CN105276924A - Light hydrocarbon cryogenic separation and recovery device and method - Google Patents
Light hydrocarbon cryogenic separation and recovery device and method Download PDFInfo
- Publication number
- CN105276924A CN105276924A CN201410455184.0A CN201410455184A CN105276924A CN 105276924 A CN105276924 A CN 105276924A CN 201410455184 A CN201410455184 A CN 201410455184A CN 105276924 A CN105276924 A CN 105276924A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- methane
- carbon
- heat exchanger
- recovery tower
- 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.)
- Granted
Links
Landscapes
- Separation By Low-Temperature Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a light hydrocarbon cryogenic separation and recovery device and method. The device is provided with a methane/hydrogen separation system and comprises a 1# tail gas heat exchanger, a hydrogen/methane separation tank and a hydrogen flow dividing controller. A top pipeline of a 3# demethanizer feeding separation tank is connected with the hydrogen/methane separation tank after passing the 1# tail gas heat exchanger; a bottom pipeline of the hydrogen/methane separation tank is connected with a demethanizer after passing the 1# tail gas heat exchanger; a top outlet pipeline of the hydrogen/methane separation tank is provided with the hydrogen flow dividing controller; a flow dividing pipeline of the hydrogen flow dividing controller is connected with a hydrogen/methane expansion machine system. According to the device and method, due to the fact that chilling separation is performed on dried light hydrocarbon pyrolysis gas, high-purity H2 can be obtained, CH4 and C2's are almost totally separated, and the device and method are particularly suitable for ethylene devices with ethane being pyrolysis raw materials.
Description
Technical field
The present invention relates to lighter hydrocarbons recovery field, say further, relate to a kind of lighter hydrocarbons cryogenic separation retracting device and method.Be adapted to especially on ethylene unit, when taking ethane as major cleavage raw material, separate section requires higher ethene and the place of hydrogen recovery rate.
Background technology
The cracking stock of ethylene unit mainly contains ethane, propane, saturated LPG, naphtha, hydrogenation tail oil and light diesel fuel etc., and the yield of the lighter ethene of general raw material is higher, and the energy consumption of device is also lower.Along with state inside/outside liquefied natural gas (LNG) develops improving constantly of output, and a large amount of exploitation of shale gas, be that the ethylene unit of major cleavage raw material will certainly further be developed and apply with ethane.
In heavy charge cracking gas CH4, C3s and above heavy component output higher, and in ethane cracking product, H2 and ethane content are very high, heavy constituent output is minimum.Domestic existing cracking of ethylene deep cooling process for separating flow process, mainly for the ubiquitous liquid phase heavy charge customization of current China (see Fig. 1), is not too suitable for the separation of the phase feed cracking gases such as the very high ethane of light component content.Such as: when taking naphtha as cracking stock, yield of ethene can reach 99.6%, more than hydrogen purity 95mol%.And during for separating of ethane cracking gas, hydrogen purity is only 86mol%; Ethylene loss, up to 3.3%, for the ethylene unit of a set of megaton, is namely equivalent to the ethylene loss amount of about 4 tons/hour, and waste is serious.
External existing light hydrocarbon cracking device, it is not the problem that very high, hydrogen also needs separately to establish transformation adsorption device (PSA) to purify that its isolation technics also also exists the ethene of high added value and hydrogen product yield, causes certain loss of economic benefit or the extra increase of plant investment.
Summary of the invention
For solving produced problem in prior art, the invention provides a kind of lighter hydrocarbons cryogenic separation retracting device and method.For separating of when taking ethane as the cracking gas of primary raw material, the rate of recovery and the hydrogen purity of ethene can be improved significantly, make it to reach can be suitable with existing feed naphtha separation process degree.
An object of the present invention is to provide a kind of lighter hydrocarbons cryogenic separation retracting device.
