CN102267850B - Method for separating light olefins gas - Google Patents
Method for separating light olefins gas Download PDFInfo
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- CN102267850B CN102267850B CN201010188717.5A CN201010188717A CN102267850B CN 102267850 B CN102267850 B CN 102267850B CN 201010188717 A CN201010188717 A CN 201010188717A CN 102267850 B CN102267850 B CN 102267850B
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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 (is mainly methyl alcohol, ethanol, dme, C with oxygenatedchemicals
4～C
10alkylol cpd or its mixture etc.) be raw material, in generation, take low-carbon alkene in the successive reaction and regenerative process of main streams (being mainly ethene and propylene), 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 technique of light naphthar raw material at present.Due to the shortage of crude resources and the raising day by day of price, it is not enough that naphtha resource has 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, 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 that to take ethene, propylene be main reaction product, just be subject to extensive attention both domestic and external, in industrialization phase.
The oxygen-containing organic compound that methyl alcohol or dme be representative of take is typical oxygen-containing organic compound, mainly by synthetic gas coal-based or Sweet natural gas base, is produced.The oxygen-containing organic compound that is representative in order to methyl alcohol is that raw material production be take ethene and propylene (main patent is US Patent No. P6166282, USP5744680 as main low-carbon alkene technique mainly contains the MTO technology of American UOP company at present; 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 technique (EP0448000A, DE233975A1) and the Dalian Chemistry and Physics Institute of the Chinese Academy of Sciences.
The reaction characteristics of oxygenatedchemicals (current typical case adopt be methyl alcohol) preparing low-carbon olefins technique (MTO) is that rapid reaction, strong heat release and alcohol agent are lower frequently, is react and regenerate in the dense fluidized bed bioreactor of continuous reaction-regeneration.The high-temperature oil gas that is rich in the low-carbon alkenes such as ethene and propylene that reaction generates, need to carry out chilling and washing, removes wherein after catalyzer and cooling, is sent to bottom olefin separation system and carries out separation.The object 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 in MTO gas, hydrogen and methane content are lower, and propylene and propane content are apparently higher than propylene and propane content in naphtha cracking gas.The cracked gas that how this part is rich in to the low-carbon alkenes such as ethene and propylene carries out separated, improves the yield of object product ethene and propylene, receives publicity always.
WO01/25174 has disclosed a kind of method of producing ethene, and the principal feature of the method is: (1) adopts 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 demethanizer overhead, thereby improved demethanizing tower top temperature, avoid adopting ethene cold; (3) in order to reclaim the ethene in demethanizing overhead gas, this gas is sent into pressure-variable adsorption facility, separation of methane, hydrogen and ethene, by the ethene Returning oxidation reactor outlet material reclaiming.This separation method facility investment is low, but owing to having adopted PSA technology, schedule of operation is more complicated, and the workload of system maintenance is larger.
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 by sending into deethanizing column after the pre-treatment of MTO/MTP reaction product
2/ C
3sharp separation, deethanizing top gaseous 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 column tower reactor product introduction subsequent separation system; Absorption is steamed to overhead product and after cooling, send into oil-absorption tower, oil-absorption tower adopts ethane as poor absorption agent, and separate absorbent steams the ethene in column overhead product, and all the other light gas are discharged by tower top, and tower reactor product returns to absorb as rich absorbent and steams tower; Absorption steams tower tower reactor product introduction ethylene column, after tower reactor ethane component is cooling as poor absorption agent, enters oil-absorption tower.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 Recovery rate of ethylene, this invention is a kind of high Recovery rate of ethylene, the light hydrocarbon separating method of energy-conservation and low demethanizing tower load, lighter hydrocarbons are through overdraft, the gas and the liquid that after cooling and flash distillation, obtain enter respectively high pressure deethanizing column, carry out the non-clear cutting of C-2-fraction, the low product of high pressure deethanizing column tower enters low pressure deethanizing column and carries out the separated of carbon two and C3 fraction, high pressure deethanizer overhead product obtains two strands of above liquid as the charging of demethanizing tower through multistage cooling and flash distillation, the gas of knockout drum outlet is through the cooling methane absorber that enters, with liquid phase methane as absorption agent, 99.5% ethene in gas is absorbed, and methane absorber outlet at bottom liquid returns to demethanizing tower as charging, demethanizing tower reactor liquid 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 feature forming for DMTO gas, improves the flow process after four sections of compressions in conventional front-end deethanization separation process.According to this invention, between five sections of compressions and deethanizing column return tank, arrange and add hydrogen-oxygen conversion, remove the oxygen producing in acetylene and reaction regeneration process, material after condensing cooling is through deethanizing column return tank, liquid phase refluxes as deethanizing column, and gas phase enters deep cooling demethanizing system, and material is after condensing cooling, do not need to arrange the front dehydrogenation system of loaded down with trivial details ice chest, directly enter high pressure demethanizer.Adopt the separated DMTO gas of the present invention can obtain 99.5% above Recovery rate of ethylene.
In sum, the separation method of the low-carbon alkene relating in prior art, the deep cooling flow process that sequence flow, front-end deethanization flow process and predepropanization process are representative is take in employing, majority is applied to ethylene cracker, but, any flow process, for separation of methane, hydrogen and C2 hydrocarbon class all need deep cooling, all need to be provided the cold of multiple differing temps grade by propylene compressor and ethylene compressor, for example, need ethene refrigerant condenser that the cold of-100 ℃ is provided.For low temperature demethanizing, also need to have methane compressor that the cold of-135 ℃ of left and right is provided.Except complicated refrigerant condenser system, go back the ice chest equipment of Structure of need precision, these all make, and low temperature separation process flow process is complicated, investment is large.
Summary of the invention
Object of the present invention is just to provide a kind of separation method of low carbon olefin gas, to produce the object 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) compressed, the washing of low carbon olefin gas raw material and dry after enter deethanizing column, the tower base stream of deethanizing column is delivered to depropanizing tower, propylene rectification tower, isolate propylene product, the overhead stream of deethanizing column carries out separated through four sections of laggard demethanizing towers of compression of compressor with absorption agent contact;
2) the top gaseous phase logistics carrying device of demethanizing tower or enter fuel gas system, the tower base stream of demethanizing tower is rich absorbent, enter desorption tower and carry out desorb, after the overhead stream of desorption tower is cooling, its liquid phase stream returns to desorption tower, gas gas-phase objects flows to acetylene converter, then enters ethylene rectification tower and produces ethylene product, and the tower base stream of desorption tower is that the absorption agent after desorb returns to demethanizing tower and recycles.
The present invention is further characterized in that: the tower top pressure of demethanizing tower is within the scope of 2.0～2.0MPa, and tower top temperature is within the scope of-30～-38 ℃.
The present invention is further characterized in that: the tower top pressure of desorption tower is within the scope of 2.2～2.6MPa, and temperature is within the scope of-16～-22 ℃.
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 rich absorbent, after extraction, be divided into two-way, one tunnel enters the 2nd shelf theory column plate from tower top to the tower truth of a matter of desorption tower, after the tower base stream heat exchange of another road and desorption tower, enter 10th～20 shelf theory column plates from tower top to the tower truth of a matter of desorption tower, the rich absorbent amount of wherein entering the 2nd shelf theory column plate is 10～90 % by weight, the rich absorbent amount of entering 10th～20 shelf theory column plates is 10～90 % by weight, in rich absorbent gross weight.
The present invention is further characterized in that: the overhead stream of deethanizing column enters demethanizing tower head tank after four sections of compressions of compressor, and the gaseous stream of demethanizing tower head tank carries out separated with the different beds that liquid phase stream is delivered to respectively demethanizing tower with absorption agent contact.
The present invention is further characterized in that: the overhead stream of deethanizing column enters demethanizing tower head tank after four sections of compressions of compressor, the gaseous stream of demethanizing tower head tank enters 7th～13 shelf theory column plates from tower top to the tower truth of a matter of demethanizing tower, and the liquid phase stream of demethanizing tower head tank enters 14th～19 shelf theory column plates from tower top to the tower truth of a matter of demethanizing tower.
The present invention is further characterized in that: the tower base stream of desorption tower is the absorption agent after desorb, the feeding manner of cooling rear employing sub-thread or multiply enters the top of demethanizing tower, while adopting sub-thread feeding manner, the 2nd shelf theory column plate charging from tower top to the tower truth of a matter from demethanizing tower, while adopting multiply feeding manner, respectively from the 2nd layer and 4th～7 shelf theory column plate chargings from tower top to the tower truth of a matter of demethanizing tower, the absorption dose that wherein enters the 2nd shelf theory column plate is 10～100 % by weight, the absorption dose that enters 4th～7 shelf theory column plates is 0～90 % by weight, gross weight in the absorption agent after desorb.
The present invention is further characterized in that: the tower base stream of demethanizing tower is rich absorbent, after extracting out at the bottom of the tower of demethanizing tower, be divided into two-way, one tunnel enters the 2nd shelf theory column plate from tower top to the tower truth of a matter of desorption tower, enters 10th～20 shelf theory column plates from tower top to the tower truth of a matter of desorption tower after the tower base stream heat exchange of another road and desorption tower.The rich absorbent amount of wherein entering the 2nd shelf theory column plate is 10～90 % by weight, and the rich absorbent amount of entering 10th～20 shelf theory column plates is 10～90 % by weight, in rich absorbent gross weight.
The present invention is further characterized in that: described absorption agent is selected from C
3, C
4or C
5 +one or more in cut, preferably propane.
Pressure of the present invention is gauge pressure.
The separation method of low carbon olefin gas of the present invention is applicable to all rich full scale plants that produce low-carbon alkene, the catalytic cracking unit of especially applicable oil refining process and deriving device, the MTO process unit of methanol-to-olefins are, the MTA device of the MTP device of preparing propylene from methanol, Methanol aromatic hydrocarbons is preferably applied to MTO process unit.
The present invention compared with prior art has the superiority of the following aspects:
(1) adopt method of the present invention, for low carbon olefin gas, especially the feature of MTO reactant gases, adopts absorption agent to reclaim substantially the ethene in demethanizing tower top tail gas, improves the rate of recovery of ethene, reduces 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 the absorption agent in demethanizing tower can be desorbed, then return to demethanizing tower, completed recycling of absorption agent.And can reduce the feed loading of depropanizing tower and propylene rectification tower, reduce device gross investment.
(3) adopt method of the present invention, demethanizing tower system can adopt C
3, C
4and C
5 +deng one or more of cut, make absorption agent, there is higher separation efficiency.
(4) adopt method of the present invention, in demethanizing tower system, be provided with the different feed entrance point of absorption agent, adopt sub-thread or multiply feeding manner, improved the efficiency of demethanizing tower, increased the handiness of operation.
Below in conjunction with the drawings and specific embodiments, the present invention is described further.But do not limit the scope of the invention.
Accompanying drawing and accompanying drawing explanation
Fig. 1 is the basic flowsheet of coal preparation of a kind of MTO reaction gas of the present invention separation.
Fig. 2 is a kind of demethanizing tower of the present invention and desorption tower basic flowsheet of coal preparation.
In figure: 1-MTO reaction gas, 2-deethanizing column, 3-deethanizer bottoms stream, four sections, 4-compressor, 5-demethanizing tower, the logistics of 6-demethanizing top gaseous phase, 7-desorption tower, 8-acetylene converter, 9-ethylene rectification tower, 10-ethylene product, 11-ethane logistics, tetra-sections of compressed gass of 12-, 13-demethanizing tower head tank, 14-demethanizing tower top gas water cooler, 15-fuel gas, 16-demethanizing tower top separatory tank, 17-desorption tower top gas water cooler, 18-desorption tower top gas, 19-desorb return tank of top of the tower, 20-desorption tower bottom reboiler, oil the first water cooler at the bottom of 21-desorption tower, 22-desorption tower feed exchanger, oil the second water cooler at the bottom of 23-desorption tower, 24-demethanizing tower bottom reboiler.
Embodiment
As shown in Figure 1, through three sections of compressions of compressor, washing, alkali cleaning/washing and dried MTO reaction gas 1, enter deethanizing column 2, by C
2following component and C
3above component is separated.Deethanizer bottoms stream 3 is delivered to depropanizing tower, propylene rectification tower, isolates propylene product.The overhead stream of deethanizing column 2 becomes four sections of compressed gass 12 after four section of 4 compression of compressor, four sections of 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 entered respectively demethanizing tower 5 different positionss, carry out hydrogen, methane is separated with carbon two components in demethanizing tower 5.The tower top pressure of demethanizing tower 5 is within the scope of 2.0～3.0MPa, and tower top temperature is within the scope of-30～-38 ℃.From desorption tower 7 bottoms, enter demethanizing tower 5 tops as absorption agent, during start up, absorption agent can be introduced by device is outer.During unit normal run, absorption agent can be by supplementing at the bottom of propylene rectification tower.Demethanizing top gaseous phase logistics 6 (being mainly hydrogen and methane) after cold is reclaimed in throttling, gas phase carrying device or enter 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, in desorption tower 7, complete C
2separated with propane.The tower top pressure of desorption tower 7 is within the scope of 2.2～2.6MPa, and temperature is within the scope of-16～-22 ℃.
Desorption tower 7 overhead streams enter desorption tower top return tank 19 after desorption tower top gas water cooler 17 is cooling, liquid phase in desorb return tank of top of the tower 19 is returned to desorption tower 7 as backflow, gas phase in desorb return tank of top of the tower 19 is entered acetylene converter 8 as desorption tower top gas 18, optionally remove acetylene, propine, propadiene, guarantee polymer grade ethylene product requirement.From acetylene converter 8 logistics out, enter ethylene rectification tower 9 and produce ethylene product 10, ethylene rectification tower 9 tower base streams are mainly ethane logistics 11, or as ethane product, or deliver to fuel gas system.
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 of compressed gass 12, through continuously step by step after Quench, enter demethanizing tower head tank 13, go out the gas phase of demethanizing tower head tank 13 and different beds that liquid phase stream is delivered to respectively demethanizing tower 5 and carry out hydrogen, methane etc. and C
2the separation of component, absorption agent enters demethanizer column overhead, maximizes the ethene reclaiming in tower top tail gas.Be generally, the gaseous stream of demethanizing tower head tank 13 enters 7th～13 shelf theory column plates from tower top to the tower truth of a matter of demethanizing tower 5, and the liquid phase stream of demethanizing tower head tank 13 enters 14th～19 shelf theory column plates from tower top to the tower truth of a matter of demethanizing tower 5.The tower base stream of demethanizing tower 5 is rich absorbent, after extraction, be divided into two-way, one tunnel enters the 2nd shelf theory column plate from tower top to the tower truth of a matter of desorption tower 7, another road enters 10th～20 shelf theory column plates from tower top to the tower truth of a matter of desorption tower 7 after the tower base stream heat exchange of desorption tower feed exchanger 22 and desorption tower 7, in desorption tower 7, completes C
2separated with propane.The rich absorbent amount of wherein entering the 2nd shelf theory column plate is 10～90 % by weight, and the rich absorbent amount of entering 10th～20 shelf theory column plates is 10～90 % by weight, in rich absorbent gross weight.
The tower base stream of demethanizing tower 5, after the tower base stream heat exchange of desorption tower feed exchanger 22 and desorption tower 7, enters desorption tower 7.In desorption tower, complete C
2separated with propane.Desorption tower 7 overhead streams enter desorption tower top return tank 19 after desorption tower top gas water cooler 17 is cooling, and the liquid phase in desorb return tank of top of the tower 19 is returned to desorption tower 7 as backflow, and the gas phase in desorb return tank of top of the tower 19 is desorption tower top gas 18.Desorption tower bottoms stream is passed through oil the first water cooler 21 at the bottom of desorption tower successively, at the bottom of desorption tower feed exchanger 22 and desorption tower oil the second water cooler 23 cooling after, adopt the feeding manner of sub-thread or multiply to enter demethanizing tower 5 tower tops, shown in Fig. 2, be two strands of feeding manners of employing, as absorption agent, recycle, while adopting sub-thread charging from the 2nd shelf theory column plate charging from tower top to the tower truth of a matter of demethanizing tower 5, while adopting multiply charging respectively from the 2nd layer and 4th～7 shelf theory column plate chargings from tower top to the tower truth of a matter of demethanizing tower 5, the absorption dose that wherein enters the 2nd shelf theory column plate is 10～100 % by weight, the absorption dose that enters 4th～7 shelf theory column plates is 0～90 % by weight, gross weight in the absorption agent after desorb.
Absorption agent of the present invention can be selected from C
3, C
4or C
5 +in cut one or more, preferably propane.
The demethanizing top gaseous phase logistics 6 of demethanizing tower 5 is after demethanizing tower top gas water cooler 14 is cooling, enter demethanizing tower top separatory tank 16 and carry out separation, the bottom of demethanizing tower top separatory tank 16 is liquid phase stream, return to demethanizing tower 5, the top of demethanizing tower top separatory tank 16 is that gaseous stream is delivered to outside device as fuel gas.
5 ends of demethanizing tower, are provided with demethanizing tower bottom reboiler 24, use three sections of 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, are provided with desorption tower bottom reboiler 20, use low-pressure steam or low-temperature water heating as thermal source.
Claims (9)
1. a separation method for low carbon olefin gas, is characterized in that comprising the steps:
1) compressed, the washing of low carbon olefin gas raw material and dry after enter deethanizing column, the tower base stream of deethanizing column is delivered to depropanizing tower, propylene rectification tower, isolate propylene product, the overhead stream of deethanizing column carries out separated through four sections of laggard demethanizing towers of compression of compressor with absorption agent contact;
2) the top gaseous phase logistics carrying device of demethanizing tower or enter fuel gas system, the tower base stream of demethanizing tower is rich absorbent, enter desorption tower and carry out desorb, after the overhead stream of desorption tower is cooling, its liquid phase stream returns to desorption tower, gas gas-phase objects flows to acetylene converter, then enters ethylene rectification tower and produces ethylene product, and the tower base stream of desorption tower is that the absorption agent after desorb returns to demethanizing tower and recycles;
Described absorption agent is selected from C
3, C
4or C
5 +one or more in cut.
2. method according to claim 1, is characterized in that: the tower top pressure of demethanizing tower is within the scope of 2.0～3.0MPa; Tower top temperature is within the scope of-30～-38 ℃.
3. method according to claim 1, is characterized in that: the tower top pressure of desorption tower is within the scope of 2.2～2.6MPa; Temperature is within the scope of-16～-22 ℃.
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 rich absorbent, after extraction, be divided into two-way, one tunnel enters the 2nd shelf theory column plate from tower top to the tower truth of a matter of desorption tower, after the tower base stream heat exchange of another road and desorption tower, enter 10th～20 shelf theory column plates from tower top to the tower truth of a matter of desorption tower, the rich absorbent amount of wherein entering the 2nd shelf theory column plate is 10～90 % by weight, the rich absorbent amount of entering 10th～20 shelf theory column plates is 10～90 % by weight, in rich absorbent gross weight.
6. method according to claim 1, it is characterized in that: the overhead stream of deethanizing column enters demethanizing tower head tank after four sections of compressions of compressor, the gaseous stream of demethanizing tower head tank carries out separated with the different beds that liquid phase stream is delivered to respectively demethanizing tower with absorption agent contact.
7. method according to claim 1, it is characterized in that: the overhead stream of deethanizing column enters demethanizing tower head tank after four sections of compressions of compressor, the gaseous stream of demethanizing tower head tank enters 7th～13 shelf theory column plates from tower top to the tower truth of a matter of demethanizing tower, and the liquid phase stream of demethanizing tower head tank enters 14th～19 shelf theory column plates from tower top to the tower truth of a matter of demethanizing tower.
8. method according to claim 1, it is characterized in that: the tower base stream of desorption tower is the absorption agent after desorb, after heat exchange, adopt the feeding manner of sub-thread or multiply to enter the top of demethanizing tower, while adopting sub-thread feeding manner, the 2nd shelf theory column plate charging from tower top to the tower truth of a matter from demethanizing tower, while adopting multiply feeding manner, respectively from the 2nd layer and 4th～7 shelf theory column plate chargings from tower top to the tower truth of a matter of demethanizing tower, the absorption dose that wherein enters the 2nd shelf theory column plate is 10～100 % by weight, the absorption dose that enters 4th～7 shelf theory column plates is 0～90 % by weight, gross weight in the absorption agent after desorb.
9. method according to claim 1, is characterized in that: described absorption agent is propane.
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| 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 |
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| 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 |
| 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 |
| US10239013B2 (en) * | 2014-04-22 | 2019-03-26 | Shell Oil Company | Process for recovering methane from a gas stream comprising methane and ethylene |
| KR102162297B1 (en) | 2017-06-08 | 2020-10-06 | 주식회사 엘지화학 | Method and Apparatus of separating ethylene |
| 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 |
| 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 |
| CN115055132B (en) * | 2022-06-15 | 2022-12-16 | 天津大学 | Production process and device for preparing ethylene by ethanol dehydration |
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