CN102503757A - Process flow for separating low-carbon hydrocarbons and separating gas during production of olefins (M-OS/MTO) from methanol - Google Patents
Process flow for separating low-carbon hydrocarbons and separating gas during production of olefins (M-OS/MTO) from methanol Download PDFInfo
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Abstract
The invention provides a non-cryogenic oil absorption separation method for a mixture of low-carbon hydrocarbons, which is used for separating the mixture of the hydrocarbons from gas during production of olefins from methanol. Methane/hydrogen can be separated from heavy components, namely C2 and above by absorbing fractions of the C2 and above by adopting two or more strands of absorbing agents. According to the method disclosed by the invention, an absorbing agent separating tower is increased before a demethanization tower, one strand of material flow, which is separated from the tower is taken as a main absorbing agent of the demethanization tower for absorbing the C2 and C3, the strand of the absorbing agent is the mixture of the fractions, which is from the former system and needs to be separated, and circulation is not required. The second strand of the absorbing agent of the demethanization tower is from a system including a depropanization tower and a debutanization tower, and the absorption effect is further enhanced. Compared with the prior art, the method can greatly reduce the using quantity of the circulating absorbing agents; moreover, the multiple strands of the absorbing agents are adopted, equipment investment and energy consumption are significantly reduced, the recovery rate of ethylene and propylene is further improved; and furthermore, the flow is simple, the operation cost is low, and the operation is safe and reliable.
Description
Technical field
This lower carbon number hydrocarbons separates and methanol-to-olefins (M-OS/MTO) gas separating technology flow process is applicable to oxide compound system alkene, hydrocarbon cracking, and the hydro carbons catalyzed reaction is produced alkene, also is adapted to traditional petrochemical complex ethene field simultaneously.
Background technology
Most of intermediates and the finished product are basic material with alkene and aromatic hydrocarbons all in the petrochemical industry.Ethylene unit is a main production plant of producing alkene (ethene, propylene, divinyl) and aromatic hydrocarbons.Past is mainly produced alkene by petroleum naphtha through pyrolysis in tubular furnace, because petroleum resources are in short supply, methanol-to-olefins (MTO/MTP) technology progressively is developed, and has got into industrialization phase in recent years.The methanol-to-olefins technology is made up of reaction technology and stripping technique.Reaction technology is a core with Study of Catalyst and reactor drum development and Design, is the raw material production alkene mixture with methyl alcohol; Stripping technique then is to be raw material with the reaction product, produces polymer grade ethylene and propylene product through processes such as impurity removal, compression, separation, and its core is the exploitation and the design of separation process.
Pass through converting methanol to prepare low carbon olefin gas; The product of petroleum naphtha, hydrocarbon cracking system alkene is similar in its product and the ethylene unit; All form by hydrogen, methane, carbon two, carbon three, carbon four, carbon five and above composition; Proportion of composing has certain difference, and hydrogen in methanol-to-olefins (MTO/MTP) device, methane content are lower, and the hydro carbons of carbon more than five seldom.Therefore, the separation process scheme that is adopted compares with existing ethylene unit that flow process is simple, the table of equipment number is less, does not need low temperature separation process, does not need methane or ethylene refrigeration machine, only needs propylene refrigeration to get final product.Based on the gas composition characteristics of methanol-to-olefins (MTO/MTP), its separation process scheme is suitable for adopting once adopted ethylene unit 50, the sixties used oil absorption extraction technology.
What industrialized at home Shenhua packet header MTO device promptly adopted at present is oily method for absorbing and separating.The method that oil absorption extraction technology and difference between the low temperature separation process mainly are to remove hydrogen and methane in the gaseous mixture is different.Low temperature separation process is method separation of hydrogen and the methane from splitting gas that adopts low temperature fractional condensation and low-temperature fractionation, and required coldcondition can reach (high pressure demethanizer top temperature reaches-99 ℃, and low-pressure methane removing cat head temperature reaches-134 ℃) below-90 ℃.Oil-absorption process general using C3, C4, C5 and aromatic fraction absorb carbon two and the above hydro carbons in the splitting gas and from splitting gas, isolate methane and hydrogen as absorption agent; But required coldcondition can be more than-40 ℃; Therefore whole device only need dispose-40 ℃ propylene refrigeration system; Refrigeration system is greatly simplified, can be avoided the use of the related low-temperature steel of low temperature separation process simultaneously.
But because oil-absorption process adopts a large amount of round-robin absorption agents, its energy consumption is higher, and ethene and propylene loss are bigger in cat head methane, hydrogen cut.According in the books such as Wang Songhan chief editor " ethylene unit technology ", " ethylene process and technology " about the description of oily absorption techniques; The energy consumption of producing 1 ton of alkene oil absorption extraction method is about 1.5 times of Deep Cooling Method; Secondly; Ethene and propylene loss maybe be up to 3%～6% in methane, the hydrogen cut, and because cracking temperature is high, produced the diolefine of more easy coking.Therefore, oil-absorption process was almost all replaced by separation by deep refrigeration in the sixties in 20th century.
After the sixties in 20th century, the research and the improvement of oil-absorption process are being carried out always.The Beijing Chemical Research Institute carries out the research that cold oil absorbs in the splitting gas since the seventies in 20th century; The middle cold oil absorption techniques of developing at that time is mainly used in separation regenerative furnace pyrolysis gas and pyrolysis in tubular furnace is so incensed that ethene and propylene, and chemical plant, Changzhou, Beijing Chemical Factory No. 3 etc. have set up covering device more than 10 at home.This technical matters flow process comprises: cracking, compress, remove sour gas, remove alkynes, C3 oil absorbs, the C2 cut separates and separates with the C3 cut.Its key point is that employing deethanizing Tata still carbon three is that main material absorbs C2 and above heavy constituent as absorption agent on the absorption tower, isolates noncondensable gases such as methane, hydrogen, adopts decompressor and ice chest to reclaim the lighter hydrocarbons in the tail gas simultaneously.This technology has been done certain improvement to traditional oil-absorption process; The recovery of ethene and propylene improves; The consumption of absorption agent has minimizing to a certain degree, but should technology mainly still lean on the material of back system (at the bottom of the deethanizing column) to circulate as absorption agent, and energy consumption does not obtain substantial reduction.
The oily absorption extraction technology (ALCET) that Brown&Root proposes, decarburization three front-end hydrogenations and solvent absorbing process combined before adopting.What absorption agent adopted is to be main absorption agent with C5.This technology and traditional oils absorption technique specific energy consumption mutually decrease, but the separation of demethanizing tower mainly relies on the circulation absorption agent, and for guaranteeing alkene specific absorption preferably, the amount of the circulation absorption agent that needs usually is all bigger.
The global chemico chemical construction corporation of China developed a kind of separating hydrocarbons mixture solvent absorption patent (99122104.4), select a kind of by C5 be the hydrocarbon mixture of major ingredient as absorption agent, carry out solvent absorbing and separate.The ALCET oil absorption technique of this method and Brown &Root is similar.In addition, absorption agent also is to lean on the back Analytic Tower to parse.
Lee enclose the tide and Wang Songhan in oil-absorption process having been done a large amount of research in the nineties; And on " ethylene industry ", delivered the paper that is entitled as " feasibility analysis of oily absorption extraction flow process and evaluation " in 1999, this paper is to the main evaluation index of oil-absorption process: the assimilated efficiency result of study of energy consumption and alkene has been done disclosure.Its research adopts various absorption agents to comprise that C4, C5, C6, C4 and C5 mix solvent, aromatic hydrocarbons is that main solvent has all been done to calculate and research, and has listed the assimilated efficiency of the energy consumption, ethene and the propylene that adopt various absorption agent to draw.According to the conclusion of this paper, the alkene assimilated efficiency and the energy consumption of C4 and C5 mixed solvent and C5 solvent are all better.
What industrialized Shenhua packet header MTO device adopted at present is to be the top board that main absorption agent gets into demethanizing tower with propane; C2 and above component are absorbed; Its assimilated efficiency is better, but the absorption agent consumption is more and absorption agent from subsequent separation system (propylene rectification tower tower still), the round-robin route is longer; Cause equipment such as corresponding tower bigger, investment is high, energy consumption is higher.
Except the oily absorption technique of above-mentioned some that list, in recent years, also have some patent merchants that the stripping technique of methanol-to-olefins is studied, be absorbed as the master with oil basically, the sub-thread absorption agent that adopts the back systemic circulation to return absorbs C2 and above heavy constituent.Adopting carbon four like Chinese patent 200780003084.2 is that main absorption agent, ethane, propane or the ethane/propane mixture that Chinese patent 201010607679.2 adopts the back systemic circulation to return are made absorption agent.The absorption agent that these technology are adopted basically all derives from the back system, enters into absorption tower (demethanizing tower) as the sub-thread absorption agent.For obtaining higher olefin recovery, all need guarantee the amount of certain circulation absorption agent, and the amount of circulation absorption agent there is bigger influence to the investment and the energy consumption of separation system.
Summary of the invention
The present invention is intended to overcome the defective of traditional oils absorption extraction technology and existing lighter hydrocarbons separating technology, and the lower carbon number hydrocarbons separation method of the non-deep cooling that a kind of facility investment is few, energy consumption is low, olefin recovery is high is provided.
The present invention absorbs with traditional oils and existing all kinds of lighter hydrocarbons stripping technique are compared, and its principal feature is:
(1) the multiply absorption agent is adopted on the absorption tower, adopts two strands of absorption agents in an embodiment of the present invention, and progressive absorption mode has not only strengthened the assimilation effect of absorption tower (demethanizing tower), has reduced investment and energy consumption simultaneously.
(2) one main absorber of the present invention is the main absorber of master's cut as demethanizing tower from rough segmentation is come out from splitting gas (or reaction gas) before the demethanizing tower C3, C4 mixture.This strand absorption agent itself is to treat isolating fraction mixture, avoided the increase of the energy consumption that absorption agent mainly brings from the back systemic circulation.
(3) in order further to improve the recovery of alkene, measure smaller absorption agent from depropanizing tower and/or debutanizing tower system for second strand of the present invention, major ingredient is the mixture that the above heavy constituent of C4, C5 and C5 are formed.The characteristics of this absorption agent are to go out according to the characteristic optimization of splitting gas (or reaction gas) absorption agent of different proportionings, strengthen the assimilation effect of alkene, cut down the consumption of energy.
The present invention is mainly used in lower carbon number hydrocarbons and separates, and comprises the lighter hydrocarbons cracking, the hydro carbons catalyzed reaction; The gaseous mixture of oxide compound system alkene such as alcohol, ether separates; The compositing characteristic of its gaseous mixture is the yield high (with the methanol-to-olefins is example, the mass yield of alkene about 80%) of alkene, and generates a certain amount of butylene; Produce a spot of hydrogen, methane, carbon monoxide, carbonic acid gas, other oxide compounds simultaneously, and the hydro carbons of small amount of carbon more than five.More than listed different methods produce low-carbon alkene after gas delivery all can adopt method of the present invention.Therefore, the present invention only describes with the methanol-to-olefins gas separation unit, mainly comprises following steps:
(1) reaction gas of methyl alcohol being produced through catalyzed reaction boosts to 2.0MPaG step by step, after cooling, is divided into gas-liquid two-phase, gets into dehumidification system respectively and carries out drying.
(2) dried vapour, liquid phase get into an absorption agent knockout tower, and is to send into the main absorber of the correct position on demethanizing tower top as demethanizing tower after master's cut cools off from tower still or side line extraction with C3, C4 mixture.Absorption agent knockout tower top, is isolated vapour, liquid two through separating tank and is removed demethanizing tower as charging after compression, cooling than lighter-than-air gas.
(3) second of demethanizing tower strand of absorption agent adopts C4, C5 and the above mixture of depropanizing tower and/or debutanizing tower; Send into the top of demethanizing tower and further reclaim alkene; This strand absorption agent can be provided by the self-produced hydrocarbon mixture of back system, also can be provided by the outside.
(4) second of demethanizing tower strand of absorption agent can between demethanizing tower, depropanizing tower and/or debutanizing tower, circulate (seeing accompanying drawing 1).Also can parse (seeing accompanying drawing 2) through Analytic Tower, between demethanizing tower and Analytic Tower, circulate.
When (5) utilizing two strands of absorption agents to absorb for present methanol-to-olefins gaseous mixture, demethanizing tower can only use absorption agent, cat head not to need to be provided with systems such as condensing surface, return tank, reflux pump again.If but gas composition changes greatly, after improving, systems such as condensing surface, return tank, reflux pump can be set as required than light constituent content.For the separation of present methanol to olefins reaction gas, when particularly propylene content was high, the demethanizing cat head can not established cooling, condensation, return-flow system usually.
When (6) second of demethanizing tower strand of absorption agent provided by back systemic circulation mode, demethanizer still material was sent into deethanizing column, isolates carbon two components through deethanizer overhead and goes ethylene rectification tower rectifying to produce qualified ethylene product.Deethanizing Tata still material is sent into depropanizing tower, isolates carbon three components by the depropanizing tower cat head and sends into propylene rectification tower rectifying and produce qualified propylene product.Depropanizing Tata still material is sent into debutanizing tower and is removed carbon four.Depropanizing tower and debutanizing tower are extracted out respectively and are removed demethanizing tower (seeing accompanying drawing 1) as second strand of absorption agent above-mentioned after the shallow bid material mixes according to a certain percentage.
When (7) second of demethanizing tower strand of absorption agent parsed by Analytic Tower, demethanizing tower still material was directly sent into Analytic Tower, and one absorption agent that parsing Tata still parses is got back to the demethanizing tower top after cooling, and rest materials is sent into debutanizing tower.Desorption tower cat head material is sent into deethanizing column, isolates C-2-fraction by deethanizer overhead and goes ethylene rectification tower to obtain qualified ethylene product, and tower still material goes propylene rectification tower to obtain propylene product.(seeing accompanying drawing 2)
Description of drawings
Fig. 1: a kind of low-carbon (LC) hydro carbons separates and methanol-to-olefins (M-OS/MTO) gas separating technology flow process one, and second strand of absorption agent of demethanizing tower is through separating out at depropanizing tower and/or debutanizing tower circulant solution.Wherein, D1: absorption agent knockout tower; D2: demethanizing tower; D3: deethanizing column; D4: depropanizing tower; D5: debutanizing tower.
Fig. 2: a kind of low-carbon (LC) hydro carbons separates and methanol-to-olefins (M-OS/MTO) gas separating technology flow process two, and second strand of absorption agent of demethanizing tower parses through Analytic Tower.Wherein, D1: absorption agent knockout tower; D2: demethanizing tower; D3: Analytic Tower.
Fig. 3: methanol-to-olefins (MTO) gas separating technology flow implementation illustration.Wherein, D1: absorption agent knockout tower; D2: demethanizing tower; D3: deethanizing column; D4: depropanizing tower; D5: debutanizing tower; D6: ethylene rectification tower; D7: propylene rectification tower.
Embodiment
Below be embodiments of the invention, produce the methanol to olefins reaction gas of 600,000 tons of alkene with certain factory per year and form foundation that about 1: 1 of the ratio of therein ethylene and propylene adopts the technical process of accompanying drawing 3 to separate as charging.Protection scope of the present invention is not limited to following embodiment.
In the present embodiment, the reaction gas that methyl alcohol is produced through catalyzed reaction boosts to 2.0MPaG step by step, after cooling, is divided into gas-liquid two-phase, gets into dehumidification system respectively and carries out drying.Dried reaction gas gets among the absorption agent knockout tower D1, and absorption agent knockout tower cat head mainly is methane, hydrogen, carbon two and part carbon three, and the main ingredient of tower still is carbon three, carbon four and the heavy constituent of carbon more than four, is a unintelligible splitter.Absorption agent knockout tower cat head gas phase gets into compressor compresses to about 3.2MPaG; In E3, E4, E5, condense to-21 ℃～-37 ℃ step by step then through recirculated water cooling, the heat exchange of demethanizer still, propylene refrigerant; Different positions gets into demethanizing tower from the middle part of demethanizing tower D2 respectively as the charging of demethanizing tower for the gas phase of separating, liquid phase fluid; Absorption agent knockout tower tower bottoms is cooled to-21 ℃～-37 ℃ through recirculated water and propylene refrigerant, enters into demethanizing tower D2 as absorption agent from demethanizing tower top.
Second strand of absorption agent of demethanizing tower provided by depropanizing tower and debutanizing tower system.Demethanizer still material is sent into deethanizing column D3, and isolating carbon two components through deethanizer overhead, to go ethylene rectification tower D6 rectifying to produce purity be 99.96% ethylene product.Deethanizing Tata still material is sent into depropanizing tower D4, isolates carbon three components by the depropanizing tower cat head and sends into propylene rectification tower D7 rectifying to produce purity be 99.6% propylene product.Propylene rectification tower adopts single tower in this embodiment.Depropanizing tower D4 tower still material is sent into debutanizing tower and is removed carbon four.Depropanizing Tata still and debutylize Tata still are extracted one material separately out and are mixed according to a certain percentage as second strand of absorption agent of demethanizing tower top from demethanizing tower and get into, and utilize the assimilation effect of absorption agent further to reduce the loss of ethene and propylene.
In this embodiment, the main absorber of demethanizing tower is to treat isolating cut from one of absorption agent knockout tower, has compared with prior art greatly reduced the consumption of circulation absorption agent, has reduced corresponding apparatus investment and energy consumption; And the multiply absorption agent has strengthened the assimilated efficiency of alkene, has reduced the loss of ethene and propylene; In addition, because absorption agent does not circulate through propylene rectification tower, propylene rectification tower can adopt single tower, has further reduced facility investment.For these reasons, compare investment saving with existing industrialized 600,000 tons of MTO alkene separating technologies about 10%, and energy consumption saves about 5%.The assimilated efficiency of alkene improves 5～10%.The calculation result of present embodiment is as seeing table 1.
The calculation result of table 1 embodiment
| Mole is formed | The D1 charging | The D1 charging | The D2 charging | The D2 charging | Ethylene product | Propylene product |
| H2 | 4.95 | 0.12 | 26.61 | 1.25 | 0.00 | 0.00 |
| C0 | 0.48 | 0.00 | 1.70 | 0.21 | 0.00 | 0.00 |
| 02 | 0.00 | 0.00 | 0.01 | 0.00 | 0.00 | 0.00 |
| N2 | 0.41 | 0.00 | 1.65 | 0.15 | 0.00 | 0.00 |
| CH4 | 5.89 | 0.89 | 13.31 | 3.74 | 0.00 | 0.00 |
| C2H4 | 61.34 | 32.44 | 50.31 | 60.48 | 99.96 | 0.00 |
| C2H6 | 1.02 | 0.77 | 0.66 | 1.15 | 0.04 | 0.01 |
| C3H6 | 22.28 | 45.50 | 5.47 | 30.98 | 0.00 | 99.60 |
| C3H8 | 1.44 | 3.42 | 0.29 | 1.93 | 0.00 | 0.38 |
| C4H6 | 0.04 | 0.32 | 0.00 | 0.00 | 0.00 | 0.00 |
| C4H8 | 1.94 | 12.33 | 0.00 | 0.09 | 0.00 | 0.00 |
| C4H10 | 0.08 | 0.58 | 0.00 | 0.00 | 0.00 | 0.00 |
| More than C5 reaches | 0.12 | 3.63 | 0.00 | 0.03 | 0.00 | 0.00 |
Claims (8)
1. a low-carbon (LC) hydro carbons separates and methanol-to-olefins (M-OS/MTO) gas separating technology flow process; It is characterized in that absorption tower (demethanizing tower) selected two bursts of differing absorption agent; Different positions gets into from top; And wherein one main absorber is before isolated from the absorption tower, does not need circulation.May further comprise the steps:
(1) gets into an absorption agent knockout tower through compression, drying, cooled hydrocarbon mixture or methanol to olefins reaction gas; Is that master's cut is sent into demethanizing tower top correct position from tower still or side line extraction with C3, C4 mixture, as the main absorber of demethanizing tower.Absorption agent knockout tower top than lighter-than-air gas through the compression, the cooling after, through separating tank isolate vapour, liquid two goes to absorption tower (demethanizing tower) as charging;
(2) another strand absorption agent staple of demethanizing tower is C4, C5 and above mixture; This strand absorption agent can be provided by the outside; Also can extract out from depropanizing tower system (side line or tower still); Or, perhaps provide by a certain percentage by depropanizing tower system and debutanizing tower system from debutanizing tower system (side line or tower still) extraction.This strand absorption agent gets into the top of demethanizing tower and further reclaims alkene;
(3) demethanizing tower can only be used absorption agent, and cat head need not be provided with systems such as condensing surface, return tank, reflux pump.If but gas composition changes greatly, also condensing surface, return tank, reflux pump can be set.For present methanol-to-olefins separation of gaseous mixture, the demethanizing cat head can not established cooling, condensation, return-flow system usually;
(4) absorption tower can be provided with one or two according to different MTO reaction gases or more than two; When an absorption tower is set; Two strands or multiply absorption agent get into from the different position of tower respectively; When two or more absorption towers were set, absorption agent got into the differing absorption tower respectively with sub-thread or multiply form.
2. according to claim 1; A kind of low-carbon (LC) hydro carbons separates and methanol-to-olefins gas separating technology flow process; It is characterized in that: demethanizing tower (absorption tower) has two strands of absorption agents; Respectively from the hydrocarbon mixture of absorption agent knockout tower with the back system, and different positions gets into demethanizing tower from demethanizing tower top respectively.
3. according to claim 1; A kind of low-carbon (LC) hydro carbons separates and methanol-to-olefins gas separating technology flow process; It is characterized in that: one main absorption agent of demethanizing tower itself is to treat isolating fraction mixture; From one material that separate the demethanizing tower front, do not need circulation from splitting gas (reaction gas).
4. according to claim 1, a kind of low-carbon (LC) hydro carbons separates and methanol-to-olefins gas separating technology flow process, it is characterized in that: the major ingredient of absorption agent: one is that C3, C4 mixture are main absorption agent; One is the absorption agent of the above mixture of C4, C5 and C5 according to different splitting gas (or reaction gas) compositional optimization.
5. according to claim 1; A kind of low-carbon (LC) hydro carbons separates and methanol-to-olefins gas separating technology flow process, it is characterized in that: the source from the absorption agent of back system is: the mixture of the material of the material of depropanizing tower extraction or debutanizing tower extraction or depropanizing tower and the different proportionings of debutanizing tower extraction.This absorption agent can parse from Analytic Tower, also can parse through back system local circulation.
6. according to claim 1; A kind of low-carbon (LC) hydro carbons separates and methanol-to-olefins gas separating technology flow process; It is characterized in that: the absorption agent of every employing more than two strands or two strands carries out the hydro carbons separation processes; And the multiply absorption agent can absorb in a tower or in the systemic technical process of a plurality of towers, all belong to this patent protection domain.
7. according to claim 1, a kind of low-carbon (LC) hydro carbons separates and methanol-to-olefins gas separating technology flow process, and every absorption agent is from preceding system, and the absorption technique flow process that does not need circulant solution to separate out all belongs to this patent protection domain.
8. this patent protection domain comprises that methanol-to-olefins gas delivery, hydrocarbon cracking or catalyzed reaction produce the separation of the separation of alkene, ether system alkene etc.; The equivalence that the content of all claims of the present invention is done changes and modifies, and is technological category of the present invention.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013029401A1 (en) * | 2011-09-01 | 2013-03-07 | 富德（北京）能源化工有限公司 | Method for absorbing and separating cracking gas from preparation process of low carbon olefin |
| CN103467231A (en) * | 2013-08-15 | 2013-12-25 | 上海河图工程股份有限公司 | Process for absorption and recycling of ethylene in olefin reaction products prepared from methanol |
| CN105272812A (en) * | 2014-06-05 | 2016-01-27 | 中国石化工程建设有限公司 | System for recovering ethylene from methanol-to-propylene product gas, and method thereof |
| CN106316758A (en) * | 2015-06-24 | 2017-01-11 | 中石化广州工程有限公司 | Method for separation of products of reaction for preparation of propylene by conversion of methanol |
| CN106316752A (en) * | 2015-06-24 | 2017-01-11 | 中石化广州工程有限公司 | Separation method for methanol-to-propylene (MTP) reaction product |
| CN106316759A (en) * | 2015-06-24 | 2017-01-11 | 中石化广州工程有限公司 | Method for separation of gases in preparation of propylene by conversion of methanol |
| CN106316757A (en) * | 2015-06-24 | 2017-01-11 | 中石化广州工程有限公司 | Separation process used in conversion of methanol into propylene gas |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1847203A (en) * | 2006-05-15 | 2006-10-18 | 中国石油化工集团公司 | Separating method for converting methanol to prepare low carbon olefin gas |
| CN101234946A (en) * | 2008-02-29 | 2008-08-06 | 中国天辰化学工程公司 | Method for separating low-carbon olefin mixed 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 |
| CN101575254A (en) * | 2009-06-05 | 2009-11-11 | 上海东化环境工程有限公司 | Process for recycling polymer grade ethylene from refinery dry gas |
-
2011
- 2011-09-20 CN CN201110279313.1A patent/CN102503757B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1847203A (en) * | 2006-05-15 | 2006-10-18 | 中国石油化工集团公司 | Separating method for converting methanol to prepare low carbon olefin 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 |
| CN101234946A (en) * | 2008-02-29 | 2008-08-06 | 中国天辰化学工程公司 | Method for separating low-carbon olefin mixed gas |
| CN101575254A (en) * | 2009-06-05 | 2009-11-11 | 上海东化环境工程有限公司 | Process for recycling polymer grade ethylene from refinery dry gas |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9446999B2 (en) | 2011-09-01 | 2016-09-20 | Fude (Beijing) Chemical & Industry Co., Ltd. | Process for separating by absorption the pyrolysis gas from preparation of lower carbon olefins |
| WO2013029401A1 (en) * | 2011-09-01 | 2013-03-07 | 富德（北京）能源化工有限公司 | Method for absorbing and separating cracking gas from preparation process of low carbon olefin |
| CN103467231A (en) * | 2013-08-15 | 2013-12-25 | 上海河图工程股份有限公司 | Process for absorption and recycling of ethylene in olefin reaction products prepared from methanol |
| CN105272812B (en) * | 2014-06-05 | 2017-06-20 | 中国石化工程建设有限公司 | The system and method for ethene is reclaimed in a kind of product gas from preparing propylene from methanol |
| CN105272812A (en) * | 2014-06-05 | 2016-01-27 | 中国石化工程建设有限公司 | System for recovering ethylene from methanol-to-propylene product gas, and method thereof |
| CN106316758A (en) * | 2015-06-24 | 2017-01-11 | 中石化广州工程有限公司 | Method for separation of products of reaction for preparation of propylene by conversion of methanol |
| CN106316759A (en) * | 2015-06-24 | 2017-01-11 | 中石化广州工程有限公司 | Method for separation of gases in preparation of propylene by conversion of methanol |
| CN106316757A (en) * | 2015-06-24 | 2017-01-11 | 中石化广州工程有限公司 | Separation process used in conversion of methanol into propylene gas |
| CN106316752A (en) * | 2015-06-24 | 2017-01-11 | 中石化广州工程有限公司 | Separation method for methanol-to-propylene (MTP) reaction product |
| CN106316758B (en) * | 2015-06-24 | 2018-07-27 | 中石化广州工程有限公司 | The separation method of preparing propylene by methanol transformation reaction product |
| CN106316757B (en) * | 2015-06-24 | 2018-07-27 | 中石化广州工程有限公司 | The separating technology of preparing propylene by methanol transformation gas |
| CN106316752B (en) * | 2015-06-24 | 2018-08-24 | 中石化广州工程有限公司 | A kind of separation method of preparing propylene by methanol transformation reaction product |
| CN106316759B (en) * | 2015-06-24 | 2018-08-24 | 中石化广州工程有限公司 | The separation method of preparing propylene by methanol transformation gas |
| CN112760120A (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 |
| CN112760120B (en) * | 2019-11-01 | 2022-04-15 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
| CN112760134A (en) * | 2019-11-04 | 2021-05-07 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
| CN112760134B (en) * | 2019-11-04 | 2022-04-12 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
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