Comprise: domethanizing column, carbon two recovery tower, 1# ~ 7# tail gas heat exchanger, 1# ~ 3# domethanizing column charging knockout drum,
Described device is provided with methane/hydrogen piece-rate system, comprising: 1# tail gas heat exchanger, hydrogen/methane separation tank and hydrogen flow controller; 3# domethanizing column charging knockout drum overhead line connects hydrogen/methane separation tank after 1# tail gas heat exchanger, and hydrogen/methane separation pot bottom pipeline connects domethanizing column after 1# tail gas heat exchanger; Hydrogen/methane separation tank top outlet line arranges hydrogen flow controller, and the bypass line of hydrogen flow controller connects hydrogen methane expander system;
Demethanizer overhead connects carbon two recovery tower, arranges condenser, connect domethanizing column bottom carbon two recovery tower in carbon two recovery tower, and carbon two recovery tower top connects hydrogen methane expander system;
Hydrogen methane expander system comprises: expander inlet blending tank, decompressor, outlet knockout drum; Expander inlet blending tank is connected after the bypass line of hydrogen flow controller merges with carbon two recovery tower overhead line, expander inlet blending tank top connects decompressor, connection outlet knockout drum after expander outlet pipeline and expander inlet blending tank outlet line merge, outlet knockout drum bottom line is divided into two, a condenser connected in carbon two recovery tower, another sends out-of-bounds after tail gas heat exchanger.
Wherein,
Described carbon two recovery tower adopts segregation fractionating column pattern.
Two of object of the present invention is to provide a kind of lighter hydrocarbons cryogenic separation recovery method.
Comprise:
1) cracking gas of drying and dehydrating is after heat exchange and cooling, isolates liquid phase wherein, from bottom to top successively as first, second, and third burst of charging of domethanizing column by 1#, 2# and 3# domethanizing column charging knockout drum;
2) gas phase of 3# domethanizing column charging knockout drum enters hydrogen/methane separation tank after the heat exchange of 1# tail gas heat exchanger, the liquid phase that hydrogen/methane separation tank is separated after the heat exchange of 1# tail gas heat exchanger as the 4th of domethanizing column the burst of charging; The gas phase portion that hydrogen/methane separation tank is separated is sent out-of-bounds as high pressure hydrogen, and branching part is to hydrogen methane expander system;
3) demethanation top gaseous phase sends into carbon two recovery tower, and recovered ethylene, is back to domethanizing column at the bottom of carbon two recovery tower tower;
4) carbon two reclaims top gaseous phase and hydrogen that methane/hydrogen piece-rate system distributes converges, enter expander inlet blending tank, gas phase is as the charging of decompressor, liquid phase and expander outlet mixing of materials, enter outlet knockout drum, the gas phase separated is second burst of hydrogen product, and the liquid phase a separated part provides cold for the condenser in carbon two recovery tower, and another part provides deep cooling cold for tail gas heat exchanger.
Deep cooling cold needed for methane/hydrogen piece-rate system, be not that the hydrogen that all gone out by this systematic position and methane throttling produce, the cold of 68 ~ 83% is provided by decompressor;
In step (2), the gas phase that hydrogen/methane separation tank is separated branches to the ratio of hydrogen methane expander system between 63 ~ 100%.
In step (3), the charging of carbon two recovery tower based on methane, tower top temperature less than-108 DEG C.
In step (4), in decompressor charging, the volumn concentration of hydrogen is 83 ~ 92%.
The present invention can be achieved through the following technical solutions:
Described lighter hydrocarbons deep cooling process for separating flow process contains a set of cracking gas chilling train.
Plate-fin tail gas heat exchanger (being placed in ice chest) containing some series connection in chilling train, multiple domethanizing column charging knockout drum and a methane/hydrogen separator system.
The function of chilling train mainly cools cracking gas, for domethanizing column provides charging, and separating hydrogen gas.Cold required for it provides primarily of propylene refrigerant, ethene cryogen and hydrogen/methane expander system, reclaims the cold of cycle ethane, demethanation tower bottoms, hydrogen and Methane offgas etc. simultaneously.
Described methane/hydrogen piece-rate system contains a tail gas heat exchanger the coldest, a hydrogen/methane separation tank and a hydrogen flow controller.Described hydrogen flow controller, shunt ratio between 63 ~ 100%, the hydrogen fed downstream hydrogen/methane decompressor separated.The liquid phase methane that this systematic position goes out is not directly do methane product, but returns tail gas heat exchange re-heat to after-101 DEG C, goes up one charging most, to reclaim carbon two component wherein further as domethanizing column.
