CN1064700C - Separation method for oil generated from hydrogen conversion process of hydrocarbon - Google Patents
Separation method for oil generated from hydrogen conversion process of hydrocarbon Download PDFInfo
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- CN1064700C CN1064700C CN98112925A CN98112925A CN1064700C CN 1064700 C CN1064700 C CN 1064700C CN 98112925 A CN98112925 A CN 98112925A CN 98112925 A CN98112925 A CN 98112925A CN 1064700 C CN1064700 C CN 1064700C
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- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 210
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 210
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 210
- 238000000034 method Methods 0.000 title claims abstract description 113
- 230000008569 process Effects 0.000 title claims abstract description 78
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 32
- 238000000926 separation method Methods 0.000 title claims abstract description 18
- 239000001257 hydrogen Substances 0.000 title claims description 38
- 229910052739 hydrogen Inorganic materials 0.000 title claims description 38
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims description 37
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims description 188
- 239000003381 stabilizer Substances 0.000 claims description 36
- 238000010521 absorption reaction Methods 0.000 claims description 26
- 239000000203 mixture Substances 0.000 claims description 18
- 239000003795 chemical substances by application Substances 0.000 claims description 17
- 241000282326 Felis catus Species 0.000 claims description 15
- 239000002283 diesel fuel Substances 0.000 claims description 12
- 230000002745 absorbent Effects 0.000 claims description 11
- 239000002250 absorbent Substances 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 10
- 239000003350 kerosene Substances 0.000 claims description 8
- 229910052717 sulfur Inorganic materials 0.000 claims description 7
- 239000003208 petroleum Substances 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 239000012467 final product Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 22
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 9
- 239000006096 absorbing agent Substances 0.000 abstract description 4
- 230000000087 stabilizing effect Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 56
- 239000000047 product Substances 0.000 description 15
- 239000002994 raw material Substances 0.000 description 11
- 230000000694 effects Effects 0.000 description 8
- 239000003502 gasoline Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 238000005336 cracking Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 238000005194 fractionation Methods 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000002407 reforming Methods 0.000 description 3
- 230000006641 stabilisation Effects 0.000 description 3
- 238000011105 stabilization Methods 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 239000001993 wax Substances 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- -1 H 2O Inorganic materials 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000012084 conversion product Substances 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000004058 oil shale Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a separation method of generated oil in a hydrogenation conversion process of hydrocarbons, which is especially suitable for a hydrocracking process. In the method, a C3<+> hydrocarbon in C3<+> hydrocarbon enriched gas can be simultaneously recovered. The generated oil is evaporated in a flash mode at reduced pressure into first gas and first hydrocarbon liquid; the first hydrocarbon liquid after being mixed with first C3<+> hydrocarbon enriched gas is divided into second gas and second hydrocarbon liquid; the second gas as second C3<+> hydrocarbon enriched gas is divided into third gas and a rich absorbing agent after the second gas is mixed with a hydrocarbon oil absorbing agent, and the second hydrocarbon liquid and the rich absorbing agent are divided into tower bottom heavy hydrocarbon liquid, tower top light hydrocarbon liquid and tower top gas in a stabilizing tower; the top gas is circularly used as the first C3<+> hydrocarbon enriched gas. The present invention can be used for improving the recovery rate of the C3<+> hydrocarbon in the C3<+> hydrocarbon enriched gas.
Description
The invention belongs to separation method for oil generated from hydrogen conversion process of hydrocarbon, relate to and be the method for gas, stabilization heavy hydrocarbon streams and lighter hydrocarbons logistics with described generation is separating of oil, particularly utilize hydrocarbon hydrogenating conversion process generate oily logistics for absorption agent reclaims rich C
3 +Hydrocarbon (C
3And C
3Above heavy hydrocarbon) C in the gas
3 +The method of hydrocarbon relates to simultaneously and is hydrogen-rich gas, rich CH with described generation is separating of oil
4, C
2H
6The method of gas, stabilization heavy hydrocarbon streams and lighter hydrocarbons logistics, the present invention is the improvement to the described method of Chinese patent ZL93106265.9.
As everyone knows, hydrocarbon hydrogenating conversion process is the hydroconversion process of hydrocarbon feed under catalyzer and hydrogen existence condition, and the leading reaction of this process is the reaction of consumption hydrogen, and generally speaking, most hydrocarbons hydrogenation processes are exothermic process of consumption hydrogen.Here said hydrocarbon hydrogenating conversion process, its raw material hydrocarbon can be the hydro carbons from oil or coal or oil shale, the cut scope of described hydro carbons from gasoline, kerosene, diesel oil, wax oil up to residual oil, and above-mentioned raw materials sulfur-bearing all in most cases.Processes such as above-mentioned hydroconversion process comprises that usually said hydrocracking, hydrogenating desulfurization, hydrodenitrification, aromatic hydrogenation are saturated, hydroisomerization and hydrodemetallation (HDM), wherein hydrocracking is a kind of important hydroconversion process, it is a raw material with gasoline, kerosene, diesel oil, wax oil and residual oil, be widely used in production liquefied petroleum gas (LPG), catalytic reforming raw material, high-quality intermediate oil, cracking ethylene raw material, WHITE OIL PRODUCTION raw material and lubricated wet goods, be a kind of method of utilizing wax oil or residual oil to obtain the high-quality intermediate oil, widely use.The present invention mainly is based on hydrocracking process, yet this is not to limit Application Areas of the present invention, and the present invention can also be widely used in above-mentioned other hydroconversion process such as hydrodesulfurization process.
The wax oil hydrogenation cracking is the excellent means of production high-quality boat coal and low freezing point diesel fuel, in the hydrocracking reaction part, in reactor, contact with hydrogen make-up from the external wax oil of device with catalyzer, be generally 5.0～30.0MPa at pressure, be generally under the reaction conditions of 5.0～20.0MPa, finish hydrogenation reaction, the reaction effluent autoreactor flows out.The reaction pressure of some other hydrocarbon hydrogenating conversion process is low, is generally 0.7～5.0MPa, is generally 1.4～5.0MPa.Usually contain impurity composition such as H
2S, NH
3, H
2O, HCl are also mainly by H
2, C
5 +Hydrocarbon (C
5And C
5Above heavy hydrocarbon) and conventional gas hydrocarbon (C
1, C
2, C
3, C
4Hydrocarbon) the described hydrocracking reaction effluent of Zu Chenging is after condensation, being cooled to certain temperature; usually sneak into wash-down water; mixture enters a gas-liquid separator that is referred to as high-pressure separator usually after further condensation, cooling then; at this, the hydrocracking reaction effluent is separated into high-pressure separator gas, hydrocracking process generates oil and the high-pressure separator sour water logistics of existence usually.Described high-pressure separator gas turns back to hydrogenator as circulation gas and recycles, and discharges a part of high-pressure separator gas sometimes.Described sour water logistics disacidify water treatment device.The hydrocarbon conversion product of hydrocracking has substantially all entered hydrocracking process and has generated in the oil, and hydrocracking process generates the oily H that some hydrogen make-up are brought that also dissolved simultaneously
2, this is because described high-pressure separator is being generally 25～90 ℃, is being generally the result who operates under the pressure condition of 30～65 ℃ temperature and 5.0～20.0MPa.
Usually, described hydrocracking process forms the logistics of a gas, liquid mixed phase after generating oil process energy recovery turbine or dropping valve step-down, and described mixed phase logistics enters a gas-liquid separator that is referred to as light pressure separator usually and is dissolved in the H that generates in the oil to separate a sucking-off part
2, C
1And C
2Hydrocarbon is that 0.5～2.7MPa, temperature are generally 25～90 ℃, are generally under 30～65 ℃ the operational condition at pressure, is separated on volumetric concentration mainly by H
2, C
1, C
2The light pressure separator gas that hydrocarbon is formed and mainly by C
3 +The light pressure separator hydrocarbon liquid that hydrocarbon is formed.Common described light pressure separator gas contains H
2S is so need through taking off H
2The S treatment unit takes off H
2Just can go the fuel gas pipe network to make fuel or go device for producing hydrogen to make raw material behind the S.Contain most of C that hydrocracking process produces
3, C
4The high-temperature product logistics heat exchange of the light pressure separator hydrocarbon liquid of hydrocarbon and described reaction effluent or this device enters a separation column that is referred to as stabilizer tower or debutanizing tower or depentanizer or de-hydrogen sulfide column usually after heating up, at pressure is under the operational condition of 0.5～2.7MPa, be separated into heavy hydrocarbon streams at the bottom of an overhead gas, the logistics of cat head lighter hydrocarbons and the tower, the effect of this tower is C in the heavy hydrocarbon streams at the bottom of the restriction tower
4 -Hydrocarbon (C
4And C
4Following lighter hydrocarbons) content.Under aforesaid operational condition, do not reclaiming C in the overhead gas
3, C
4In the generation oil separating method that includes light pressure separator and stabilizer tower of hydrocarbon, low pressure is separated C in the gas
3 +The volumetric concentration of hydrocarbon is than C in stabilizer tower overhead gas, deethanizer overhead gas, the depropanizing tower overhead gas
3 +Low many of hydrocarbon volumetric concentration lowly divide H in the gas
2Concentration is higher, H
2Molecular amounts and CH
4, C
2H
6The ratio of molecular amounts is higher, C
3, C
4Hydrocarbon concentration is lower.The component that flows out the stabilizer tower cat head enters gas-liquid separator so that two overhead products to be provided after condensation, cooling.The logistics of cat head lighter hydrocarbons is mainly by C
3, C
4Hydrocarbon is formed and directly or through deethanizing column is taken off C usually
2 -(C
1And C
2Hydrocarbon) takes off H behind the hydrocarbon
2S handles and finally carries out fractionation to obtain propane fraction and butane cut.Heavy hydrocarbon streams is mainly by C at the bottom of the tower
5 +Hydrocarbon is formed and is entered the fractionation is made up of one or more separation columns usually partly it is divided into narrow fraction oil product such as petroleum naphtha, kerosene, diesel oil and wax oil etc.Described stabilizer tower is formed and the stabilizer tower operational condition according to light pressure separator hydrocarbon liquid, sometimes by total reflux operation, does not have the logistics of cat head lighter hydrocarbons this moment.Subject to the foregoing, C in the stabilizer tower overhead gas
3 +Hydrocarbon (mainly is C
3, C
4Hydrocarbon) content can reach 40～90% (weight), and the overhead gas flow is generally 0.7～7.0% (weight) of device material quantity or higher, and this has caused the influence of two aspects: reduced C on the one hand
3, C
4Hydrocarbon liquids recovery rate; On the other hand, take off H because of hydroconversion process hydrocarbon gas product
2S handles and typically uses the organic amine aqueous solution is that absorption agent is finished under certain condition for validity, and the hydrocarbon gas that hydroconversion process is discharged is taking off H
2Can aggravate the foaming tendency of amine desulfurization solvent in the S process, influence the stably manufactured of sweetening process, and can cause sour gas (H
2S gas) contain more hydro carbons in, finally influence the sulfur recovery facility quality product as causing the sulphur blackout.For processing the higher wax oil of sulphur content or the hydrocracking process of residual oil, above-mentioned situation is even more serious.At present, coastal area of china, riverine petroleum chemical plant processing high-sulfur oils quantity just further increase.
United States Patent (USP) U.S.P4551238 relates to a kind of separation method for oil generated from hydrogen conversion process that does not use separation column, its objective is hydroconversion process is generated separating of oil be dry gas and stabilization oil product.
Chinese patent ZL93101645.2 relates to C in a kind of recovery hydrocracking stabilizer tower overhead gas
3, C
4The method of hydrocarbon, its major technique feature is: use the hydro carbons absorption agent to reclaim C in the overhead gas in the absorption tower
3 +Hydrocarbon, rich absorbent leave the absorption tower and remove described stabilizer tower desorb, the C in the rich absorbent
3, C
4Hydrocarbon finally enters in the overhead hydrocarbon liquid product and is recovered, and the absorber component in the rich absorbent enters at the bottom of the tower in the oil.
Chinese patent ZL93106265.9 relates to and a kind ofly utilizes hydrocarbon hydrogenating conversion process to generate oily logistics to reclaim C in the described hydroconversion process stabilizer tower overhead gas as absorption agent
3, C
4The method of hydrocarbon, its prominent feature are to utilize the C of the generation oil logistics in the hydroconversion process flow process
3 +The hydrocarbon receptivity absorbs, and finishes removal process then in stabilizer tower, has that flow process is simple, absorption agent number change scope is big, and removal process does not influence outstanding advantages such as stablizing at the bottom of the Tata heavy hydrocarbon streams sepn process, and its major technique feature is: contain H
2, H
2S, C
4 -Hydrocarbon and C
5 +Be mixed into mixture with circulation gas after the generation oil step-down of the hydrocarbon hydrogenating conversion process of hydrocarbon, described mixture enters light pressure separator, be to be separated into light pressure separator gas and light pressure separator hydrocarbon liquid under the operational condition of 0.5～2.7MPa at pressure, described light pressure separator gas goes out device, light pressure separator hydrocarbon liquid enter in the stabilizer tower that working pressure is 1.0～2.3MPa and be separated into tower at the bottom of heavy hydrocarbon streams, logistics of cat head lighter hydrocarbons and overhead gas, at least a portion overhead gas returns described light pressure separator, the C in the circulation gas after mixing as the oil of the generation after circulation gas and the step-down
3, C
4Hydrocarbon is absorbed and finally enters in stabilizer tower in the logistics of cat head lighter hydrocarbons by light pressure separator hydrocarbon liquid and is recovered.
Hydroconversion process generates C in the oil herein
3, C
4The hydrocarbon rate of recovery is defined as C in lighter hydrocarbons logistics and the heavy hydrocarbon streams
3, C
4Hydrocarbon molecule is counted sum and is generated C in the oil
3, C
4The ratio of hydrocarbon molecule number.
In the described method of patent ZL93106265.9, the hydrocarbon hydrogenating conversion process of gas-liquid mixed phase generate oil with overhead gas mixings contact separation process in, from the olefiant gas composition of hydrocarbon hydrogenating conversion process life to C
3, C
4The removal process of hydrocarbon has played the C of gas phase in the mixture that reduces contact
3, C
4The effect of hydrocarbon volumetric concentration, thereby reduced the impellent of absorption process and reduced the rate of recovery, particularly when generating H in the oil
2, C
1, C
2The hydrocarbon component more for a long time, above-mentioned effect is more obvious.Simultaneously, played the H of gas phase in the living olefiant mixture of the hydrocarbon hydrogenating conversion process that reduces contact from the gas composition of overhead gas
2The effect of volumetric concentration, promptly overhead gas has played H in the reduction light pressure separator gas
2The effect of concentration is unfavorable for containing H
2The further recovery of gas.Owing to generating oily logistics, hydrocarbon hydrogenating conversion process itself contains a certain amount of C again
3, C
4Therefore hydrocarbon and gasoline component, contain certain C in the absorption process expellant gas
3 +Hydrocarbon and gasoline component do not reach higher C
3 +The hydrocarbon rate of recovery.Again on the one hand, the described method of patent ZL93106265.9, when its light pressure separator working pressure was higher, the selectivity of removal process was lower.One of purpose of the present invention is to improve C
3 +The hydrocarbon rate of recovery and selectivity.
Two of purpose of the present invention is, is improving C
3 +In the time of the hydrocarbon rate of recovery, with H in the described generation oil
2, C
1, C
2The hydrocarbon component is separated into hydrogen-rich gas and rich C
1, C
2Gas.
For the technical scheme that reaches the separation method for oil generated from hydrogen conversion process of hydrocarbon that above-mentioned purpose the present invention adopts comprises following steps: (1) contains H
2, H
2S, C
4 -Hydrocarbon and C
5 +It is first gas and the first hydrocarbon liquid that the generation oil of the hydrocarbon hydrogenating conversion process of hydrocarbon enters the first separate part step-down flash separation, and the operational condition of described first separate part is: temperature is 20～95 ℃, and pressure is 0.7～5.1MPa; (2) the described first hydrocarbon liquid and the first rich C
3 +The appropriate hydrocarbon gas contact mixes, and mixture flow is separated into second gas and the second hydrocarbon liquid at second separate part, and the operational condition of described second separate part is: temperature is 20～95 ℃, and pressure is 0.4～5.0MPa; (3) described second gas of at least a portion enters step (4) as the second rich C
3 +Appropriate hydrocarbon gas is used; (4) second rich C
3 +Appropriate hydrocarbon gas contacts mixing with the hydrocarbon ils absorption agent, and mixture flow is separated into the 3rd gas and rich absorbent at the 3rd separate part, and the operational condition of described the 3rd separate part is: temperature is 20～95 ℃, and pressure is 0.5～5.0MPa; (5) the described second hydrocarbon liquid, rich absorbent enter stabilizer tower, and stabilizer tower is separated into charging mainly by C
5 +Heavy hydrocarbon liquid at the bottom of the tower that hydrocarbon is formed is mainly by C
3, C
4Cat head light hydrocarbon liquid and overhead gas that hydrocarbon is formed, the operational condition of described stabilizer tower is: tower top pressure is 0.5～2.7MPa, tower top temperature is 55～120 ℃; (6) the described overhead gas of at least a portion returns step (2) as the first rich C
3 +Appropriate hydrocarbon gas is used.
Also be for its feature of technique scheme: described hydrocarbon ils absorption agent can be gasoline, kerosene, diesel oil and mixing oil thereof, preferably kerosene, diesel oil and mixing oil thereof.
Be for its further technical characterictic of technique scheme: described first, second rich C
3 +Appropriate hydrocarbon gas also comprises the C that contains of other device in hydrocracking device deethanizer overhead gas or depropanizing tower overhead gas or the petroleum chemical plant
3 +Gas, or the mixed gas of above-mentioned two or more gases, or above-mentioned gas take off H
2After handling, S removes H
2The gas of S.
Also be for its further technical characterictic of technique scheme: the working pressure of first separate part of described step (1) can guarantee make the not compressed supercharging of first gas get final product final scope as device for producing hydrogen unstripped gas or the use of hydrogen concentration unit unstripped gas.
Unusual effect of the present invention is:
In the present invention, what stablize the overhead gas contact is the first hydrocarbon liquid of gained after the flash liberation of first separate part process, thereby under the identical operations pressure condition, can improve and stablize overhead gas is the C in the gas phase in the first hydrocarbon liquid contact process with degassing generation oil
3 +Volumetric concentration improves C
3 +The hydrocarbon rate of recovery.In order further to reclaim C in second gas
3 +Hydrocarbon reclaims C in second gas with the hydrocarbon ils absorption agent
3 +Hydrocarbon has further improved the rate of recovery.Simultaneously, with H in the described generation oil
2, C
1, C
2The hydrocarbon component is separated into first gas and the 3rd gas, H in first gas
2Concentration is higher to be hydrogen-rich gas, C in the 3rd gas
1, C
2Hydrocarbon concentration is higher to be rich C
1, C
2Gas.
On the other hand, hydrocarbon hydrogenating conversion process is discharged contains C
3 +Appropriate hydrocarbon gas also has deethanizer overhead gas or depropanizing tower overhead gas except that stablizing overhead gas, and C wherein
3 +Hydrocarbon concentration is higher, can reach 75～90% (weight), also can be used as the C that contains of contact process
3 +Hydrocarbon feed gases.Also can be with the C that contains of other device discharging
3 +Appropriate hydrocarbon gas is introduced hydrocarbon hydrogenating conversion process and is reclaimed wherein C
3 +Hydrocarbon.Such as, the machinery that a cover is made of wax oil hydrogenation cracking unit, device for producing hydrogen, diesel oil hydrofining device, naphtha reforming device fully can be with the C that contains of diesel oil hydrofining device and the discharging of wax oil hydrogenation cracking unit
3 +Appropriate hydrocarbon gas puts together, and carries out C at hydroeracking unit
3 +Reclaim.The present invention can realize this point, can will stablize overhead gas rich C in addition according to the present invention
3 +Appropriate hydrocarbon gas is as first, second rich C
3 +Appropriate hydrocarbon gas has been incorporated in the whole recovery process, has further utilized the receptivity that generates oily logistics, has improved C
3 +The hydrocarbon yield.
At present, along with comprehensive utilization, sometimes with H to hydroconversion process hydrogen-containing gas product
2The higher hydrocarbon gas of content takes off H
2After S handled, compressed machine supercharging went working pressure to be generally 0.8～4.5MPa, be generally chemical method device for producing hydrogen such as the lighter hydrocarbons reforming hydrogen manufacturing of 1.0～3.5MPa or hydro carbons dry gas reforming hydrogen manufacturing device is made unstripped gas or go working pressure to be generally 0.8～4.0MPa, be generally 1.0～3.5MPa pressure-swing absorption apparatus or go working pressure to be not less than the membrane separation device of 2.0～5.0MPa to reclaim H wherein
2Component.Sometimes after converging, all lighter hydrocarbons dry gas of hydrocracking device generation take off H
2S handles, and takes off H
2Dry gas removes to do the device for producing hydrogen raw material or hydrogen is carried dense raw material behind the S.And the pressure of hydrogenation unit stabilizer tower is generally 1.0～1.8MPa, and gas takes off H
2Pressure is reduced to 0.8～1.6MPa behind the S, and dry gas just must compressed machine supercharging before entering the device for producing hydrogen conversion process like this.In said process, some dry gas such as light pressure separator gas, deethanizing cat head gas, depropanizing cat head gas have experienced the unreasonable process of boosting after the first step-down.The invention provides the means that overcome this shortcoming, can improve C by selecting the pressure of the first suitable sepn process according to the present invention
3 +In the time of the hydrocarbon rate of recovery, guarantee that first gas can directly connect as device for producing hydrogen unstripped gas or the use of hydrogen recovery unit unstripped gas without compressor boost.
Be described in detail technology contents of the present invention below in conjunction with accompanying drawing, accompanying drawing is just in order to illustrate that substance of the present invention draws, it does not limit content of the present invention and type of service, in fact according to the concrete operations condition, need on some pipelines to be provided with as conventional equipment or piping elements such as compressor, pump, interchanger, process furnace, mixing tank, dropping valves.
As shown in Figure 1, the hydrocarbon hydrogenating conversion process of described composition forms gas after generating oily step-down, liquid mixed phase thing flowing pipe 1 enters in first separator 2 and carries out the step-down flash distillation, on volumetric concentration mainly by H
2, CH
4, C
2H
6That forms contains H
2First gas of S leaves first separator 2 through managing 3, mainly by C
3 +The first hydrocarbon liquid that hydrocarbon is formed goes in second separator 7 through managing 4.In above-mentioned sepn process, generate the most of H in the oil
2By desorb.First gas finally uses as device for producing hydrogen unstripped gas or hydrogen recovery unit unstripped gas usually.As an example, the operational condition of first separator is: temperature is 20～95 ℃, and pressure is 0.7～5.1MPa; Be preferably: temperature is 30～55 ℃, and pressure is 2.0～4.0MPa.Especially, the working pressure of first separator should be able to guarantee that the not compressed supercharging of first gas can be finally as device for producing hydrogen unstripped gas or the use of hydrogen concentration unit unstripped gas.
As shown in Figure 1, the first hydrocarbon liquid through manage 4 with through managing 5 and the first rich C that comes
3 +Appropriate hydrocarbon gas is mixed into mixture, and mixture enters in second separator 7, mainly by C through managing 6
3 +The second hydrocarbon liquid that hydrocarbon is formed goes in the stabilizer tower 15 through managing 25, in above-mentioned mixing contact separation process, and the first rich C
3 +C in the appropriate hydrocarbon gas
3 +Hydrocarbon is absorbed, on volumetric concentration mainly by CH
4, C
2H
4, H
2That forms contains H
2Second gas of S leaves second separator 7 through managing 8.As an example, the operational condition of second separator is generally: temperature is 20～95 ℃, and pressure is 0.4～5.0MPa; Be preferably: temperature is 30～55 ℃, and pressure is 0.5～2.7MPa.Recommend the working pressure of second separator to be lower than the working pressure of first separator.
As shown in Figure 1, the present invention is provided with the hydrocarbon ils absorption process of second gas, and second gas that at least a portion is come along pipe 9 is as the second rich C
3 +Appropriate hydrocarbon gas is mixed with the hydrocarbon ils absorption agent that comes along pipe 10, mixes the mixture that forms to enter the 3rd separator 12 along pipe 11, and is separated into the 3rd gas and rich absorbent, and shown in the figure is that whole second gases are as the second rich C
3 +Appropriate hydrocarbon gas enters the situation of the 3rd separator 12.The 3rd gas enters subsequent disposal as finally entering the fuel gas pipe network as the dry gas product usually.Rich absorbent enters in the stabilizer tower 15 along pipe 14, to reclaim the C in the rich absorbent
3, C
4Hydrocarbon, absorption agent component and other C
5 +Hydrocarbon, the absorption agent component after the recovery can recycle.As an example, the operational condition of the 3rd separator is: temperature is 20～95 ℃, and pressure is 0.5～5.0MPa; Be preferably: temperature is 30～55 ℃, and pressure is 0.80～2.0MPa.Described hydrocarbon ils absorption agent: can be gasoline, kerosene, diesel oil and mixing oil thereof.The molecular amounts of described hydrocarbon ils absorption agent and the second rich C
3 +C in the appropriate hydrocarbon gas
3 +The ratio of the molecular amounts of hydrocarbon component: be generally 1～4.
As shown in Figure 1, the second hydrocarbon liquid enters stabilizer tower 15 middle parts through managing 25.Contain C
3, C
4The steam effluent of hydrocarbon is through managing 16, entering behind the condensate cooler 17, pipe 18 and carry out gas-liquid separation in the return tank of top of the tower 19, mainly by C
3, C
4The overhead hydrocarbon liquid that hydrocarbon is formed leaves return tank 19 from return tank 19 bottoms through managing 20, and a part is returned stabilizer tower 15 tops through managing 21 as trim the top of column, and a part is left return tank 19 as cat head lighter hydrocarbons thing flowing pipe 22 and removed deethanizing column or liquefied gas separation column.Mainly by C
5 +Oil leaves stabilizer tower 15 bottoms through managing 23 at the bottom of the tower that hydrocarbon is formed, and going the fractionation part is narrow fraction oil product such as petroleum naphtha, kerosene, diesel oil and wax oil etc. with the fractionation.Contain a large amount of C
3, C
4The overhead gas of hydrocarbon leaves return tank 19 through managing 24 from return tank 19 tops.The operating method of stabilizer tower 15 can be that reboiler furnace at the bottom of bottom reboiler or the tower is set, and also can be the water steam stripped.Stabilizer tower is debutanizing tower or depentanizer or takes off H
2S tower, the effect of this tower are C in the heavy hydrocarbon streams at the bottom of the restriction tower
4 -The content of hydrocarbon, its operational condition is according to material component situation and separation requirement decision.As an example, stabilizer tower is tray column or packing tower, and the plate number is 8～50, and feed plate is positioned at tower middle part or top.As an example, the operational condition of stabilizer tower is: tower top pressure is 0.5～2.7MPa, preferably 0.8～2.0MPa; Tower top temperature is 55～120 ℃, and column bottom temperature is mainly by by C in the raw material
3 +Hydrocarbon is formed decision, and it is bigger to form variation with raw material, is generally 200～330 ℃, and the trim the top of column temperature is generally 35～45 ℃; Trim the top of column is 1～15 than (weight ratio of quantity of reflux and overhead product total amount).
As shown in Figure 1, with at least a portion overhead gas as the first rich C
3 +Appropriate hydrocarbon gas is mixed with the first hydrocarbon liquid and contact to returning second separator 7 behind the mixture with the C in the recovery overhead gas through managing 5
3, C
4Hydrocarbon, shown in the figure is that whole overhead gases are as the first rich C
3 +The situation of appropriate hydrocarbon gas.
It should be noted that for accompanying drawing 1 any is, particular case according to second separator, 7 working pressures and stabilizer tower 15 working pressures, need on relevant pipeline, be provided with compressor (not expressing among the figure) with or pump (not expressing among the figure) is set on relevant pipeline, about this point, the those of skill in the art in present technique field are easy to judge and make decision.The flow process pressure condition of recommending is: stabilizer tower 15 tower top pressures are higher than second separator, 7 pressure.
The used hydrocarbon ils absorption agent of the present invention can be provided by hydrocracking device or outer device, but provides more stable, convenient by the hydrocracking device, and does not influence this device product quality.
As shown in Figure 1, also can be by pipe 26 with other rich C
3 +Appropriate hydrocarbon gas is as the first rich C
3 +Appropriate hydrocarbon gas is incorporated into second separator 7 or/and through managing 27 with other rich C
3 +Appropriate hydrocarbon gas is as the second rich C
3 +Appropriate hydrocarbon gas is incorporated in the 3rd separator 12 to reclaim C wherein
3 +Hydrocarbon, described other rich C
3 +Appropriate hydrocarbon gas can be in hydrocracking device deethanizer overhead gas or depropanizing tower overhead gas or the petroleum chemical plant other device contain C
3 +Being suitable for of hydrocarbon, reclaimed wherein C at the hydrocracking device
3 +The gas of hydrocarbon also can be the mixed gas of above-mentioned gas, can also be the H that takes off of above-mentioned gas
2After handling, S removes H
2The gas of S, according to the difference in its source, the representative condition of its composition, temperature, pressure sees Table 1:
Table 1 hydroconversion process discharging gas typical case forms and operational condition
| Gas | Pressure MPa | Temperature ℃ | C 3 +Hydrocarbon content % (volume) |
| Hydrocracking device discharging gas | Scope 0.5～1.6 | 30～65 | 15～35 |
| Stablize overhead gas | Scope 0.6～2.2 | 35～45 | 20～50 |
| Deethanizing cat head gas | Scope 2.8～3.5 | 35～45 | 30～70 |
| Depropanizing cat head gas | Scope 2.8～3.5 | 35～45 | 30～70 |
Obviously, first separator 2, second separator 7 in the flow process shown in the accompanying drawing 1, the 3rd separator 12 also can be for including the separate part of one or more gas-liquid separators, " separate part " speech should be broadly construed, for example, it can be the separate part that includes conventional equipments such as water cooler, compressor, pump, gas-liquid separator.
Accompanying drawing and drawing explanation:
Accompanying drawing 1: be typical process synoptic diagram of the present invention.
Embodiment:
Certain refinery processing power is 100 * 10
4T/a wax oil hydrogenation treatment unit, year running 8000 hours, generate oil separating by the inventive method, its main operational condition sees Table 2, under the situation of the various schemes that table 3 to table 7 has been listed in the table 2 respectively to be mentioned, generate the oil recovery result, listed file names with device in the table 2 and do not established C in the stabilizer tower overhead gas
3, C
4Hydrocarbon recvery facility and employing ZL93106265.9 method are carried out C in the overhead gas
3, C
4The operational condition of each scheme that hydrocarbon reclaims.In the design of present embodiment, the hydroconversion process hydrogen-rich gas finally goes transformation absorption hydrogen retrieving arrangement to make unstripped gas and be separated into hydrogen and fuel gas, rich C
1, C
2Appropriate hydrocarbon gas enters the fuel gas pipe network, and the hydrogen-rich gas device terminal pressure condition of requirement is not less than 3.2MPa, and the fuel gas price is 750 yuan/ton, C
3, C
4Hydrocarbon finally is recovered as liquefied gas, and its price is 1730 yuan/ton, C
5 +Be recovered as price and be 1850 yuan/ton light naphthar.External gas described in the table 2 is the hydrocarbon gas product of this refinery one cover diesel oil hydrofining device.
Compare as can be seen with scheme 2 from scheme 3: adopt patent ZL93106265.9 method, improve overhead gas and generate the pressure that oil contacts, greatly reduce the absorption process selectivity, scheme 3 is compared with scheme 2, stablizes cat head tolerance and has increased by 250% (molecule).
Compare as can be seen with scheme 3 from scheme 4: adopt the present invention, improved the absorption process selectivity, stablize cat head tolerance 45% (molecule) that descended, while C
3, C
4The hydrocarbon yield has improved 1.3% (molecule).Hydrogen molecule percentage ratio has brought up to 75% by 62% in the hydrogen-rich gas product.
Table 8 has been listed scheme listed in the table 24, scheme 5 is compared C with scheme 1
3 +The increment of hydrocarbon yield and value thereof, as can be seen, with C in the recovery overhead gas
3 +The conventional scheme of hydrocarbon is compared, the C that adopts the solution of the present invention 4, scheme 5 to be reclaimed
3 +The value of hydrocarbon increases by 2,607 ten thousand yuan/year, 3,233 ten thousand yuan/year respectively.
Table 9 has been listed scheme listed in the table 24, scheme 5 is compared C with scheme 2
3 +The increment of hydrocarbon yield and value thereof as can be seen, are compared the scheme 4 that adopts the present invention program, the C that scheme 5 is reclaimed with patent ZL93106265.9 method
3 +The value of hydrocarbon increases by 1,299 ten thousand yuan/year and 1,925 ten thousand yuan/year respectively.
As can be seen in each goes into operation year, value of the present invention is considerable from table 8, table 9.Above-mentioned this numerical value is not considered the investment and the process cost that should increase, yet it is seldom that the investment of increase is compared with above-mentioned value of the present invention with process cost.Above-mentioned analysis does not consider to use other good effect of bringing behind the present invention yet.
The main operational condition table of table 2
| The scheme numbering | 1 | 2 | 3 | 4 | 5 | |
| The scheme explanation | Do not reclaim C in the overhead gas 3 +Hydrocarbon | Adopt patent ZL93106265.9 | Adopt the inventive method | |||
| Main operational condition | First separator temperature ℃ pressure MPa | 45 2.1 | 45 3.5 | 45 3.5 | ||
| Second separator temperature ℃ pressure MPa | 45 1.5 | 45 3.5 | 45 1.5 | 45 1.5 | ||
| The 3rd separator temperature ℃ pressure MPa | 40 1.3 | 40 1.3 | ||||
| Stabilizer tower tower top pressure MPa tower top temperature ℃ column bottom temperature ℃ return tank temperature ℃ | 1.65 76 250 40 | 1.65 75 250 40 | 1.65 72 250 40 | 1.65 73 250 40 | 1.65 72 250 40 | |
| Generate C in the oil 3、C 4Hydrocarbon rate of recovery % molecule | 77.5 | 87.4 | 92.7 | 94.0 | 97.8 | |
| Main streams flow rate kgmol/h | Generate oily external gas absorbent heavy hydrocarbon streams lighter hydrocarbons logistics first gas second gas the 3rd gas tower overhead gas | 2165.86 1420.00 324.46 283.41 136.50 | 2165.86 1420.00 371.24 373.21 116.55 | 2165.86 1422.50 400.31 340.97 408.59 | 2165.86 40 1461.00 414.23 230.64 110.22 98.07 223.21 | 2165.86 68.00 60 1481.00 439.16 230.64 161.19 141.02 280.37 |
Table is formed in 1 logistics of table 3 scheme
| Form kgmol/h | The pipe Taoist monastic name | ||||
| 1 | 3 | 24 | 22 | 23 | |
| H 2O | 3.35 | 0.94 | 0.63 | 0.29 | |
| H 2S | 54.99 | 9.74 | 21.43 | 23.82 | |
| H 2 | 212.11 | 191.74 | 19.51 | 0.86 | |
| C 1 | 74.56 | 44.01 | 24.38 | 6.17 | |
| C 2 | 28.22 | 7.58 | 10.60 | 10.04 | |
| C 3 | 114.38 | 12.44 | 27.56 | 74.37 | 0.01 |
| iC 4 | 185.68 | 9.08 | 24.86 | 147.30 | 4.44 |
| nC 4 | 69.88 | 2.58 | 6.74 | 53.16 | 7.40 |
| C 5 + | 1422.69 | 5.30 | 0.79 | 8.45 | 1408.15 |
| Add up to | 2165.86 | 283.41 | 136.50 | 324.46 | 1420.00 |
Table is formed in 2 logistics of table 4 scheme
| Form kgmol/h | The pipe Taoist monastic name | ||
| 8 | 22 | 23 | |
| H 20 | 1.62 | 0.32 | |
| H 2S | 21.46 | 33.53 | |
| H 2 | 211.40 | 0.71 | |
| C 1 | 67.82 | 6.74 | |
| C 2 | 15.17 | 13.05 | |
| C 3 | 24.69 | ?89.69 | |
| iC 4 | 17.13 | 164.92 | 3.63 |
| nC 4 | 4.78 | ?57.28 | 7.82 |
| C 5 + | 9.14 | 5.00 | 1408.55 |
| Amount to | 373.21 | 371.24 | 1420.00 |
Table is formed in 3 logistics of table 5 scheme
| Form kgmol/h | The pipe Taoist monastic name | ||
| 8 | 22 | 23 | |
| H 2O | 0.93 | 0.34 | |
| H 2S | 17.27 | 37.72 | |
| H 2 | 211.42 | 0.69 | |
| C 1 | 67.51 | 7.05 | |
| C 2 | 13.04 | 15.18 | |
| C 3 | 15.62 | 98.75 | 0.01 |
| iC 4 | 8.95 | 172.65 | 4.08 |
| nC 4 | 2.33 | 60.21 | 7.34 |
| C 5 + | 3.90 | 7.72 | 1411.07 |
| Amount to | 340.97 | 400.31 | 1422.50 |
Table is formed in 4 logistics of table 6 scheme
| Form kgmol/h | The pipe Taoist monastic name | ||||
| 3 | 10 | 13 | 22 | 23 | |
| H 2O | 0.53 | 0.55 | 0.35 | ||
| H 2S | 5.35 | 7.53 | 42.11 | ||
| H 2 | 173.58 | 38.23 | 0.30 | ||
| C 1 | 31.10 | 34.69 | 8.77 | ||
| C 2 | 4.41 | 6.35 | 17.46 | ||
| C 3 | 6.72 | 6.19 | 101.46 | 0.01 | |
| iC 4 | 4.81 | 2.65 | 174.24 | 3.98 | |
| nC 4 | 1.36 | 0.61 | 60.91 | 7.00 | |
| C 5 + | 2.78 | 40 | 1.27 | 8.63 | 1450.01 |
| Add up to | 230.64 | 40 | 98.07 | 414.23 | 1461.00 |
Table is formed in 5 logistics of table 7 scheme
| Form kgmol/h | The pipe Taoist monastic name | ||||
| 10 | 13 | 22 | 23 | 27 | |
| H 2O | 0.80 | 0.38 | 0.30 | ||
| H 2S | 12.12 | 44.45 | 6.93 | ||
| H 2 | 46.89 | 0.23 | 8.59 | ||
| C 1 | 50.86 | 8.10 | 15.50 | ||
| C 2 | 14.11 | 25.42 | 15.72 | ||
| C 3 | 9.80 | 109.94 | 0.01 | 12.09 | |
| iC 4 | 3.80 | 176.79 | 3.82 | 3.54 | |
| nC 4 | 0.89 | 64.34 | 6.92 | 3.63 | |
| C 5 + | 60 | 1.84 | 9.51 | 1470.25 | 1.69 |
| Add up to | 60 | 141.02 | 439.16 | 1481.00 | ?67.99 |
Table 8 C
3 +Hydrocarbon yield increment and value table
| Component | Reference scheme is a scheme 1 | Scheme 4 increments | Scheme 5 increments | ||
| kgmol/h | kgmol/h | t/a | kgmol/h | t/a | |
| C 3 | Benchmark (74.38) | 27．09 | 9556 | 35．57 | 12547 |
| C 4 | Benchmark (212.30) | 33．83 | 15730 | 39．57 | 18398 |
| C 5 +(with C 5Meter) | Benchmark (1416.60) | 2．04 | 1178 | 3．16 | 1824 |
| Ten thousand yuan/year of values of the product | Benchmark | Benchmark+2607 | Benchmark+3233 | ||
Table 9 C
3 +Hydrocarbon yield increment and value table
| Component | Reference scheme is a scheme 2 | Scheme 4 increments | Scheme 5 increments | ||
| kgmol/h | kgmol/h | t/a | kgmol/h | t/a | |
| C 3 | Benchmark (89.69) | 11．78 | 4155 | 20．26 | 7146 |
| C 4 | Benchmark (233.65) | 12．48 | 5802 | 18．22 | 8471 |
| C 5 +(with C 5Meter) | Benchmark (1413.55) | 5．09 | 2938 | 6．21 | 3584 |
| Ten thousand yuan/year of values of the product | Benchmark | Benchmark+1299 | Benchmark+1925 | ||
Claims (13)
1, a kind of separation method for oil generated from hydrogen conversion process of hydrocarbon is characterized in that: may further comprise the steps:
(1) contains H
2, H
2S, C
4 -Hydrocarbon and C
5 +It is first gas and the first hydrocarbon liquid that the generation oil of the hydrocarbon hydrogenating conversion process of hydrocarbon enters the first separate part step-down flash separation, and the operational condition of described first separate part is: temperature is 20～95 ℃, and pressure is 0.7～5.1MPa;
(2) the described first hydrocarbon liquid and the first rich C
3 +The appropriate hydrocarbon gas contact mixes, and mixture flow is separated into second gas and the second hydrocarbon liquid at second separate part, and the operational condition of described second separate part is: temperature is 20～95 ℃, and pressure is 0.4～5.0MPa;
(3) described second gas of at least a portion enters step (4) as the second rich C
3 +Appropriate hydrocarbon gas is used;
(4) second rich C
3 +Appropriate hydrocarbon gas contacts mixing with the hydrocarbon ils absorption agent, and mixture flow is separated into the 3rd gas and rich absorbent at the 3rd separate part, and the operational condition of described the 3rd separate part is: temperature is 20～95 ℃, and pressure is 0.5～5.0MPa;
(5) the described second hydrocarbon liquid, rich absorbent enter stabilizer tower, and stabilizer tower is separated into charging mainly by C
5 +Heavy hydrocarbon liquid at the bottom of the tower that hydrocarbon is formed is mainly by C
3, C
4Cat head light hydrocarbon liquid and overhead gas that hydrocarbon is formed, the operational condition of described stabilizer tower is: tower top pressure is 0.5～2.7MPa, tower top temperature is 55～120 ℃:
(6) the described overhead gas of at least a portion returns step (2) as the first rich C
3 +Appropriate hydrocarbon gas is used.
2, according to the described method of claim 1, it is characterized in that: described hydrocarbon ils absorption agent is kerosene, diesel oil and mixing oil thereof.
3, according to the described method of claim 1, it is characterized in that: described first, second rich C
3 +Appropriate hydrocarbon gas also comprises the C that contains of other device in hydrocracking device deethanizer overhead gas or depropanizing tower overhead gas or the petroleum chemical plant
3 +Gas, or the mixed gas of above-mentioned two or more gases, or above-mentioned gas take off H
2After handling, S removes H
2The gas of S.
4, according to the described method of claim 1, it is characterized in that: the working pressure of first separate part of described step (1) guarantees make the not compressed supercharging of first gas get final product final scope as device for producing hydrogen unstripped gas or the use of hydrogen concentration unit unstripped gas.
5, according to the described method of claim 1, it is characterized in that: the working pressure of described step (4) stabilizer tower cat head is higher than the working pressure of second separate part of described step (2).
6, according to the described method of claim 1, it is characterized in that: the working pressure of second separate part of described step (2) is lower than the working pressure of first separate part of described step (1).
According to the described method of claim 1, it is characterized in that 7, the stabilizer tower of described step (4) is hydrocracking device debutanizing tower or depentanizer or takes off H
2The S tower.
8, according to the described method of claim 1, it is characterized in that: the first separate part operational condition of described step (1) is: temperature is 30～55 ℃, and pressure is 2.0～4.0MPa.
9, according to claim 1 described method, it is characterized in that: the operational condition of second separate part of described step (2) is: temperature is 30～55 ℃, and pressure is 0.5～2.7MPa.
10, according to the described method of claim 1, it is characterized in that: the working pressure of the stabilizer tower cat head of described step (4) is 0.8～2.0MPa.
11, according to the described method of claim 1, it is characterized in that: the described hydrocarbon ils absorption agent and the second rich C
3 +C in the appropriate hydrocarbon gas
3 +The molecular ratio of hydrocarbon component is 1～4.
12, according to the described method of claim 1, it is characterized in that: the operational condition of described the 3rd separate part is: temperature is 30～55 ℃, and pressure is 0.8～2.0MPa.
13, according to the described method of claim 1, it is characterized in that: the generation oil of described hydroconversion process is meant the generation oil of hydrocracking process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98112925A CN1064700C (en) | 1998-07-16 | 1998-07-16 | Separation method for oil generated from hydrogen conversion process of hydrocarbon |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98112925A CN1064700C (en) | 1998-07-16 | 1998-07-16 | Separation method for oil generated from hydrogen conversion process of hydrocarbon |
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| CN1209451A CN1209451A (en) | 1999-03-03 |
| CN1064700C true CN1064700C (en) | 2001-04-18 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98112925A Expired - Fee Related CN1064700C (en) | 1998-07-16 | 1998-07-16 | Separation method for oil generated from hydrogen conversion process of hydrocarbon |
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| CN111393250B (en) * | 2019-05-10 | 2022-11-18 | 中国石化工程建设有限公司 | Light hydrocarbon separation device and method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1036600A (en) * | 1988-03-31 | 1989-10-25 | 国际壳牌研究有限公司 | The separation method of hydroprocessed effluent streams |
| CN1074928A (en) * | 1993-02-20 | 1993-08-04 | 中国石化洛阳石油化工工程公司 | Hydroeracking unit C 3, C 4The recovery method of hydrocarbon |
| CN1160748A (en) * | 1996-03-21 | 1997-10-01 | 中国石油化工总公司石油化工科学研究院 | Separation method of catalytically converted hydrocarbon product |
-
1998
- 1998-07-16 CN CN98112925A patent/CN1064700C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1036600A (en) * | 1988-03-31 | 1989-10-25 | 国际壳牌研究有限公司 | The separation method of hydroprocessed effluent streams |
| CN1074928A (en) * | 1993-02-20 | 1993-08-04 | 中国石化洛阳石油化工工程公司 | Hydroeracking unit C 3, C 4The recovery method of hydrocarbon |
| CN1160748A (en) * | 1996-03-21 | 1997-10-01 | 中国石油化工总公司石油化工科学研究院 | Separation method of catalytically converted hydrocarbon product |
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