CN102267850A - Method for separating light olefins gas - Google Patents
Method for separating light olefins gas Download PDFInfo
- Publication number
- CN102267850A CN102267850A CN2010101887175A CN201010188717A CN102267850A CN 102267850 A CN102267850 A CN 102267850A CN 2010101887175 A CN2010101887175 A CN 2010101887175A CN 201010188717 A CN201010188717 A CN 201010188717A CN 102267850 A CN102267850 A CN 102267850A
- Authority
- CN
- China
- Prior art keywords
- tower
- demethanizing
- stream
- desorption
- column
- 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
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for separating a light olefins gas, which is used for producing target products such as ethylene, propylene and the like. The method comprises the following steps of: compressing the light olefins gas as the raw material, washing and drying, and introducing into a dethanizing column; separating a propylene product from column bottom material flow of the dethanizing column; performing four-section compression on the column top material flow of the dethanizing column, introducing into a demethanizing column and contacting with an absorbent for separating; introducing the column bottom material flow of the demethanizing column into a desorption column; introducing the column top gas-phase material flow of the desorption column into an acetylene converter; introducing into an ethylene rectifying column for producing an ethylene product; and returning the column bottom material flow of the desorption column to the upper part of the demethanizing column for recycling. The method has the advantages of small investment, low energy consumption, high recovery rates of ethylene and propylene, and the like.
Description
Technical field
The invention belongs to low-carbon alkene purification techniques field, relating to a kind of (mainly is methyl alcohol, ethanol, dme, C with oxygenatedchemicals
4～C
10Alkylol cpd or its mixture etc.) be raw material, be in the successive reaction and regenerative process of main streams (mainly being ethene and propylene) generating with the low-carbon alkene, the separation method of product low carbon olefin gas.
Background technology
Low-carbon alkene (ethene, propylene, divinyl) and light aromatics (benzene,toluene,xylene) are the basic raw materials of petrochemical complex.Ethylene production mainly relies on the tube furnace steam cracking technology of light naphthar raw material at present.Because it is not enough that the shortage of crude resources and the raising day by day of price, naphtha resource have more and more seemed, the production cost of low-carbon alkene is more and more higher.The domestic and international positive abundanter ethylene production route of active development raw material sources, the organic oxygen-containing compound raw material is through the katalysis of metal-modified SAPO type aperture phosphorus pure aluminium silicate Zn-Al-P-Si-oxide molecular sieve, can generate reaction product based on ethene, propylene, just be subjected to extensive attention both domestic and external, be in industrialization phase.
With methyl alcohol or dme is that the oxygen-containing organic compound of representative is typical oxygen-containing organic compound, mainly by the synthetic gas production of coal-based or Sweet natural gas base.In order to methyl alcohol is that to be raw material production mainly contain the MTO technology of American UOP company at present based on the low-carbon alkene technology of ethene and propylene that (main patent is U.S. Pat P6166282, USP5744680 for the oxygen-containing organic compound of representative; Chinese patent ZL00137259.9), (main patent is USP6673978, USP6717023, USP6613950 to the MTO technology of U.S. ExxonMobil company; Chinese patent ZL00815363.2, ZL00802040.x, ZL03821995.6), the DMTO technology (ZL96115333.4, ZL92109905.3) of MTP technology (EP0448000A, DE233975A1) and the Dalian Chemistry and Physics Institute of the Chinese Academy of Sciences.
The reaction characteristics that oxygenatedchemicals (current typical case adopt be methyl alcohol) is produced low-carbon alkene technology (MTO) is that rapid reaction, strong heat release and pure agent are lower frequently, is to react in successive reaction-regenerated dense fluidized bed bioreactor and regenerate.The high-temperature oil gas that is rich in low-carbon alkenes such as ethene and propylene that reaction generates need be carried out chilling and washing, remove wherein catalyzer and cooling after, be sent to the bottom olefin separation system and separate.The purpose product of MTO process unit is ethene and propylene, byproduct liquefied gas, C
5Above component and fuel gas.The formation of MTO gas and naphtha cracking gas are very different, and maximum difference is that hydrogen and methane content are lower in the MTO gas, propylene and propane content propylene and propane content in the naphtha cracking gas.The cracked gas that how this part is rich in low-carbon alkenes such as ethene and propylene separates, and improves the yield of purpose product ethene and propylene, receives publicity always.