Described lighter hydrocarbons deep cooling process for separating flow process adopts high pressure demethanation technology, and single tower, tower is pressed between 2.9 ~ 3.2MPaG, has four bursts of chargings, by the ethene cryogen condensing reflux of the coldest (-101 DEG C) one-level.Replace original return tank at demethanizer overhead, carbon two recovery tower is separately set, adopt segregation fractionating column (CFT) pattern, provide cold, recovered ethylene by a part of liquid phase methane of hydrogen/methane expander outlet.
Described lighter hydrocarbons deep cooling process for separating flow process also contains a set of hydrogen, methane expands/recompress machine system, comprises hydrogen/methane decompressor, Methane offgas recompression machine and hydrogen recompression each one of machine.
Described hydrogen/methane decompressor, its charging is mainly low temperature H2, and depending on the needs manufactured and designed, can be one section and also can be divided into two sections, entrance establishes hydrogen/methane blended tank, and knockout drum is established in outlet.It is parallel with decompressor that expenditure and pressure valve is set, extremely exports the direct conveying of knockout drum for liquid phase from entrance blending tank.
Described hydrogen/methane expander system, except first for except methane/hydrogen piece-rate system and carbon two recovery tower provide cold, the H2 that also carbon two can be reclaimed in tower top methane reclaims clean, and again can isolate the higher hydrogen product of purity.
Effect of the present invention is: by the shunting hydrogen of vast scale, decompressor is entered together with methane, not only directly can isolate the hydrogen that one purity is 92 ~ 97mol%, the cold that tower top provides the coldest one-level can also be reclaimed for chilling train, carbon two, thus isolate the high pressure of one concentration between 95 ~ 99mol%, high-purity hydrogen, and ethylene loss rate in whole Quench and demethanation system is made to be reduced to the ultra low levels of 0.039 ~ 0.084%.In Methane offgas, hydrogen loss can be controlled within 0.3%.
Replace demethanizer reflux tank with carbon two recovery tower, Recovery rate of ethylene can be made to improve 0.5 percentage point, for a set of 1,000,000 tons/year of ethylene light hydrocarbon devices, be equivalent to many recovered ethylene and be about 622kg/h, nearly 5,000 ten thousand yuan of annual increase yield.
Accompanying drawing explanation
One of process flow diagram of Fig. 1 prior art
Fig. 1 description of symbols:
1 ~ 7-1# ~ 7# tail gas heat exchanger; 8-methane recompression machine; 9-exports water cooler; 10-Methane offgas; 11-low-pressure methane; 12-high pressure hydrogen; 14-cycle ethane; 17-cracking gas; 18-hydrocarbon liquid; The pre-demethanation tower bottoms of 19-; 20-demethanation tower bottoms; 21-cycle ethane vaporizer; The pre-domethanizing column feed cooler of 22-; 23-pre-domethanizing column charging knockout drum; 24 ~ 26-1 ~ 3# domethanizing column charging knockout drum; 27-hydrogen/methane separation tank; 28-domethanizing column first charging chiller; 29-domethanizing column second charging chiller; The pre-domethanizing column of 30-; The pre-demethanizer reboiler of 31-; The pre-domethanizing column condenser of 32-; 33-domethanizing column; 34-demethanizer reboiler; 35-domethanizing column condenser; 37-reflux pump; 38-return tank; 40-Methane offgas decompressor.
Fig. 2 process flow diagram of the present invention
Fig. 2 description of symbols:
1 ~ 7-1# ~ 7# tail gas heat exchanger; 8-methane recompression machine; 9-methane water cooler; 10-Methane offgas; 12-high pressure hydrogen; 13-low pressure hydrogen; 14-cycle ethane; 15-hydrogen water cooler; 16-hydrogen recompression machine; 17-cracking gas; 20-demethanation tower bottoms; 21-cycle ethane vaporizer; 24 ~ 26-1# ~ 3# domethanizing column charging knockout drum; 27-hydrogen/methane separation tank; 28-domethanizing column first charging chiller; 29-domethanizing column second charging chiller; 33-domethanizing column; 34-demethanizer reboiler; 35-domethanizing column condenser; 36-carbon two recovery tower condenser; 37-reflux pump; 39-carbon two recovery tower; 41-hydrogen/methane decompressor; 42-expander inlet blending tank; 43-choke valve; 44-exports knockout drum; 45-hydrogen flow controller; 46-methane/hydrogen separator system.
Detailed description of the invention
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment
As shown in Figure 2, a kind of lighter hydrocarbons cryogenic separation retracting device.
Comprise: domethanizing column 33, carbon two recovery tower 39,1# ~ 7# tail gas heat exchanger, 1# ~ 3# domethanizing column charging knockout drum,
Described device is provided with methane/hydrogen piece-rate system, comprising: 1# tail gas heat exchanger 1, hydrogen/methane separation tank 27 and hydrogen flow controller 45; 3# domethanizing column charging knockout drum 26 overhead line connects hydrogen/methane separation tank 27 after 1# tail gas heat exchanger 1, and hydrogen/methane separation tank 27 bottom line connects domethanizing column 33 after 1# tail gas heat exchanger 1; Hydrogen/methane separation tank 27 top exit pipeline arranges hydrogen flow controller 45, and the bypass line of hydrogen flow controller 45 connects hydrogen methane expander system;
Domethanizing column 33 top connects carbon two recovery tower 39, arranges condenser, connect domethanizing column 33 bottom carbon two recovery tower in carbon two recovery tower 39, and carbon two recovery tower 39 top connects hydrogen methane expander system;
Hydrogen methane expander system comprises: expander inlet blending tank 42, decompressor 41, outlet knockout drum 44; Expander inlet blending tank 42 is connected after the bypass line of hydrogen flow controller 45 merges with carbon two recovery tower 39 overhead line, expander inlet blending tank 42 top connects decompressor 41, connection outlet knockout drum 44 after decompressor 41 outlet line and expander inlet blending tank 42 outlet line merge, outlet knockout drum 44 bottom line is divided into two, a condenser connected in carbon two recovery tower 39, another sends out-of-bounds after tail gas heat exchanger.
Wherein,
Described carbon two recovery tower 39 adopts segregation fractionating column pattern.
After the cracking gas of drying and dehydrating enters chilling train, by the plate-fin tail gas heat exchanger of common autoclave heat exchanger and multiple series connection, through propylene refrigerant at different levels, cycle ethane, demethanation tower bottoms and ethene cryogens at different levels etc., be cooled to-45 ~-55 DEG C ,-70 ~-72 DEG C and-96 ~-98 DEG C step by step, liquid phase is wherein isolated, from bottom to top successively as first, second, and third burst of charging of domethanizing column 33 by domethanizing column 1#, 2# and 3# charging knockout drum.
Last remaining cracking gas contains the feeding methane/hydrogen separator systems such as H2 and CO, the half of the overwhelming majority many CH4 and a small amount of C2 ' s, through most cold junction 1# tail gas heat exchanger be further cooled to-152 ~-182 DEG C even below, enter hydrogen/methane separation tank.Isolated liquid phase at the bottom of tank, is mainly CH4 and C2 ' s, returns the re-heat of 1# tail gas heat exchanger to after more than-101 DEG C by governor valve control, goes up one (the 4th strand) charging most, fully recovery carbon two component wherein as domethanizing column.The gas that tank deck separates is the high-purity hydrogen of 95 ~ 99mol% concentration, distributes a small part by hydrogen flow controller, and after cracking gas chilling train recovery cold, re-heat is to normal temperature (30 DEG C), directly as high pressure hydrogen product; Another major part is then sent to follow-up hydrogen, methane expander system.
Demethanizer reboiler propylene refrigerant does thermal source, ensures tower reactor not containing CH4; Tower top ethene cryogen is cooled to about-98 DEG C.At the bottom of tower, still liquid product is through chilling train re-heat, send downstream units after components vaporize; Top gaseous phase effluent sends into carbon two recovery tower bottom, and recovered ethylene, improves its rate of recovery.Carbon two recovery tower, by a part of liquid phase methane condensing reflux of hydrogen/methane expander outlet, can to control in its overhead product ethylene contents at below 0.2mol%; Liquid phase at the bottom of tower returns demethanation tower top and refluxes together.
Carbon two reclaims top gaseous phase product and hydrogen that methane/hydrogen separator system distributes converges, enter hydrogen/methane expander inlet blending tank together, gas phase is as the charging of decompressor, liquid phase by Liquid level through choke valve reduce pressure after, walk around decompressor directly and its discharge mixing of materials, jointly enter expander outlet knockout drum.The gas phase that knockout drum separates is second burst of hydrogen product, purity at more than 92mol%, for chilling train provides the refrigeration cold of the coldest level; Liquid phase is high-purity methane, is discharged by Liquid level, and a part first provides cold for carbon two scrubber overhead, then continues as chilling train and provide deep cooling cold together with another part.
At the latter half of chilling train, two strands of hydrogen product, Methane offgas, cycle ethane and ethylene products after propylene refrigerant etc. reclaims cold, all by re-heat to about 30 DEG C.High Pressure Hydrogen pneumatic transmission methanation unit or directly send outside; Low pressure hydrogen is increased to after about 2.5MPaG through recompression machine and sends outside, and wherein hydrogen gas compressor one section is driven by decompressor.Methane offgas boosts to about 0.50MPaG through recompression machine, send drier regenerative system to use, finally send pyrolysis furnace to make fuel.
Claims (7)
1. a lighter hydrocarbons cryogenic separation retracting device, comprising: domethanizing column, carbon two recovery tower, 1# ~ 7# tail gas heat exchanger, 1# ~ 3# domethanizing column charging knockout drum, is characterized in that:
Described device is provided with methane/hydrogen piece-rate system, comprising: 1# tail gas heat exchanger, hydrogen/methane separation tank and hydrogen flow controller; 3# domethanizing column charging knockout drum overhead line connects hydrogen/methane separation tank after 1# tail gas heat exchanger, and hydrogen/methane separation pot bottom pipeline connects domethanizing column after 1# tail gas heat exchanger; Hydrogen/methane separation tank top outlet line arranges hydrogen flow controller, and the bypass line of hydrogen flow controller connects hydrogen methane expander system;
Demethanizer overhead connects carbon two recovery tower, arranges condenser, connect domethanizing column bottom carbon two recovery tower in carbon two recovery tower, and carbon two recovery tower top connects hydrogen methane expander system;
Hydrogen methane expander system comprises: expander inlet blending tank, decompressor, outlet knockout drum; Expander inlet blending tank is connected after the bypass line of hydrogen flow controller merges with carbon two recovery tower overhead line, expander inlet blending tank top connects decompressor, connection outlet knockout drum after expander outlet pipeline and expander inlet blending tank outlet line merge, outlet knockout drum bottom line is divided into two, a condenser connected in carbon two recovery tower, another sends out-of-bounds after tail gas heat exchanger.
2. lighter hydrocarbons cryogenic separation retracting device as claimed in claim 1, is characterized in that:
Described carbon two recovery tower adopts segregation fractionating column pattern.
3. adopt a lighter hydrocarbons cryogenic separation recovery method for device as claimed in claim 1 or 2, it is characterized in that described method comprises:
1) cracking gas of drying and dehydrating is after heat exchange and cooling, isolates liquid phase wherein, from bottom to top successively as first, second, and third burst of charging of domethanizing column by 1#, 2# and 3# domethanizing column charging knockout drum;
2) gas phase of 3# domethanizing column charging knockout drum enters hydrogen/methane separation tank after the heat exchange of 1# tail gas heat exchanger, the liquid phase that hydrogen/methane separation tank is separated after the heat exchange of 1# tail gas heat exchanger as the 4th of domethanizing column the burst of charging; The gas phase portion that hydrogen/methane separation tank is separated is sent out-of-bounds as high pressure hydrogen, and branching part is to hydrogen methane expander system;
3) demethanation top gaseous phase sends into carbon two recovery tower, and recovered ethylene, is back to domethanizing column at the bottom of carbon two recovery tower tower;
4) carbon two reclaims top gaseous phase and hydrogen that methane/hydrogen piece-rate system distributes converges, enter expander inlet blending tank, gas phase is as the charging of decompressor, liquid phase and expander outlet mixing of materials, enter outlet knockout drum, the gas phase separated is second burst of hydrogen product, and the liquid phase a separated part provides cold for the condenser in carbon two recovery tower, and another part provides deep cooling cold for tail gas heat exchanger.
4. lighter hydrocarbons cryogenic separation recovery method as claimed in claim 3, is characterized in that:
In step (2), the gas phase that hydrogen/methane separation tank is separated branches to the ratio of hydrogen methane expander system between 63 ~ 100%.
5. lighter hydrocarbons cryogenic separation recovery method as claimed in claim 3, is characterized in that:
In step (3), the charging of carbon two recovery tower is based on methane, and tower top temperature is below-108 DEG C.
6. lighter hydrocarbons cryogenic separation recovery method as claimed in claim 3, is characterized in that
In step (4), in decompressor charging, the volumn concentration of hydrogen is 83 ~ 92%.
7. lighter hydrocarbons cryogenic separation recovery method as claimed in claim 3, is characterized in that:
68 ~ 83% of deep cooling cold needed for methane/hydrogen piece-rate system is provided by decompressor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410455184.0A CN105276924B (en) | 2014-07-04 | 2014-09-09 | A kind of lighter hydrocarbons cryogenic separation retracting device and method |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2014103176119 | 2014-07-04 | ||
| CN201410317611 | 2014-07-04 | ||
| CN201410455184.0A CN105276924B (en) | 2014-07-04 | 2014-09-09 | A kind of lighter hydrocarbons cryogenic separation retracting device and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105276924A true CN105276924A (en) | 2016-01-27 |
| CN105276924B CN105276924B (en) | 2017-09-01 |
Family
ID=55146374
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410455184.0A Active CN105276924B (en) | 2014-07-04 | 2014-09-09 | A kind of lighter hydrocarbons cryogenic separation retracting device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105276924B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106766674A (en) * | 2016-12-09 | 2017-05-31 | 杭州杭氧股份有限公司 | A kind of ice chest deep cooling separating method of preparing isobutene through dehydrogenation of iso-butane project |
| CN107285973A (en) * | 2016-03-30 | 2017-10-24 | 中国石油化工股份有限公司 | The production and processing technology and production equipment of a kind of hydrocarbon gas containing naphthalene |
| CN108276236A (en) * | 2017-01-06 | 2018-07-13 | 中国石化工程建设有限公司 | A kind of Fischer-Tropsch process exhaust cryogenic separation recovery method of volume increase alkene |
| CN110006216A (en) * | 2019-03-29 | 2019-07-12 | 大连理工大学 | A kind of not solidifying discharge gas process for separating and recovering of the ethylene recycle refrigeration system that deep cooling is coupled with film |
| CN111895723A (en) * | 2019-05-06 | 2020-11-06 | 中国石化工程建设有限公司 | Separation device and separation method for reaction generated gas in propylene preparation through propane dehydrogenation |
| CN114034129A (en) * | 2021-11-26 | 2022-02-11 | 北京恒泰洁能科技有限公司 | Energy expansion reconstruction device and method for pyrolysis gas post-hydrogenation device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3902329A (en) * | 1970-10-28 | 1975-09-02 | Univ California | Distillation of methane and hydrogen from ethylene |
| JPS54103797A (en) * | 1978-02-03 | 1979-08-15 | Sumitomo Heavy Ind Ltd | H2 separation and purification from h2 containing gas |
| CN102675024A (en) * | 2011-03-07 | 2012-09-19 | 中国石油化工股份有限公司 | Separation process for preparing low-carbon olefin gas through methanol conversion |
| CN103318859A (en) * | 2012-03-22 | 2013-09-25 | 中国石油化工集团公司 | Rectification dehydration tower and dehydration method for nitrogen dioxide |
| CN103542693A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Ethylene cryogenic separation method for large-sized ethylene device |
-
2014
- 2014-09-09 CN CN201410455184.0A patent/CN105276924B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3902329A (en) * | 1970-10-28 | 1975-09-02 | Univ California | Distillation of methane and hydrogen from ethylene |
| JPS54103797A (en) * | 1978-02-03 | 1979-08-15 | Sumitomo Heavy Ind Ltd | H2 separation and purification from h2 containing gas |
| CN102675024A (en) * | 2011-03-07 | 2012-09-19 | 中国石油化工股份有限公司 | Separation process for preparing low-carbon olefin gas through methanol conversion |
| CN103318859A (en) * | 2012-03-22 | 2013-09-25 | 中国石油化工集团公司 | Rectification dehydration tower and dehydration method for nitrogen dioxide |
| CN103542693A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Ethylene cryogenic separation method for large-sized ethylene device |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107285973A (en) * | 2016-03-30 | 2017-10-24 | 中国石油化工股份有限公司 | The production and processing technology and production equipment of a kind of hydrocarbon gas containing naphthalene |
| CN106766674A (en) * | 2016-12-09 | 2017-05-31 | 杭州杭氧股份有限公司 | A kind of ice chest deep cooling separating method of preparing isobutene through dehydrogenation of iso-butane project |
| CN106766674B (en) * | 2016-12-09 | 2019-03-08 | 杭州杭氧股份有限公司 | A kind of ice chest deep cooling separating method of preparing isobutene through dehydrogenation of iso-butane project |
| CN108276236A (en) * | 2017-01-06 | 2018-07-13 | 中国石化工程建设有限公司 | A kind of Fischer-Tropsch process exhaust cryogenic separation recovery method of volume increase alkene |
| CN110006216A (en) * | 2019-03-29 | 2019-07-12 | 大连理工大学 | A kind of not solidifying discharge gas process for separating and recovering of the ethylene recycle refrigeration system that deep cooling is coupled with film |
| CN111895723A (en) * | 2019-05-06 | 2020-11-06 | 中国石化工程建设有限公司 | Separation device and separation method for reaction generated gas in propylene preparation through propane dehydrogenation |
| CN111895723B (en) * | 2019-05-06 | 2022-06-21 | 中国石化工程建设有限公司 | Separation device and separation method for reaction generated gas in propylene preparation through propane dehydrogenation |
| CN114034129A (en) * | 2021-11-26 | 2022-02-11 | 北京恒泰洁能科技有限公司 | Energy expansion reconstruction device and method for pyrolysis gas post-hydrogenation device |
| CN114034129B (en) * | 2021-11-26 | 2022-08-16 | 北京恒泰洁能科技有限公司 | Energy expansion reconstruction device and method for pyrolysis gas post-hydrogenation device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105276924B (en) | 2017-09-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105276924B (en) | A kind of lighter hydrocarbons cryogenic separation retracting device and method | |
| AU2013370173B2 (en) | Integrated process for NGL (natural gas liquids recovery) and LNG (liquefaction of natural gas) | |
| CN103940199B (en) | Method and device for extracting ethane-mixed hydrocarbon from natural gas | |
| CN109111336B (en) | Deep cooling recovery device and process for waste towed synthetic tail gas | |
| CN103175381B (en) | Low concentration coal-bed gas produces LNG technique containing oxygen cryogenic liquefying | |
| CN102408910B (en) | Method and device for recovering light hydrocarbon through refrigeration using compound refrigerant and secondary dealkylation | |
| CN106866339B (en) | Device and method for recovering ethane and co-producing crude helium from natural gas | |
| RU2629047C1 (en) | Complex for liquefaction, storage and offloading of natural gas | |
| CN105716371A (en) | Method and device for recycling mixed refrigerant refrigeration natural gas light hydrocarbon | |
| CN110538476A (en) | Low-temperature flash light hydrocarbon recovery system and method for oilfield associated gas | |
| CN108976099A (en) | A kind of deep cooling separating method of low carbon olefin gas | |
| CN109749780A (en) | A kind of oily device and method absorbed and compression condensation method recycles carbon two in oil refinery dry gas | |
| CN104061755B (en) | A kind of nitrogen rejection facility for natural gas and denitrification process thereof | |
| CN103994635A (en) | Device and method for recovering light hydrocarbon through cold energy of LNG | |
| CN103175380B (en) | Low concentration coal-bed gas produces LNG device containing oxygen cryogenic liquefying | |
| CN204981793U (en) | Processing apparatus of associated gas is applied to to LNG cold energy | |
| AU2016324362B2 (en) | A method of preparing natural gas to produce liquid natural gas (LNG) | |
| CN107163975B (en) | A kind of device and method of lighter hydrocarbons depth recycling | |
| CN206207884U (en) | A kind of oven gas LNG coproducing synthetic ammonia devices | |
| CN103086827A (en) | Olefin separation system and olefin separation method | |
| CN211273608U (en) | Low-temperature flash light hydrocarbon recovery system for oilfield associated gas | |
| CN212778207U (en) | Cold dry gas circulation recovery ethane device | |
| CN110590490A (en) | System and method for recovering hydrocarbons in liquefied natural gas | |
| CN209481601U (en) | A kind of heavy hydrocarbon separator and light ends unit for natural gas | |
| CN106568298A (en) | Coke-oven gas produced LNG coproduction ammonia synthesis device and control method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |