CN1027819C - Method for recovery of C3 and C4 hydrocarbons from overhead gas in hydrotreating process - Google Patents
Method for recovery of C3 and C4 hydrocarbons from overhead gas in hydrotreating process Download PDFInfo
- Publication number
- CN1027819C CN1027819C CN 93106265 CN93106265A CN1027819C CN 1027819 C CN1027819 C CN 1027819C CN 93106265 CN93106265 CN 93106265 CN 93106265 A CN93106265 A CN 93106265A CN 1027819 C CN1027819 C CN 1027819C
- Authority
- CN
- China
- Prior art keywords
- hydrocarbon
- gas
- pressure separator
- stabilizer tower
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a recovery method of C3 hydrocarbon and C4 hydrocarbon of overhead gas in a hydrotreatment process of hydrocarbon, which is particularly suitable for recovering C3 and C4 of overhead gas in a hydrocracking process. Hydrocarbon liquid obtained in a high-pressure separator in the hydrotreatment process depressurized, enters a low-pressure separator, and is divided into gas and hydrocarbon liquid which enters a stabilizer and is divided into overhead gas, overhead light-hydrocarbon material flow and tower-bottom heavy-hydrocarbon material flow, and then the overhead gas used as recycle gas contacts and is mixed with charging materials in the low-pressure separator, and then returns to the low-pressure separator to recover the C3 hydrocarbon and the C4 hydrocarbon in the recycle gas. The present invention has the advantages that the present invention can increase the recovery rate of the C3 hydrocarbon and the C4 hydrocarbon in the hydrotreatment process, and has simple process flow.
Description
The invention belongs to hydrocarbons hydrogenation treating processes C
3, C
4The recovery of hydrocarbon relates generally to C in the hydrocarbons hydrogenation treating processes stabilizer tower overhead gas
3, C
4The recovery of hydrocarbon.
As everyone knows, the hydrocarbons hydrogenation treating processes is the hydroconversion process of hydrocarbon feed under catalyzer and hydrogen existence condition, and the leading reaction of this process is the thermopositive reaction of consumption hydrogen, and generally speaking, the hydrocarbons hydrogenation process is the exothermic process of consumption hydrogen.Here said hydrocarbons hydrogenation treating processes, 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.Above-mentioned hydrotreatment process comprises processes such as usually said hydrocracking, hydrogenating desulfurization, hydrodenitrification and hydrodemetallation (HDM), wherein hydrocracking is a kind of important hydrotreatment 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 hydrotreatment process such as hydrodesulfurization process.
As everyone knows, 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 the catalyzer with hydrogenating function of nickeliferous (Ni) component, at pressure is under the reaction conditions of 7.5～20.0MPa, finish hydrogenation reaction, the reaction effluent autoreactor flows out.The reaction pressure of some other hydrocarbons hydrogenation treating processes is low, is generally 1.4～7.5MPa.Usually, contain H
2S, NH
3, H
2O, H
2, C
+ 5Hydrocarbon and conventional gas hydrocarbon (C
1, C
2, C
3, C
4Hydrocarbon) described hydrocracking reaction effluent enters a gas-liquid separator that is referred to as high-pressure separator usually after condensation, cooling, at this, the hydrocracking reaction effluent is separated into high-pressure separator gas, high-pressure separator hydrocarbon liquid and the logistics of high-pressure separator sour water, described high-pressure separator gas turns back to hydrocracking reactor as circulation gas and recycles, described sour water logistics disacidify water treatment device.The hydrocarbon conversion product of hydrocracking has all entered in the high-pressure separator hydrocarbon liquid, and high-pressure separator hydrocarbon liquid has also dissolved the H that some hydrogen make-up are brought simultaneously
2, this is because the result that described high-pressure separator is operated under the pressure condition of 30～65 ℃ temperature and 5.0～18.0MPa usually.Usually high-pressure separator hydrocarbon liquid forms the logistics of a gas, liquid mixed phase after through 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 H in the high-pressure separator hydrocarbon liquid to separate a sucking-off part
2, CH
4And C
2H
6, be that 0.5～2.7MPa, temperature are under 30～65 ℃ the operational condition at pressure, be separated into mainly by H
2, CH
4, C
2H
6The light pressure separator gas of forming and mainly by C
+ 3The 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 0.5～1.9MPa, be separated into heavy hydrocarbon streams at the bottom of a stabilizer tower overhead gas, stabilizer tower cat head lighter hydrocarbons logistics and the stable Tata, the effect of this tower is C in the heavy hydrocarbon streams at the bottom of the restriction tower
- 4The content of hydrocarbon.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.Described stabilizer tower overhead gas is mainly by H
2And C
- 4Hydrocarbon is formed, and usually through taking off H
2S makes fuel after handling, and the logistics of described stabilizer tower cat head lighter hydrocarbons is mainly by C
3, C
4Hydrocarbon is formed and directly or through deethanizing column is taken off C usually
- 2Take off H behind the hydrocarbon
2S handles and finally carries out fractionation to obtain propane fraction and butane cut, and heavy hydrocarbon streams is mainly by C at the bottom of the described stable Tata
+ 5Hydrocarbon is formed and is entered a fractionation part of being made up of one or more separation columns usually it is divided into narrow product oil product such as petroleum naphtha, kerosene, diesel oil and the wax oil etc. of heating up in a steamer.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
+ 3Hydrocarbon (mainly is C
3, C
4Hydrocarbon) content reaches 40～90%(weight), the overhead gas flow is generally 0.7～7.0%(weight of device material quantity) or higher, this has caused the influence of two aspects: reduced C on the one hand
3, C
4Hydrocarbon liquids recovery rate; Cause C in the hydrocarbon gas that the hydrotreatment process is discharged on the other hand
3The content of hydrocarbon is higher, and contains a large amount of C
+ 3The gas of hydrocarbon 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.And purpose of the present invention just is being to manage to reclaim the C in the described stabilizer tower overhead gas
3, C
4Hydrocarbon is to avoid the problems referred to above.
About C in the existing hydrocarbon gas
3, C
4The recovery method of hydrocarbon generally is a solvent absorption, and it is to finish the recovery purpose in independent, a complete absorption desorption system of being made up of equipment such as absorption tower and desorption towers.U.S. Pat P4673488 discloses a kind of hydrocarbon conversion process that is different from described hydrocarbons hydrogenation treating processes, and its main purpose is recover hydrogen, lighter hydrocarbons and heavy hydrocarbon from the reaction effluent of hydrocarbon conversion process that produces hydrogen such as hydro carbons catforming process.In patent USP4673488, partial condensation contain H
2, C
- 4Hydrocarbon and C
+ 5The reaction effluent of the hydrocarbon conversion process of the product hydrogen of hydrocarbon enters first gas-liquid separator and is separated into first hydrogen-containing gas and the first hydrocarbon liquid, a part first hydrogen-containing gas recycles as circulating hydrogen dereaction device after compression, another part first hydrogen-containing gas contacts as equilibrium hydrogen successively compressed machine supercharging and water cooler cooling back and the first hydrocarbon liquid after the pump supercharging and is mixture, to absorb the lighter hydrocarbons in the gas, described mixture enters in second gas-liquid separator and is separated into second hydrogen-containing gas and the second hydrocarbon liquid, and the working pressure of second gas-liquid separator is than the working pressure height of first gas-liquid separator.The hydrogen-containing gas discharger that leaves last gas-liquid separator is as the feed hydrogen of the hydrocarbon conversion process of consumption hydrogen such as hydrodesulfurizationof of hydrocarbons process or as the fuel gas of factory system.Heavy hydrocarbon streams at the bottom of the second hydrocarbon liquid enters stabilizer tower and is separated into overhead gas, the logistics of cat head lighter hydrocarbons and tower, the logistics of described stabilizer tower cat head lighter hydrocarbons enters deethanizing column and is separated into overhead gas and a tower base stream, directly turn back at least a portion stabilizer tower overhead gas and deethanizer overhead gas in the equilibrium hydrogen compressor hydrogen inlet pipeline or turn back to compression, in the pipeline of the equilibrium hydrogen cooled off, enter second gas-liquid separator then and finish and the contacting of hydrocarbon liquid to reclaim lighter hydrocarbons and H wherein
2U.S. Pat P4673488 is specially adapted to catforming process to improve H
2And C
3, C
4The rate of recovery, at this moment, described first gas-liquid separator is that 0.35～1.0MPa, temperature are to operate under 15～60 ℃ of conditions at pressure, last gas-liquid separator is that 4.7～5.5MPa, temperature are to operate under 15～60 ℃ of conditions at pressure.