WO01/25174 has disclosed a kind of method of producing ethene, and the principal feature of this method is: (1) adopts the front-end deethanization flow process, reduces the inlet amount of demethanizing tower; (2) produce ethylene unit with conventional naphtha cracking and compare, improved the ethylene content in the demethanizer overhead, thereby improved demethanizing cat head temperature, avoid adopting the ethene cold; (3) in order to reclaim the ethene in the demethanizing cat head gas, this gas is sent into transformation absorption facility, separation of methane, hydrogen and ethene are in the ethene Returning oxidation reactor outlet material that reclaims.This separation method facility investment is low, but owing to adopted the PSA technology, schedule of operation is complicated, and the workload of system maintenance is bigger.
CN101367697A has disclosed the separation method of light hydrocarbon product in a kind of MTO/MTP reaction product.This invention is to carry out C with sending into deethanizing column after the pre-treatment of MTO/MTP reaction product
2/ C
3Sharp separation, deethanizing cat head gas phase is delivered to absorb and is steamed tower, absorbs to steam tower and adopt the rich absorbent from oil-absorption tower to absorb, deethanizing Tata still product enters subsequent separation system; Absorption is steamed overhead product send into oil-absorption tower after cooling, oil-absorption tower adopts ethane as poor absorption agent, and separate absorbent steams the ethene in the column overhead product, and all the other light gas are discharged by cat head, and tower still product returns to absorb as rich absorbent and steams tower; Absorption steams Tata still product and enters ethylene column, and tower still ethane component enters oil-absorption tower after cooling off as poor absorption agent.Compared with prior art, the present invention has less investment, material recovery rate advantages of higher.
CN1157280A has disclosed a kind of light hydrocarbon separating method that improves the ethylene recovery rate, this invention is a kind of high ethylene recovery rate, the light hydrocarbon separating method of energy-conservation and low demethanizing tower load, lighter hydrocarbons are through overdraft, the gas and the liquid that obtain after cooling and the flash distillation enter the high pressure deethanizing column respectively, carry out the non-clear cutting of C-2-fraction, high pressure deethanizing Tata low yield thing enters the low pressure deethanizing column and carries out separating of carbon two and C3 fraction, high pressure deethanizer overhead product obtains liquid more than two strands as the charging of demethanizing tower through multistage cooling and flash distillation, the gas of knockout drum outlet enters methane absorber through cooling, with liquid phase methane as absorption agent, 99.5% ethene in the gas is absorbed, and methane absorber outlet at bottom liquid returns demethanizing tower as charging, and the demethanizing tower bottoms removes acetylene hydrogenation reactor or ethylene rectification tower.
CN100398498C has disclosed the separation method of a kind of converting methanol to prepare low carbon olefin (hereinafter to be referred as DMTO) gas, and the characteristics that constitute at DMTO gas are improved the flow process after four sections compressions in the conventional front-end deethanization separation process.According to this invention, between five sections compressions and deethanizing column return tank, be provided with and add the hydrogen-oxygen conversion, remove the oxygen that produces in acetylene and the reaction regeneration process, the cooled material of condensation is through the deethanizing column return tank, liquid phase refluxes as deethanizing column, and gas phase enters deep cooling demethanizing system, after material cools off through condensation, do not need to be provided with the preceding dehydrogenation system of loaded down with trivial details ice chest, directly enter high pressure demethanizer.Adopt the present invention to separate DMTO gas and can obtain 99.5% above ethylene recovery rate.
In sum, the separation method of the low-carbon alkene that relates in the prior art, employing is the deep cooling flow process of representative with sequence flow, front-end deethanization flow process and predepropanization process, majority is applied to ethylene cracker, but, any flow process all needs deep cooling for separation of methane, hydrogen and C2 hydrocarbon class, and the cold of multiple differing temps grade all need be provided by propylene compressor and ethylene compressor, for example needs the ethene refrigerant condenser that-100 ℃ cold is provided.Also need methane compressor for the low temperature demethanizing cold about-135 ℃ is provided.Except the refrigerant condenser system of complexity, also need the ice chest equipment of precise structure, these all make low temperature separation process flow process complexity, investment greatly.
Summary of the invention
Purpose of the present invention just is to provide a kind of separation method of low carbon olefin gas, to produce purpose products such as ethene and propylene.
The invention provides a kind of separation method of low carbon olefin gas, this separation method is characterised in that and comprises the steps:
1) enters deethanizing column after compressed, washing of low carbon olefin gas raw material and the drying, the tower base stream of deethanizing column is delivered to depropanizing tower, propylene rectification tower, isolate propylene product, four sections laggard demethanizing towers of compression of the compressed machine of the overhead stream of deethanizing column separate with the absorption agent contact;
2) the cat head gaseous stream carrying device of demethanizing tower or advance fuel gas system, the tower base stream of demethanizing tower is a rich absorbent, advance desorption tower and carry out desorb, after the overhead stream cooling of desorption tower, its liquid phase stream returns desorption tower, gaseous stream advances acetylene converter, advances ethylene rectification tower then and produces ethylene product, and the tower base stream of desorption tower is that the absorption agent after the desorb returns demethanizing tower and recycles.
The present invention is further characterized in that: the tower top pressure of demethanizing tower is in 2.0～2.0MPa scope, and tower top temperature is in-30～-38 ℃ of scopes.
The present invention is further characterized in that: the tower top pressure of desorption tower is in 2.2～2.6MPa scope, and temperature is in-16～-22 ℃ of scopes.
The present invention is further characterized in that: the laggard desorption tower of tower base stream heat exchange of the tower base stream of demethanizing tower and desorption tower.
The present invention is further characterized in that: the tower base stream of demethanizing tower is a rich absorbent, be divided into two-way after the extraction, one the tunnel enter desorption tower from the 2nd shelf theory column plate of cat head to the tower truth of a matter, enter after the tower base stream heat exchange of another road and desorption tower desorption tower from 10th～20 shelf theory column plate of cat head to the tower truth of a matter, the rich absorbent amount of wherein advancing the 2nd shelf theory column plate is 10～90 weight %, the rich absorbent amount of advancing the 10th～20 shelf theory column plate is 10～90 weight %, in the rich absorbent gross weight.
The present invention is further characterized in that: enter the demethanizing tower head tank after four sections compressions of the compressed machine of the overhead stream of deethanizing column, the gaseous stream of demethanizing tower head tank separates with the absorption agent contact with the different beds that liquid phase stream is delivered to demethanizing tower respectively.
The present invention is further characterized in that: enter the demethanizing tower head tank after four sections compressions of the compressed machine of the overhead stream of deethanizing column, the gaseous stream of demethanizing tower head tank enter demethanizing tower from 7th～13 shelf theory column plate of cat head to the tower truth of a matter, the liquid phase stream of demethanizing tower head tank enter demethanizing tower from 14th～19 shelf theory column plate of cat head to the tower truth of a matter.
The present invention is further characterized in that: the tower base stream of desorption tower is the absorption agent after the desorb, the cooling back adopts the feeding manner of sub-thread or multiply to enter the top of demethanizing tower, when adopting the sub-thread feeding manner, from demethanizing tower from the 2nd shelf theory column plate charging of cat head to the tower truth of a matter, when adopting the multiply feeding manner, respectively from demethanizing tower from 2nd layer and 4th～7 shelf theory column plate charging of cat head to the tower truth of a matter, the absorption dose that wherein advances the 2nd shelf theory column plate is 10～100 weight %, the absorption dose that advances the 4th～7 shelf theory column plate is 0～90 weight %, in the gross weight of the absorption agent after the desorb.
The present invention is further characterized in that: the tower base stream of demethanizing tower is a rich absorbent, after extracting out at the bottom of the tower of demethanizing tower, be divided into two-way, one the tunnel enter desorption tower from the 2nd shelf theory column plate of cat head to the tower truth of a matter, enter after the tower base stream heat exchange of another road and desorption tower desorption tower from 10th～20 shelf theory column plate of cat head to the tower truth of a matter.The rich absorbent amount of wherein advancing the 2nd shelf theory column plate is 10～90 weight %, and the rich absorbent amount of advancing the 10th～20 shelf theory column plate is 10～90 weight %, in the rich absorbent gross weight.
The present invention is further characterized in that: described absorption agent is selected from C
3, C
4Or C
5 +In the cut one or more, preferably propane.
Pressure of the present invention is gauge pressure.
The separation method of low carbon olefin gas of the present invention is fit to all rich full scale plants that produce low-carbon alkene, the catalytic cracking unit of especially suitable oil refining process and deriving device thereof, the MTO process unit of methanol-to-olefins, the MTP device of preparing propylene from methanol, the MTA device of methyl alcohol system aromatic hydrocarbons are preferably applied to the MTO process unit.
The present invention compared with prior art has the superiority of the following aspects:
(1) adopt method of the present invention, at low carbon olefin gas, the characteristics of MTO reactant gases especially adopt absorption agent to reclaim ethene in the demethanizing cat head tail gas substantially, improve the rate of recovery of ethene, reduce the loss of propane simultaneously.
(2) adopt method of the present invention, desorption tower is set, the absorption agent of demethanizing tower not only can be provided, and can the absorption agent in the demethanizing tower be desorbed, return demethanizing tower again, finished recycling of absorption agent.And can reduce the feed loading of depropanizing tower and propylene rectification tower, reduce the device gross investment.
(3) adopt method of the present invention, the demethanizing tower system can adopt C
3, C
4And C
5 +Make absorption agent Deng one or more of cut, have higher separation efficiency.
(4) adopt method of the present invention, be provided with the different feed entrance point of absorption agent, adopt sub-thread or multiply feeding manner, improved the efficient of demethanizing tower, increased the handiness of operation in the demethanizing tower system.
The present invention is described further below in conjunction with the drawings and specific embodiments.But do not limit the scope of the invention.
Accompanying drawing and description of drawings
Fig. 1 is a kind of MTO reaction gas of the present invention separation processes principle flow chart.
Fig. 2 is a kind of demethanizing tower of the present invention and desorption tower basic flowsheet of coal preparation.
Among the figure: 1-MTO reaction gas, 2-deethanizing column, 3-deethanizer bottoms stream, four sections on 4-compressor, 5-demethanizing tower, 6-demethanizing cat head gaseous stream, the 7-desorption tower, 8-acetylene converter, 9-ethylene rectification tower, the 10-ethylene product, 11-ethane logistics, four sections compressed gass of 12-, 13-demethanizing tower head tank, the air cooling of 14-demethanizing cat head is device but, 15-fuel gas, 16-demethanizing cat head separatory jar, the air cooling of 17-desorb cat head is device but, 18-desorb overhead gas, 19-desorb return tank of top of the tower, 20-desorption tower bottom reboiler, oil first water cooler at the bottom of the 21-desorption tower, 22-desorption tower feed exchanger, oil second water cooler at the bottom of the 23-desorption tower, 24-demethanizing tower bottom reboiler.
Embodiment
As shown in Figure 1, through three sections compressions of compressor, washing, alkali cleaning/washing and dried MTO reaction gas 1, enter deethanizing column 2, with C
2Following component and C
3Above component is separated.Deethanizer bottoms stream 3 is delivered to depropanizing tower, propylene rectification tower, isolates propylene product.Become four sections compressed gass 12 after four section 4 compression of the compressed machine of the overhead stream of deethanizing column 2, four sections compressed gass 12 are through the laggard demethanizing tower head tank of Quench gas-liquid flash separation continuously step by step, gas phase and liquid phase are advanced demethanizing tower 5 different positionss respectively, carry out hydrogen in demethanizing tower 5, methane separates with carbon two components.The tower top pressure of demethanizing tower 5 is in 2.0～3.0MPa scope, and tower top temperature is in-30～-38 ℃ of scopes.Enter demethanizing tower 5 tops as absorption agent from desorption tower 7 bottoms, when device went into operation, absorption agent can be introduced by device is outer.During unit normal run, absorption agent can be by replenishing at the bottom of the propylene rectification tower.Demethanizing cat head gaseous stream 6 (mainly being hydrogen and methane) after cold is reclaimed in throttling, gas phase carrying device or advance fuel gas system.
Demethanizing tower 5 bottoms stream enter desorption tower 7 after the tower base stream heat exchange of desorption tower feed exchanger 22 and desorption tower 7, finish C in desorption tower 7
2With separating of propane.The tower top pressure of desorption tower 7 is in 2.2～2.6MPa scope, and temperature is in-16～-22 ℃ of scopes.
Fig. 2 is a kind of demethanizing tower of the present invention and desorption tower basic flowsheet of coal preparation.As shown in Figure 2, four sections compressed gass 12 enter demethanizing tower head tank 13 through continuously step by step after the Quench, and the gas phase that goes out demethanizing tower head tank 13 is carried out hydrogen, methane etc. and C with the different beds that liquid phase stream is delivered to demethanizing tower 5 respectively
2The separation of component, absorption agent advances demethanizer column overhead, and the ethene in the cat head tail gas is reclaimed in maximization.Be generally speaking, the gaseous stream of demethanizing tower head tank 13 enter demethanizing tower 5 from 7th～13 shelf theory column plate of cat head to the tower truth of a matter, the liquid phase stream of demethanizing tower head tank 13 enter demethanizing tower 5 from 14th～19 shelf theory column plate of cat head to the tower truth of a matter.The tower base stream of demethanizing tower 5 is a rich absorbent, be divided into two-way after the extraction, one the tunnel enter desorption tower 7 from the 2nd shelf theory column plate of cat head to the tower truth of a matter, another road after the tower base stream heat exchange of desorption tower feed exchanger 22 and desorption tower 7, enter desorption tower 7 from 10th～20 shelf theory column plate of cat head to the tower truth of a matter, in desorption tower 7, finish C
2With separating of propane.The rich absorbent amount of wherein advancing the 2nd shelf theory column plate is 10～90 weight %, and the rich absorbent amount of advancing the 10th～20 shelf theory column plate is 10～90 weight %, in the rich absorbent gross weight.
The tower base stream of demethanizing tower 5 advances desorption tower 7 after the tower base stream heat exchange of desorption tower feed exchanger 22 and desorption tower 7.In desorption tower, finish C
2With separating of propane.Desorption tower 7 overhead streams but enter desorption tower top return tank 19 after device 17 coolings through the air cooling of desorb cat head, and the liquid phase in the desorb return tank of top of the tower 19 is returned desorption tower 7 as backflow, and the gas phase in the desorb return tank of top of the tower 19 is a desorb overhead gas 18.The desorption tower bottoms stream is passed through oil first water cooler 21 at the bottom of the desorption tower successively, after oil second water cooler 23 cools off at the bottom of desorption tower feed exchanger 22 and the desorption tower, adopt the feeding manner of sub-thread or multiply to advance demethanizing tower 5 cats head, be two strands of feeding manners of employing shown in Fig. 2, recycle as absorption agent, when adopting the sub-thread charging from demethanizing tower 5 from the 2nd shelf theory column plate charging of cat head to the tower truth of a matter, when adopting the multiply charging respectively from demethanizing tower 5 from 2nd layer and 4th～7 shelf theory column plate charging of cat head to the tower truth of a matter, the absorption dose that wherein advances the 2nd shelf theory column plate is 10～100 weight %, the absorption dose that advances the 4th～7 shelf theory column plate is 0～90 weight %, in the gross weight of the absorption agent after the desorb.
Absorption agent of the present invention can be selected from C
3, C
4Or C
5 +In the cut one or more, preferably propane.
The demethanizing cat head gaseous stream 6 of demethanizing tower 5 is through the air cooling of demethanizing cat head but after device 14 cooling, advancing demethanizing cat head separatory jar 16 separates, the bottom of demethanizing cat head separatory jar 16 is a liquid phase stream, return demethanizing tower 5, the top of demethanizing cat head separatory jar 16 is that gaseous stream acts as a fuel pneumatic transmission to device.
5 ends of demethanizing tower, be provided with demethanizing tower bottom reboiler 24, uses three sections compressed gass or low-temperature water heating as thermal source, and tower base stream is delivered to desorption tower 7.
7 ends of desorption tower, be provided with desorption tower bottom reboiler 20, uses low-pressure steam or low-temperature water heating as thermal source.
Claims (10)
1. the separation method of a low carbon olefin gas is characterized in that comprising the steps:
1) enters deethanizing column after compressed, washing of low carbon olefin gas raw material and the drying, the tower base stream of deethanizing column is delivered to depropanizing tower, propylene rectification tower, isolate propylene product, four sections laggard demethanizing towers of compression of the compressed machine of the overhead stream of deethanizing column separate with the absorption agent contact;
2) the cat head gaseous stream carrying device of demethanizing tower or advance fuel gas system, the tower base stream of demethanizing tower is a rich absorbent, enter desorption tower and carry out desorb, after the overhead stream cooling of desorption tower, its liquid phase stream returns desorption tower, gaseous stream advances acetylene converter, advances ethylene rectification tower then and produces ethylene product, and the tower base stream of desorption tower is that the absorption agent after the desorb returns demethanizing tower and recycles.
2. method according to claim 1 is characterized in that: the tower top pressure of demethanizing tower is in 2.0～3.0MPa scope; Tower top temperature is in-30～-38 ℃ of scopes.
3. method according to claim 1 is characterized in that: the tower top pressure of desorption tower is in 2.2～2.6MPa scope; Temperature is in-16～-22 ℃ of scopes.
4. method according to claim 1 is characterized in that: the laggard desorption tower of tower base stream heat exchange of the tower base stream of demethanizing tower and desorption tower.
5. method according to claim 1, it is characterized in that: the tower base stream of demethanizing tower is a rich absorbent, be divided into two-way after the extraction, one the tunnel enter desorption tower from the 2nd shelf theory column plate of cat head to the tower truth of a matter, enter after the tower base stream heat exchange of another road and desorption tower desorption tower from 10th～20 shelf theory column plate of cat head to the tower truth of a matter, the rich absorbent amount of wherein advancing the 2nd shelf theory column plate is 10～90 weight %, the rich absorbent amount of advancing the 10th～20 shelf theory column plate is 10～90 weight %, in the rich absorbent gross weight.
6. method according to claim 1, it is characterized in that: enter the demethanizing tower head tank after four sections compressions of the compressed machine of the overhead stream of deethanizing column, the gaseous stream of demethanizing tower head tank separates with the absorption agent contact with the different beds that liquid phase stream is delivered to demethanizing tower respectively.
7. method according to claim 1, it is characterized in that: enter the demethanizing tower head tank after four sections compressions of the compressed machine of the overhead stream of deethanizing column, the gaseous stream of demethanizing tower head tank enter demethanizing tower from 7th～13 shelf theory column plate of cat head to the tower truth of a matter, the liquid phase stream of demethanizing tower head tank enter demethanizing tower from 14th～19 shelf theory column plate of cat head to the tower truth of a matter.
8. method according to claim 1, it is characterized in that: the tower base stream of desorption tower is the absorption agent after the desorb, the feeding manner of employing sub-thread or multiply enters the top of demethanizing tower after heat exchange, when adopting the sub-thread feeding manner, from demethanizing tower from the 2nd shelf theory column plate charging of cat head to the tower truth of a matter, when adopting the multiply feeding manner, respectively from demethanizing tower from 2nd layer and 4th～7 shelf theory column plate charging of cat head to the tower truth of a matter, the absorption dose that wherein advances the 2nd shelf theory column plate is 10～100 weight %, the absorption dose that advances the 4th～7 shelf theory column plate is 0～90 weight %, in the gross weight of the absorption agent after the desorb.
9. method according to claim 1 is characterized in that: described absorption agent is selected from C
3, C
4Or C
5 +In the cut one or more.
10. according to claim 1 or 9 described methods, it is characterized in that: described absorption agent is a propane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010188717.5A CN102267850B (en) | 2010-06-02 | 2010-06-02 | Method for separating light olefins gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010188717.5A CN102267850B (en) | 2010-06-02 | 2010-06-02 | Method for separating light olefins gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102267850A true CN102267850A (en) | 2011-12-07 |
| CN102267850B CN102267850B (en) | 2014-03-26 |
Family
ID=45050333
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010188717.5A Active CN102267850B (en) | 2010-06-02 | 2010-06-02 | Method for separating light olefins gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102267850B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242123A (en) * | 2012-02-10 | 2013-08-14 | 中国石油化工股份有限公司 | Method for separating low-carbon olefin gas |
| CN103351271A (en) * | 2013-06-28 | 2013-10-16 | 中国石油集团东北炼化工程有限公司吉林设计院 | Device for recycling ethylene through solvent absorption method |
| CN104419465A (en) * | 2013-09-10 | 2015-03-18 | 中国石油化工股份有限公司 | Dry gas recovery system and dry gas recovery method for refinery plant |
| CN104419464A (en) * | 2013-09-10 | 2015-03-18 | 中国石油化工股份有限公司 | Dry gas recovery system and dry gas recovery method for refinery plant |
| CN104419466A (en) * | 2013-09-10 | 2015-03-18 | 中国石油化工股份有限公司 | Dry gas recovery system and dry gas recovery method for refinery plant |
| CN104560194A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Refinery saturated dry gas recovery system and recovery method |
| CN106232206A (en) * | 2014-04-22 | 2016-12-14 | 国际壳牌研究有限公司 | The method being reclaimed methane by the gas stream containing methane and ethylene |
| WO2018225908A1 (en) * | 2017-06-08 | 2018-12-13 | 주식회사 엘지화학 | Ethylene separation process and separation apparatus |
| CN110950733A (en) * | 2018-09-27 | 2020-04-03 | 中国石油天然气股份有限公司 | Separation device and method for methanol-to-olefin gas |
| CN112760128A (en) * | 2019-11-01 | 2021-05-07 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
| CN115055132A (en) * | 2022-06-15 | 2022-09-16 | 天津大学 | Production process and device for preparing ethylene by ethanol dehydration |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1157280A (en) * | 1996-10-29 | 1997-08-20 | 倪进方 | Light hydrocarbon separation method capable of raising ethylene recovery |
| WO2001025174A1 (en) * | 1999-10-04 | 2001-04-12 | Uop Llc | Process for producing ethylene |
| CN1939881A (en) * | 2005-09-29 | 2007-04-04 | 中国石油化工集团公司 | Recovery of low-carbon olefine from feed gas |
| CN101367697A (en) * | 2008-10-15 | 2009-02-18 | 上海惠生化工工程有限公司 | Separation method for light hydrocarbon products in MTO/MTP reaction products |
| CN101445419A (en) * | 2007-11-27 | 2009-06-03 | 上海惠生化工工程有限公司 | Method for separating lower hydrocarbon containing light gas by combining distillation and solvent absorption |
-
2010
- 2010-06-02 CN CN201010188717.5A patent/CN102267850B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1157280A (en) * | 1996-10-29 | 1997-08-20 | 倪进方 | Light hydrocarbon separation method capable of raising ethylene recovery |
| WO2001025174A1 (en) * | 1999-10-04 | 2001-04-12 | Uop Llc | Process for producing ethylene |
| CN1939881A (en) * | 2005-09-29 | 2007-04-04 | 中国石油化工集团公司 | Recovery of low-carbon olefine from feed gas |
| CN101445419A (en) * | 2007-11-27 | 2009-06-03 | 上海惠生化工工程有限公司 | Method for separating lower hydrocarbon containing light gas by combining distillation and solvent absorption |
| CN101367697A (en) * | 2008-10-15 | 2009-02-18 | 上海惠生化工工程有限公司 | Separation method for light hydrocarbon products in MTO/MTP reaction products |
Non-Patent Citations (1)
| Title |
|---|
| 陈香生等: "煤基甲醇制烯烃(MTO) 工艺生产低碳烯烃的工程技术及投资分析", 《煤化工》 * |
Cited By (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242123A (en) * | 2012-02-10 | 2013-08-14 | 中国石油化工股份有限公司 | Method for separating low-carbon olefin gas |
| CN103242123B (en) * | 2012-02-10 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of separation method of low carbon olefin gas |
| CN103351271A (en) * | 2013-06-28 | 2013-10-16 | 中国石油集团东北炼化工程有限公司吉林设计院 | Device for recycling ethylene through solvent absorption method |
| CN104419464B (en) * | 2013-09-10 | 2017-01-11 | 中国石油化工股份有限公司 | Dry gas recovery system and dry gas recovery method for refinery plant |
| CN104419465A (en) * | 2013-09-10 | 2015-03-18 | 中国石油化工股份有限公司 | Dry gas recovery system and dry gas recovery method for refinery plant |
| CN104419464A (en) * | 2013-09-10 | 2015-03-18 | 中国石油化工股份有限公司 | Dry gas recovery system and dry gas recovery method for refinery plant |
| CN104419466A (en) * | 2013-09-10 | 2015-03-18 | 中国石油化工股份有限公司 | Dry gas recovery system and dry gas recovery method for refinery plant |
| CN104419466B (en) * | 2013-09-10 | 2016-12-07 | 中国石油化工股份有限公司 | A kind of oil refinery dry gas recovery system and dry-gas recovery method |
| CN104419465B (en) * | 2013-09-10 | 2016-12-07 | 中国石油化工股份有限公司 | A kind of oil refinery dry gas recovery system and dry-gas recovery method |
| CN104560194A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Refinery saturated dry gas recovery system and recovery method |
| CN104560194B (en) * | 2013-10-23 | 2017-01-11 | 中国石油化工股份有限公司 | Refinery saturated dry gas recovery system and recovery method |
| CN106232206A (en) * | 2014-04-22 | 2016-12-14 | 国际壳牌研究有限公司 | The method being reclaimed methane by the gas stream containing methane and ethylene |
| WO2018225908A1 (en) * | 2017-06-08 | 2018-12-13 | 주식회사 엘지화학 | Ethylene separation process and separation apparatus |
| KR20180134011A (en) * | 2017-06-08 | 2018-12-18 | 주식회사 엘지화학 | Method and Apparatus of separating ethylene |
| KR102162297B1 (en) | 2017-06-08 | 2020-10-06 | 주식회사 엘지화학 | Method and Apparatus of separating ethylene |
| US10889535B2 (en) | 2017-06-08 | 2021-01-12 | Lg Chem, Ltd. | Process and apparatus for separating ethylene |
| CN110950733A (en) * | 2018-09-27 | 2020-04-03 | 中国石油天然气股份有限公司 | Separation device and method for methanol-to-olefin gas |
| CN110950733B (en) * | 2018-09-27 | 2023-09-26 | 中国石油天然气股份有限公司 | Separation device and method for preparing olefin gas from methanol |
| CN112760128A (en) * | 2019-11-01 | 2021-05-07 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
| CN112760128B (en) * | 2019-11-01 | 2022-04-12 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
| CN115055132A (en) * | 2022-06-15 | 2022-09-16 | 天津大学 | Production process and device for preparing ethylene by ethanol dehydration |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102267850B (en) | 2014-03-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102267850B (en) | Method for separating light olefins gas | |
| CN103242123B (en) | A kind of separation method of low carbon olefin gas | |
| CN101367697B (en) | Separation method for light hydrocarbon products in MTO/MTP reaction products | |
| CN101559320B (en) | Separation method of Fischer-Tropsch synthesis gas by combining rectification and solvent absorption | |
| CN102115355B (en) | Method for separating low-carbon olefins | |
| CN103787814B (en) | A kind of middle cold solvent of lower carbon number hydrocarbons washes separation method | |
| CN203794811U (en) | Reaction product separation system for methanol-to-propylene and methanol-to-olefin | |
| CN102304010B (en) | Method for separating low carbon olefin mixed gas by rectifying and absorbing | |
| CN101747128B (en) | Separation method for preparing low-carbon olefin by conversion of methanol | |
| CN102206128A (en) | Separation method for low-carbon olefin prepared from oxygen-containing compound | |
| CN102304009B (en) | Method and system for separating MTP (Methanol to Propylene) reaction mixed gas | |
| CN107827698B (en) | Non-cryogenic separation method and system for ethylene-containing pyrolysis gas | |
| CN103880577A (en) | Reaction product separation system for production of propylene and olefins by using methanol | |
| CN103965009B (en) | The method of the hydrocarbonylation tail gas ethylbenzene after a kind of catalysis drying gas preparation of styrene | |
| CN101215214B (en) | Combined technique for preparing olefin by using refining plant C4 and catalytic dry gas as raw material | |
| CN109678641A (en) | A kind of separation method and device of Catalyst for Oxidative Coupling of Methane reaction gas | |
| CN102351629B (en) | Method for producing propylene and high-octane gasoline from methanol | |
| CN111004079B (en) | Separation method and device for reaction gas for preparing ethylene by oxidative coupling of methane | |
| CN103073378A (en) | Low-temperature methanol washing and alkane dehydrogenation combination system and coupling system of low-temperature methanol washing and alkane dehydrogenation combination system and alkene separation system | |
| CN111116300A (en) | Shallow cooling separation device and method for preparing olefin from synthesis gas | |
| CN103467231B (en) | Process for absorption and recycling of ethylene in olefin reaction products prepared from methanol | |
| CN101225013A (en) | Separation device and method for producing light olefin gas products by conversion of methanol and dimethyl ether | |
| CN111116297A (en) | Separation device and method for preparing olefin from synthesis gas | |
| CN106631664A (en) | Separation method for methanol-to-olefin reaction gas | |
| CN203079879U (en) | Low-temperature methanol washing and alkane dehydrogenizing combination system and coupling system of olefin separation system and combination system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent of invention or patent application | ||
| CB02 | Change of applicant information |
Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |