or its hot procedure gained oil product;
4. coal liquefaction gained liquefied coal coil or its distillate or its hot procedure gained oil product;
5. shale oil or its distillate or its hot procedure gained oil product;
6. tar sand basic weight oil or its hot procedure gained oil product;
7. petroleum base wax oil thermal cracking tars;
8. petroleum based heavy fuel oils hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;
9. other polycyclic aromatic hydrocarbons concentration higher than 10%, aromatic hydrocarbons total content higher than 40% hydrocarbon ils.
3. hydrocarbon hydrogenating conversion process according to claim 2, is characterized in that:
1. the operational condition of the first hydroconversion process R1 is: temperature is 170 ~ 460 DEG C, pressure is 4.0 ~ 28.0MPa, hydrogen/stock oil volume ratio is 50 ~ 5000, hydrogenation catalyst R1-CAT volume space velocity is 0.05 ~ 5.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 100 ~ 400 DEG C, pressure is 3.6 ~ 27.6MPa.
4. hydrocarbon hydrogenating conversion process according to claim 2, is characterized in that:
1. the operational condition of the first hydroconversion process R1 is: temperature is 230 ~ 420 DEG C, pressure is 12.0 ~ 20.0MPa, hydrogen/stock oil volume ratio is 50 ~ 2500, hydrogenation catalyst R1-CAT volume space velocity is 0.15 ~ 2.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 200 ~ 370 DEG C, pressure is 11.6 ~ 19.6MPa.
5. hydrocarbon hydrogenating conversion process according to claim 2, is characterized in that:
1. the operational condition of the first hydroconversion process R1 is: temperature is 250 ~ 400 DEG C, pressure is 15.0 ~ 18.0MPa, hydrogen/stock oil volume ratio is 50 ~ 2500, hydrogenation catalyst R1-CAT volume space velocity is 0.15 ~ 2.0hr
-1;
2. high pressure hot separator S1 operational condition is: temperature is 300 ~ 370 DEG C, pressure is 14.6 ~ 17.6MPa.
6. hydrocarbon hydrogenating conversion process according to claim 2, is characterized in that: the gangway pressure reduction of topping-up pump P is less than 3.0MPa.
7. hydrocarbon hydrogenating conversion process according to claim 2, is characterized in that: the gangway pressure reduction of topping-up pump P is less than 1.0MPa.
8. hydrocarbon hydrogenating conversion process according to claim 2, the residence time of the charging high score oil S1L of topping-up pump P is 15 ~ 120 minutes.
9. hydrocarbon hydrogenating conversion process according to claim 2, the residence time of the charging high score oil S1L of topping-up pump P is 15 ~ 60 minutes.
10. hydrocarbon hydrogenating conversion process according to claim 2, topping-up pump P-structure form is canned-motor pump.
11. hydrocarbon hydrogenating conversion process according to claim 2, the partial boost that topping-up pump P exports hot high score oil S1L1PR returns in high pressure hot separator S1 as topping-up pump P phegma.
12. hydrocarbon hydrogenating conversion process according to claim 2, hot high score oil S1L1 directly enters topping-up pump P without depressurization step.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510746198.2A CN105419866A (en) | 2015-11-03 | 2015-11-03 | Method for hydro-conversion of hydrocarbon by using thermal high-pressure separation oil pressure pump |
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| CN201510746198.2A CN105419866A (en) | 2015-11-03 | 2015-11-03 | Method for hydro-conversion of hydrocarbon by using thermal high-pressure separation oil pressure pump |
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| CN105419866A true CN105419866A (en) | 2016-03-23 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110437876A (en) * | 2019-07-11 | 2019-11-12 | 洛阳瑞华新能源技术发展有限公司 | The method in hydrocarbon material expansion bed hydroprocessing intermediate product thermal release air cooling Hou Qu downstream hydrogenation area |
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