The objective of the invention is to propose a kind ofly from the hydrocarbons hydrogenation treating processes stabilizer tower overhead gas of consumption hydrogen, reclaim C
3, C
4The method of hydrocarbon.
C in the hydrocarbons hydrogenation treating processes stabilizer tower overhead gas of the present invention
3, C
4The major technique feature of the recovery method of hydrocarbon is: contain H
2, H
2S, C
- 4Hydrocarbon and C
+ 5Be mixed into mixture with circulation gas after the high-pressure separator hydrocarbon liquid step-down of the hydrocarbons hydrogenation treating processes 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, and light pressure separator hydrocarbon liquid enters working pressure to be in 1.0～2.3MPa stabilizer tower and to be separated into mainly by C
+ 5Heavy hydrocarbon streams at the bottom of the stable Tata that hydrocarbon is formed, mainly by C
3, C
4The stabilizer tower cat head lighter hydrocarbons logistics that hydrocarbon is formed and contain C
3, C
4The stabilizer tower overhead gas of hydrocarbon, at least a portion stabilizer tower overhead gas as circulation gas with return described light pressure separator, the C in the circulation gas after high-pressure separator hydrocarbon liquid after the step-down mixes
3, C
4Hydrocarbon is absorbed and finally enters in stabilizer tower in the logistics of stabilizer tower cat head lighter hydrocarbons by light pressure separator hydrocarbon liquid and is recovered.
Accompanying drawing is a schematic flow sheet of the present invention.
Be described in detail technology contents of the present invention below in conjunction with accompanying drawing. As shown in drawings, the hydrocarbons hydrogenation processing procedure high-pressure separator hydrocarbon liquid step-down of described composition is mixed into mixture by pipe 1 and along the circulating air of managing 11, and mixture enters in the low pressure separator 5 through managing 2, mainly by H2、CH
4、C
2H
6The low minute gas (low pressure separator gas) that forms leaves low pressure separator top discharger and removes to take off H through managing 32S processes, mainly by C+ 3The low minute hydrocarbon liquid (low pressure separator hydrocarbon liquid) that hydrocarbon forms enters in the stabilizer 6 through managing 4. In low pressure separator 5, the most of H in the high-pressure separator hydrocarbon liquid2Be desorbed, simultaneously, the C in the circulating air+ 3Hydrocarbon is absorbed.
The operating condition of low pressure separator 5 is: temperature is 30～65 ℃; Pressure is 0.5～2.7MPa, is preferably 1.3～2.4MPa.
As shown in drawings, light pressure separator hydrocarbon liquid enters in the interchanger 12 through managing 4, with the reaction effluent of this hydrotreatment of mobile process or high-temperature product logistics heat exchange in the pipe 13 to reclaim heat.Light pressure separator hydrocarbon liquid after the intensification leaves 12 and enters stabilizer tower 6 middle parts through managing 4.Contain C
3, C
4The steam effluent of hydrocarbon through manage 7, behind the condensate cooler 8, pipe 9, gas, liquid mixture enter and carry out pneumatic separation in the return tank of top of the tower 10, mainly by C
3, C
4The overhead hydrocarbon liquid that hydrocarbon is formed leaves return tank 10 from 10 bottoms through managing 14, a part through manage 15, pump 17, pipe 18 return tower 6 tops as trim the top of column, a part is left return tank as cat head lighter hydrocarbons thing flowing pipe 16 and is removed deethanizing column or liquefied gas separation column.Mainly by C
+ 5Oil leaves the stabilizer tower bottom through managing 19 at the bottom of the tower that hydrocarbon is formed, a part through manage 20, pump 21, pipe 22, reboiler furnace 23, pipe 24 return tower bottom, to go the fractionation part be narrow fraction oil product such as petroleum naphtha, kerosene, diesel oil and wax oil etc. with the fractionation to a part through managing 25 as heavy hydrocarbon streams at the bottom of the tower.Contain a large amount of C
3, C
4The overhead gas of hydrocarbon leaves return tank through managing 11 from 10 tops.The operating method of stabilizer tower can be that reboiler furnace at the bottom of bottom reboiler or the tower is set, and also can be the water steam stripped.Shown in the figure is the situation that reboiler furnace is set.
Stabilizer tower 6 is tray column or packing tower, and number of theoretical plate is 8～50, and feed plate is positioned at the tower middle part.The operational condition of stabilizer tower is: tower top pressure is 1.0～2.3MPa, preferably 1.3～1.8MPa; Tower top temperature is 55～95 ℃, and column bottom temperature is 200～330 ℃, and the trim the top of column temperature is 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 drawings, at least a portion stabilizer tower overhead gas is mixed as the high-pressure separator hydrocarbon liquid after circulation gas and the step-down contact to returning behind the mixture in the light pressure separator with the C in the recovery overhead gas
3, C
4Hydrocarbon, shown in the figure is the situations of whole overhead gases as circulation gas.
It should be noted that for accompanying drawing any is, particular case according to light pressure separator working pressure and stabilizer tower working pressure, need on pipeline 11, be provided with compressor (not expressing among the figure) with after the overhead gas supercharging as circulation gas return light pressure separator 5 and or on pipeline 4, before the heat exchange of light pressure separator hydrocarbon liquid heats up, pump (not expressing among the figure) is set so that light pressure separator hydrocarbon liquid is delivered in the stabilizer tower 6, about this point, the those of skill in the art in present technique field are easy to judge and make decision.
An important feature of the present invention is for described hydrotreatment process, only the stabilizer tower overhead gas need be turned back in the light pressure separator charging and can realize purpose of the present invention.
Therefore the present invention has the flow process characteristic of simple, and can realize purpose of the present invention after can utilizing existing hydrotreater to be transformed.
The present invention utilizes light pressure separator hydrocarbon liquid weight rate than big many of stabilizer tower overhead gas weight rate with have and dissolve C more by force
+ 3The characteristics of the ability of hydrocarbon are circulated to overhead gas in the light pressure separator, the C in the circulation gas
+ 3, hydrocarbon is absorbed by light pressure separator hydrocarbon liquid and finally enters in stabilizer tower in the logistics of cat head lighter hydrocarbons.Therefore, the invention has the advantages that it can improve C in the hydrotreatment process high-pressure separator hydrocarbon liquid
3, C
4The liquids recovery rate of hydrocarbon.Characteristics of the present invention are suitable for C in the hydrocracking process stabilizer tower overhead gas
3, C
4The recovery of hydrocarbon.
The present invention be advantageous in that it is improving C
3, C
4In the time of the hydrocarbon rate of recovery, that has reduced that hydrotreater discharges removes to take off H
2C in the hydrocarbon gas of S device
+ 3The content of hydrocarbon.Taking off H
2In the S process, C
+ 3The too high hydrocarbon gas of hydrocarbon content can aggravate the foaming tendency of the solvent of amine desulfurization, influences stably manufactured, and causes sour gas (H
2S) contain more hydro carbons in the product, finally influence the sulfur recovery facility quality product as generating black sulphur, for processing the higher wax oil of sulphur content or the hydrocracking process of residual oil, above-mentioned situation is even more serious.Adopt the hydrocarbon gas of hydrotreatment process of the present invention in the hydrogen sulfide removal process that uses amine solvent, the problems referred to above can not take place.
Embodiment:
In processing power is 80 * 10
4Ton/year decompressed wax oil hydroeracking unit on, reclaim C in the high-pressure separator hydrocarbon liquid according to the inventive method
3, C
4Hydrocarbon, its operational condition and the results are shown in subordinate list.List file names with device in the table and do not established C in the stabilizer tower overhead gas
3, C
4The operational condition of stabilizer tower and C during the hydrocarbon recvery facility
3, C
4The recovery result of hydrocarbon is in order to compare.
From the table data as can be seen, C in the high-pressure separator hydrocarbon liquid of the present invention
3, C
4It is heavy that the hydrocarbon rate of recovery reaches 62～89%(), and do not establish C in the stabilizer tower overhead gas
3, C
4The hydrocarbon recvery facility is compared, C
3, C
4It is heavy that the hydrocarbon liquid product rate of recovery can improve 1.27～2.67%(, to device stock oil).
Whether reclaim C in the overhead gas
3, C
4Hydrocarbon reclaims with the present invention with the present invention and reclaims
Main operational condition
High-pressure separator hydrocarbon liquid:
Flow rate kilogram/hours 163,156 163,156 162,397 162397
C
3, C
4The heavy % 3.52 3.52 3.36 3.36 of hydrocarbon content
H
2The heavy % 0.027 0.027 1.59 1.59 of S content
Light pressure separator:
Temperature ℃ 51 49 51 49
Pressure MPa 2.20 2.20 2.05 2.05
Stabilizer tower:
Theoretical stage several piece 32 32 32 32
Tower top pressure MPa 1.65 1.65 1.65 1.65
Feed plate location plate several 19 19 19 19
Tower top temperature ℃ 80 82 59 63
Column bottom temperature ℃ 289 289 289 289
Return tank temperature ℃ 40 40 40 40
Reflux ratio 5.2 5.86 1.90 2.17
Go out device gas:
The low gas that divides of classification hangs down branch gas and low gas low branch gas and the cat head of dividing of cat head
The gas mixture of the mixture gas of gas
Flow rate kilogram/hours 2,280 3,572 6,171 9291
C
3, C
4The heavy % 27 53 34 51 of hydrocarbon content
Stabilizer tower overhead gas flow rate Mm
3/ h 2,000 1,591 7,832 3990
Circulation gas flow rate Mm
3/ h 2,000 7832
C in the high-pressure separator hydrocarbon liquid
3, C
4The hydrocarbon rate of recovery
Heavy % device C
3, C
4Hydrocarbon liquid product yield 89.2 67.0 62.0 13.1
%(is heavy, to device stock oil) 5.12 3.85 3.38 0.71
Claims (3)
1, C in a kind of hydrocarbons hydrogenation treating processes stabilizer tower overhead gas
3, C
4The recovery method of hydrocarbon is characterized in that it may further comprise the steps:
(1), contains H
2, H
2S, C
4 -Hydrocarbon and C
5 +After the high-pressure separator hydrocarbon liquid step-down of the hydrocarbons hydrogenation treating processes of hydrocarbon with from the C that contains of step (4)
3, C
4The circulation gas of hydrocarbon mixes contact and is mixture;
(2), described mixture enters in the light pressure separator, is that 0.5～2.7MPa, temperature are to be separated into mainly by H under 30～65 ℃ the operational condition at pressure
2, CH
4And C
2H
6The light pressure separator gas of forming and mainly by C
3 +The light pressure separator hydrocarbon liquid that hydrocarbon is formed, light pressure separator gas is discharged from the light pressure separator top;
(3), described light pressure separator hydrocarbon liquid enters in the stabilizer tower that working pressure is 1.0～2.3MPa and is separated into and contains C
3, C
4The stabilizer tower overhead gas of hydrocarbon, mainly by C
3, C
4The cat head lighter hydrocarbons logistics that hydrocarbon is formed and mainly by C
5 +Heavy hydrocarbon streams at the bottom of the tower that hydrocarbon is formed;
(4), at least a portion contains C by what step (3) obtained
3, C
4The stabilizer tower overhead gas of hydrocarbon is as circulation gas described in the step (1).
2, C in the overhead gas according to claim 1
3, C
4The recovery method of hydrocarbon is characterized in that: the working pressure of light pressure separator is preferably 1.3～2.4MPa.
3, C according to claim 1
3, C
4The recovery method of hydrocarbon is characterized in that: the working pressure of stabilizer tower is preferably 1.3～1.8MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93106265 CN1027819C (en) | 1993-05-29 | 1993-05-29 | Method for recovery of C3 and C4 hydrocarbons from overhead gas in hydrotreating process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93106265 CN1027819C (en) | 1993-05-29 | 1993-05-29 | Method for recovery of C3 and C4 hydrocarbons from overhead gas in hydrotreating process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1082592A CN1082592A (en) | 1994-02-23 |
| CN1027819C true CN1027819C (en) | 1995-03-08 |
Family
ID=4986138
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 93106265 Expired - Fee Related CN1027819C (en) | 1993-05-29 | 1993-05-29 | Method for recovery of C3 and C4 hydrocarbons from overhead gas in hydrotreating process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1027819C (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1320096C (en) * | 2004-10-13 | 2007-06-06 | 姜国文 | Brewing equipment for preparing lightweight alkane from heavy hydrocarbon and process thereof |
| CN100378205C (en) * | 2004-10-22 | 2008-04-02 | 中国石油化工股份有限公司 | Process for reducing contents of components above C3 in dry gas |
| CN102807891B (en) * | 2011-05-30 | 2015-03-11 | 中国石油化工集团公司 | System and method for processing condensate oil |
| CN105038889B (en) * | 2015-06-10 | 2017-06-16 | 山东宝塔新能源有限公司 | Coal tar hydrogenating LPG production technologies |
| CN106595223B (en) * | 2016-11-22 | 2018-12-28 | 西安长庆科技工程有限责任公司 | The system and method for three or more heavy hydrocarbon of carbon in a kind of recycling natural gas |
| CN111393248B (en) * | 2019-07-15 | 2023-05-26 | 中国石化工程建设有限公司 | Device and method for desulfurizing oil gas and recovering light hydrocarbon |
-
1993
- 1993-05-29 CN CN 93106265 patent/CN1027819C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1082592A (en) | 1994-02-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1642860B (en) | Process for increasing hydrogen partial pressure in hydroprocessing processes | |
| CN101273113B (en) | Hydrogen purification for make-up gas in hydroprocessing processes | |
| RU2134712C1 (en) | Oil stock hydrogenation treatment process and hydroconversion plant | |
| CN1263827C (en) | Integrated bitumen prodn. and gas conversion | |
| KR100311429B1 (en) | Process and apparatus for recovering product from hydrogenation reactor reactor stream | |
| US7276151B1 (en) | Gas turbine fuel oil and production method thereof and power generation method | |
| CN101418235B (en) | Catalytic cracking oil and gas separation method | |
| CN1876767B (en) | Coal tar hydrocracking method | |
| CN101684415B (en) | Hydrocracking method for producing chemical materials to maximum with low cost | |
| CN103146426B (en) | Method of converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas | |
| CN102146298A (en) | Hydrocarbon hydrogenation conversion process combined method | |
| CN1137967C (en) | Method for separating hydrocarbon hydrocracking products | |
| CN1027819C (en) | Method for recovery of C3 and C4 hydrocarbons from overhead gas in hydrotreating process | |
| CN102159679B (en) | Method and apparatus for recovering hydrogen in petroleum-based hydrocarbon desulfurization process | |
| CN102395658A (en) | High pressure revamp of low pressure distillate hydrotreating process units | |
| CN1128859C (en) | Converting and combining method for hydrogenation of hydrocarbon | |
| CN1721509A (en) | Medium pressure hydrocracking process for preparing jet fuel | |
| CN111348981A (en) | Crude benzene hydrofining method and device | |
| CN1896189A (en) | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil | |
| CN103497782A (en) | Method of producing low-sulfur low freezing point diesel by full-range shale oil | |
| CN1122706C (en) | Resultant oil separating method during hydrocarbon hydrotreatment | |
| CN1064700C (en) | Separation method for oil generated from hydrogen conversion process of hydrocarbon | |
| CN106221797A (en) | Deep processing of shale oil method | |
| CN1261544C (en) | Medium pressure hydrogenation method for maximumly producing high quality diesel fuel | |
| CN102161911A (en) | Hydrogenation conversion integrated method for high-nitrogen and high-aromatic hydrocarbon oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |