CN105367366A - Method for producing ethylene and propylene by means of mixed C4 - Google Patents
Method for producing ethylene and propylene by means of mixed C4 Download PDFInfo
- Publication number
- CN105367366A CN105367366A CN201410428789.0A CN201410428789A CN105367366A CN 105367366 A CN105367366 A CN 105367366A CN 201410428789 A CN201410428789 A CN 201410428789A CN 105367366 A CN105367366 A CN 105367366A
- Authority
- CN
- China
- Prior art keywords
- mixed
- ethene
- propylene
- catalytic cracking
- produce
- 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
Abstract
The invention relates to a method for producing ethylene and propylene by means of mixed C4 to mainly solve the problems of the prior art that the utilization rate of mixed C4 is low and the additional value is low. The method comprises the steps of a, conducting hydrogenation on butadiene in mixed C4 to generate monoolefine with the selective hydrogenation technique; b, conducting catalytic cracking on olefin in mixed C4 to generate ethylene and propylene with the olefin catalytic cracking technique; c, separating out unreacted mixed C4 with the rectification technique; d, removing alkane in unreacted mixed C4 with the extractive distillation technique, and taking residual C4 olefin as the catalytic cracking material in a circulating mode. The method can be applied to industrial application of increasing the production of ethylene and propylene and can increase the comprehensive chemical utilization rate of mixed C4.
Description
Technical field
The present invention relates to a kind of method utilizing mixed c 4 to produce ethene, propylene.
Background technology
Ethene, propylene are the most basic raw materials of petrochemical complex, are the bases producing various Organic chemical products, produce mainly through steam cracking and catalytic cracking.And as the mixed c 4 of one of steam cracking device and catalytic cracking unit Main By product, wherein contain Trimethylmethane, normal butane, iso-butylene, divinyl, butene-1, butene-2 etc. that quantity does not wait, these components are broad-spectrum industrial chemicals, particularly C 4 olefin.Current mixed c 4 is generally after Butadiene Extraction, iso-butylene etherificate, and remaining carbon four major part uses as liquefied gas as fuel, and added value is lower.Along with the continuous growth of carbon four output, how improving carbon four comprehensive resource utilization rate is enterprise's cost efficiency, the strong approach promoting economic benefit.
CA2297301 describes a kind of method improving carbon four and carbon more than four mixture value.This method adopts zeolite [molecular sieve to be directly low-carbon alkene by carbon four feedstock conversion, and is separated and obtains ethene, propylene.This method comprises two catalytic cracking reaction devices, selective hydrogenation reactor, a methyltertiarvbutyl ether reactor etc., and flow process is complicated, and ethene, propene yield are low, less economical.CN101279879B describes a kind of method fully utilizing mixed c 4 production propylene.This method first makes the olefins by catalytic cracking in mixed c 4 be ethene, propylene by deep catalytic cracking technology, then adopts isomerization technique that butene-1 isomery is turned to butene-2, finally by disproportionation technology, butene-2 and ethene is reacted and produce propylene.This method does not relate to the process containing divinyl raw material, and a part of unreacted carbon four directly discharges, and causes C 4 olefin to lose comparatively large, and does not process the alkane in mixed c 4, make a large amount of alkane at system internal recycle, cause equipment huge.US6075173 describes a kind of method utilizing C_4 hydrocarbon to produce iso-butylene and propylene.This method makes butadiene hydrogenation be monoolefine by selective hydrogenation, butene-1 isomery is turned to butene-2 simultaneously, then adopt rectifying separation, overhead extraction iso-butylene and a small amount of butene-1, tower reactor produces propylene by disproportionation reaction after mixing with ethene containing the cut of butene-2 and butane.US6686510B2 is the improving technique of US6075173.This method when carrying out rectifying separation to selective hydrogenation product, in rectifying tower or tower to be coupled outward an isomerization reaction, make the further isomery of butene-1 turn to butene-2, thus obtain the iso-butylene of higher degree in rectifying tower top.These two kinds of methods do not make full use of iso-butylene and for the higher raw material of iso-butylene content, the yield of propylene is low, and consumes a large amount of ethene resources.
Summary of the invention
The present invention relates to a kind of method utilizing mixed c 4 to produce ethene, propylene.Technical problem to be solved by this invention is the problem that in prior art, mixed c 4 utilization ratio is not high, added value is low.Provide a kind of mixed c 4 that utilizes newly and produce the method for ethene, propylene.The method has that mixed c 4 comprehensive utilization ratio is high, ethene and propene yield is high, the feature of good economy performance.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method utilizing mixed c 4 to produce ethene, propylene, comprise the following steps: (a) mixed c 4 raw material and hydrogen enter selective hydrogenation reactor, divinyl in raw material is hydrogenated to monoolefine, and hydrogenation reaction product enters catalytic cracking reaction device after heat exchange and preheating; B, in () catalytic cracking reaction device, C _ 4 alkene catalytic pyrolysis is ethene, propylene, catalytic cracking reaction products, after heat exchange, cooling, compression, enters rectifying tower and is separated; (c) rectifying tower top extraction ethene, propylene light constituent, tower reactor extraction carbon five and above heavy constituent, side take-off unreacted carbon four; D () unreacted carbon four enters in the middle part of extractive distillation column, extraction agent adds from extractive distillation column top, overhead extraction butane, and tower reactor must contain the overhead product of C 4 olefin and extraction agent; E () extractive distillation column reactor distillate enters in the middle part of solvent recovery tower, tower top C 4 olefin returns catalytic cracking reaction device as catalytic pyrolysis raw material, and tower reactor extraction agent returns to extractive distillation column top, recycles.
In technique scheme, mixed c 4 and hydrogen enter selective hydrogenation reactor, wherein divinyl is hydrogenated to butene-1 and/or butene-2 by selectivity, the catalyzer adopted be preferably load on the alumina support comprise at least one be selected from nickel, zinc or palladium.Selective hydrogenation reactor temperature in preferable range is 20 ~ 150 DEG C, and reaction pressure preferable range is 0.6 ~ 4.0MPaG, and reaction velocity preferable range is 1 ~ 20hr
-1, hydrogen and divinyl mol ratio preferable range are 0.9 ~ 1.2.
Selective hydrogenation product through heat exchange and be preheated to temperature required after enter catalytic cracking reaction device, reaction generates ethene, propylene, the catalyzer adopted is preferably silicoaluminophosphate molecular sieve catalyst, temperature of reaction preferable range is 500 ~ 600 DEG C, reaction pressure preferable range is 0 ~ 0.2MPaG, and reaction velocity preferable range is 15 ~ 30hr
-1.
Catalytic cracking reaction products through heat exchange and be cooled to temperature required after enter compressor, be separated by entering rectifying tower after compressor compresses to required pressure, overhead extraction carbon three and following component, tower reactor extraction carbon five and above component, unreacted mixed c 4 is from tower side take-off, enter in the middle part of extractive distillation column, extraction agent adds from tower top, and extraction agent is preferably at least one in dimethyl formamide, N-Methyl pyrrolidone, acetonitrile.Extracting rectifying tower top obtains butane, tower reactor enters in the middle part of solvent recovery tower containing the overhead product of C 4 olefin and extraction agent, tower top C 4 olefin is all back to catalytic cracking reaction device as catalytic pyrolysis raw material, tower reactor extraction agent returns to extractive distillation column top, recycle, and supplement fresh extraction agent in right amount as required.The total number of theoretical plate preferable range of extractive distillation column is 40 ~ 60, and working pressure preferable range is 0.3MPaG ~ 0.9MPaG, and solvent ratio preferable range is 4 ~ 15, and reflux ratio preferable range is 3 ~ 10.The total number of theoretical plate preferable range of solvent recovery tower is 5 ~ 20, and working pressure preferable range is 0.3MPaG ~ 0.9MPaG, and reflux ratio preferable range is 1 ~ 6.
In technique scheme, mixed c 4 by weight percentage, preferably comprises the divinyl of 10 ~ 60%; Be more preferably the divinyl of 15 ~ 40%;
In technique scheme, mixed c 4 by weight percentage, preferably comprises the iso-butylene of 5 ~ 60%; Be more preferably 10 ~ 50% iso-butylenes;
In technique scheme, mixed c 4 by weight percentage, preferably comprises butene-1 and the butene-2 of 5 ~ 50%; Be more preferably butene-1 and the butene-2 of 10 ~ 40%;
In technique scheme, mixed c 4 by weight percentage, preferably comprises the butane of 5 ~ 35%; Be more preferably the butane of 10 ~ 25%.
The present invention is by adopting selective hydrogenation technology, deep catalytic cracking technology and extraction and distillation technology, take full advantage of olefin production ethene, the propylene in mixed c 4 raw material, improve utilization ratio and the added value of mixed c 4, ethene and propene yield high, achieve good technique effect.
Accompanying drawing explanation
Fig. 1 is a kind of method process flow diagram utilizing mixed c 4 to produce ethene, propylene of the present invention.
Fig. 2 is CA2297301 process flow diagram.
Fig. 1, in Fig. 2,1 is raw material mixed c 4, 2 is hydrogen, 3 is selective hydrogenation reactor, 4 is selective hydrogenation product, 5 is interchanger, 6 is preheater, 7 is catalytic cracking reaction device, 8 is catalytic cracking reaction products, 9 is water cooler, 10 is compressor, 11 is rectifying tower, 12 is carbon three and following component, 13 is carbon five and above component, 14 is unreacted mixed c 4, 15 is extractive distillation column, 16 is fresh extraction agent, 17 is butane, 18 is the overhead product of unreacted carbon alkatetraenes and extraction agent, 19 is solvent recovery tower, 20 is unreacted carbon alkatetraenes, 21 is cycling extraction agent, 22 is the first catalytic cracking reaction device, 23 is the first rectifying tower, 24 is light constituent, 25 is ethene, 26 is propylene, 27 is carbon four, 28 is heavy constituent, 29 is selective hydrogenation reactor, 30 is methyl alcohol, 31 is methyltertiarvbutyl ether reactor, 32 is Second distillation column, 33 is MTBE, 34 is the second catalytic cracking reaction device.
By the flow process shown in Fig. 1, mixed c 41 and hydrogen 2 enter selective hydrogenation reactor 3, and through selective hydrogenation, divinyl is hydrogenated to monoolefine.It is temperature required that selective hydrogenation product 4 is preheated to reaction through interchanger 5 and preheater 6, then enters catalytic cracking reaction device 7.Olefin cracking in catalytic cracking reaction device in mixed c 4 is ethene, propylene, and catalytic cracking reaction products 8 is cooled to temperature required through interchanger 5 and water cooler 9, enters rectifying tower 11 and be separated after being then compressed to required pressure by compressor 10.Rectifying tower top extraction carbon three and following component 12, tower reactor extraction carbon five and above component 13, enter after unreacted mixed c 4 14 side take-off in the middle part of extractive distillation column 15, fresh extraction agent 16 adds from extractive distillation column top, overhead extraction butane 17, the overhead product 18 of tower reactor unreacted carbon alkatetraenes and extraction agent enters solvent recovery tower 19, before the circulation of tower top unreacted carbon alkatetraenes 20 returns catalytic cracking reaction device, tower reactor cycling extraction agent 21 returns to extractive distillation column top, and supplements fresh extraction agent in right amount on extractive distillation column top as required.
Below by specific embodiment, the present invention is further illustrated, but scope of the present invention has more than the scope being limited to embodiment and covering.
Embodiment
[comparative example 1]
Shown in Fig. 2, mixed c 4 composition (% by weight) is: divinyl: 40.0%, iso-butylene: 12.0%, butene-1: 18.0%, butene-2: 18.2%, butane: 11.8%.Adopt CA2297301 technical process, the first catalytic cracking reaction device and the second catalytic cracking reaction device employing silica alumina ratio are the silicoaluminophosphate molecular sieve catalyst of 280, temperature of reaction 550 DEG C, reaction pressure 0.1MPaG; First rectifying tower is valve tray column, stage number 110, tower top pressure 1.2MPaG; Selective hydrogenation catalyst is palladium metal series catalysts, temperature of reaction 60 DEG C, reaction pressure 3.0MPaG; Catalyst for etherification is ion exchange resin, temperature of reaction 40 DEG C, reaction pressure 1.2MPaG; Second distillation column is sieve-tray tower, stage number 60, tower top pressure 0.4MPaG.Test proof obtains ethene and propylene is respectively 5.7% and 17.0% (weight, the alkene in raw material mixed c 4 1).
[embodiment 1]
Shown in Fig. 1, mixed c 4 composition (% by weight) is: divinyl: 40.0%, iso-butylene: 12.0%, butene-1: 18.0%, butene-2: 18.2%, butane: 11.8%.Adopt present invention process flow process, selective hydrogenation catalyzer is alumina load palladium metal, reactor inlet temperature 40 DEG C, reaction pressure 1.5MPaG, reaction velocity 6hr
-1, hydrogen and divinyl mol ratio 1.08; Catalytic cracking reaction catalyzer is the ZSM-5 molecular sieve of silica alumina ratio 200, temperature of reaction 530 DEG C, reaction pressure 0.10MPaG, reaction velocity 20hr
-1; The total number of theoretical plate 60 (number from top to bottom, as follows) of rectifying tower, reflux ratio 5, the 38th piece of theoretical stage side take-off unreacted mixed c 4, tower top pressure 1.5MPaG; The total number of theoretical plate 50 of extractive distillation column, tower top working pressure 0.5MPaG, reflux ratio 5, extraction agent dimethyl formamide enters from the 2nd block of plate, solvent ratio 8; The total number of theoretical plate 15 of solvent recovery tower, working pressure 0.5MPaG, reflux ratio 3.Test proves that the yield obtaining ethene and propylene is respectively 10.6% and 37.6% (weight, the alkene in raw material mixed c 4 1).
[embodiment 2]
Shown in Fig. 1, mixed c 4 composition (% by weight) is: divinyl: 25.0%, iso-butylene: 20.0%, butene-1: 13.0%, butene-2: 25.4%, butane: 16.6%.Adopt present invention process flow process, selective hydrogenation catalyzer is alumina load metallic nickel, reactor inlet temperature 30 DEG C, reaction pressure 2.0MPaG, reaction velocity 5hr
-1, hydrogen and divinyl mol ratio 1.05; Catalytic cracking reaction catalyzer is the ZSM-5 molecular sieve of silica alumina ratio 200, temperature of reaction 550 DEG C, reaction pressure 0.06MPaG, reaction velocity 18hr
-1; The total number of theoretical plate 65 (number from top to bottom, as follows) of rectifying tower, reflux ratio 6, the 40th piece of theoretical stage side take-off unreacted mixed c 4, tower top pressure 1.5MPaG; The total number of theoretical plate 50 of extractive distillation column, tower top working pressure 0.5MPaG, reflux ratio 5, extraction agent dimethyl formamide enters from the 2nd block of plate, solvent ratio 6; The total number of theoretical plate 15 of solvent recovery tower, working pressure 0.5MPaG, reflux ratio 3.Test proves that the yield obtaining ethene and propylene is respectively 10.8% and 38.1% (weight, the alkene in raw material mixed c 4 1).
[embodiment 3]
Shown in Fig. 1, mixed c 4 composition (% by weight) is: divinyl: 22.0%, iso-butylene: 36.0%, butene-1: 8.0%, butene-2: 13.4%, butane: 20.6%.Adopt present invention process flow process, selective hydrogenation catalyzer is alumina load metallic nickel, reactor inlet temperature 40 DEG C, reaction pressure 2.5MPaG, reaction velocity 6hr
-1, hydrogen and divinyl mol ratio 1.05; Catalytic cracking reaction catalyzer is the ZSM-5 molecular sieve of silica alumina ratio 300, temperature of reaction 550 DEG C, reaction pressure 0.08MPaG, reaction velocity 20hr
-1; The total number of theoretical plate 65 (number from top to bottom, as follows) of rectifying tower, reflux ratio 7, the 40th piece of theoretical stage side take-off unreacted mixed c 4, tower top pressure 1.7MPaG; The total number of theoretical plate 55 of extractive distillation column, tower top working pressure 0.4MPaG, reflux ratio 5, extraction agent N-Methyl pyrrolidone enters from the 2nd block of plate, solvent ratio 6; The total number of theoretical plate 18 of solvent recovery tower, working pressure 0.4MPaG, reflux ratio 4.Test proves that the yield obtaining ethene and propylene is respectively 11.1% and 38.3% (weight, the alkene in raw material mixed c 4 1).
[embodiment 4]
Shown in Fig. 1, mixed c 4 composition (% by weight) is: divinyl: 15.0%, iso-butylene: 50.0%, butene-1: 6.0%, butene-2: 5.4%, butane: 23.6%.Adopt present invention process flow process, selective hydrogenation catalyzer is alumina load palladium metal, reactor inlet temperature 30 DEG C, reaction pressure 1.8MPaG, reaction velocity 8hr
-1, hydrogen and divinyl mol ratio 1.03; Catalytic cracking reaction catalyzer is the ZSM-5 molecular sieve of silica alumina ratio 300, temperature of reaction 560 DEG C, reaction pressure 0.08MPaG, reaction velocity 18hr
-1; The total number of theoretical plate 68 (number from top to bottom, as follows) of rectifying tower, reflux ratio 7, the 42nd piece of theoretical stage side take-off unreacted mixed c 4, tower top pressure 1.7MPaG; The total number of theoretical plate 55 of extractive distillation column, tower top working pressure 0.4MPaG, reflux ratio 6, extraction agent N-Methyl pyrrolidone enters from the 2nd block of plate, solvent ratio 5; The total number of theoretical plate 18 of solvent recovery tower, working pressure 0.4MPaG, reflux ratio 4.Test proves that the yield obtaining ethene and propylene is respectively 11.3% and 38.6% (weight, the alkene in raw material mixed c 4 1).
Claims (9)
1. utilize mixed c 4 to produce a method for ethene, propylene, comprise the following steps:
A () mixed c 4 raw material and hydrogen enter selective hydrogenation reactor, the divinyl in raw material is hydrogenated to monoolefine, and hydrogenation reaction product enters catalytic cracking reaction device after heat exchange and preheating;
B, in () catalytic cracking reaction device, C _ 4 alkene catalytic pyrolysis is ethene, propylene, catalytic cracking reaction products, after heat exchange, cooling, compression, enters rectifying tower and is separated;
(c) rectifying tower top extraction ethene, propylene light constituent, tower reactor extraction carbon five and above heavy constituent, side take-off unreacted carbon four;
D () unreacted carbon four enters in the middle part of extractive distillation column, extraction agent adds from extractive distillation column top, overhead extraction butane, and tower reactor must contain the overhead product of C 4 olefin and extraction agent;
E () extractive distillation column reactor distillate enters in the middle part of solvent recovery tower, tower top C 4 olefin returns catalytic cracking reaction device as catalytic pyrolysis raw material, and tower reactor extraction agent returns to extractive distillation column top, recycles.
2. utilize mixed c 4 to produce the method for ethene, propylene according to claim 1, it is characterized in that divinyl is hydrogenated to butene-1 and/or butene-2 by selectivity, the catalyzer of employing be load on the alumina support comprise at least one be selected from nickel, zinc or palladium.
3. utilize mixed c 4 to produce the method for ethene, propylene according to claim 1, it is characterized in that selective hydrogenation reactor temperature in 20 ~ 150 DEG C, reaction pressure 0.6 ~ 4.0MPaG, reaction velocity 1 ~ 20hr
-1, hydrogen and divinyl mol ratio 0.9 ~ 1.2.
4. utilize mixed c 4 to produce the method for ethene, propylene according to claim 1, it is characterized in that mixed c 4 catalytic pyrolysis is ethene, propylene, the catalyzer of employing is silicoaluminophosphate molecular sieve catalyst.
5. utilize mixed c 4 to produce the method for ethene, propylene according to claim 1, it is characterized in that catalytic cracking reaction device temperature of reaction 500 ~ 600 DEG C, reaction pressure 0 ~ 0.2MPaG, reaction velocity 15 ~ 30hr-1.
6. utilize mixed c 4 to produce the method for ethene, propylene according to claim 1, it is characterized in that the total number of theoretical plate 40 ~ 60 of extractive distillation column, working pressure 0.3MPaG ~ 0.9MPaG, solvent ratio 4 ~ 15, reflux ratio 3 ~ 10.
7. utilize mixed c 4 to produce the method for ethene, propylene according to claim 1, it is characterized in that extraction agent is selected from least one in dimethyl formamide, N-Methyl pyrrolidone, acetonitrile.
8. utilize mixed c 4 to produce the method for ethene, propylene according to claim 1, it is characterized in that the total number of theoretical plate 5 ~ 20 of solvent recovery tower, working pressure 0.3MPaG ~ 0.9MPaG, reflux ratio 1 ~ 6.
9. utilize mixed c 4 to produce the method for ethene, propylene according to claim 1, it is characterized in that solvent recuperation tower top C 4 olefin all returns catalytic cracking reaction device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410428789.0A CN105367366B (en) | 2014-08-27 | 2014-08-27 | Utilize the method for mixing the production of carbon four ethene, propylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410428789.0A CN105367366B (en) | 2014-08-27 | 2014-08-27 | Utilize the method for mixing the production of carbon four ethene, propylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105367366A true CN105367366A (en) | 2016-03-02 |
| CN105367366B CN105367366B (en) | 2017-10-27 |
Family
ID=55370067
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410428789.0A Active CN105367366B (en) | 2014-08-27 | 2014-08-27 | Utilize the method for mixing the production of carbon four ethene, propylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105367366B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109369318A (en) * | 2018-12-07 | 2019-02-22 | 宁波旭合瑞石化工程有限公司 | A method of the raw material based on C5 alkene maximizes production propylene |
| CN111233613A (en) * | 2020-04-01 | 2020-06-05 | 联泓新材料科技股份有限公司 | Hydrogenation device and hydrogenation method for producing ethylene and propylene |
| CN112679300A (en) * | 2019-10-18 | 2021-04-20 | 中国石油化工股份有限公司 | Method for preparing propylene from carbon four raw material |
| CN112694383A (en) * | 2019-10-22 | 2021-04-23 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by catalytic cracking of olefin |
| CN112707780A (en) * | 2019-10-24 | 2021-04-27 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene from raw materials with four or more carbon atoms |
| CN112759500A (en) * | 2019-10-21 | 2021-05-07 | 中国石油化工股份有限公司 | Method for producing propylene by using carbon tetrahydrocarbon |
| CN114426448A (en) * | 2020-09-09 | 2022-05-03 | 中国石油化工股份有限公司 | Method and device for increasing yield of propylene |
| CN114426449A (en) * | 2020-09-09 | 2022-05-03 | 中国石油化工股份有限公司 | Method and device for improving utilization rate of mixed carbon four |
| CN114456025A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Method and system for producing ethylene and propylene by catalyzing light gasoline |
| CN114456026A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Method and device for increasing yields of ethylene and 1-butene |
| CN114516776A (en) * | 2020-11-19 | 2022-05-20 | 中国石油化工股份有限公司 | Method and apparatus for producing ethylene and propylene |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2297301A1 (en) * | 2000-01-18 | 2001-07-18 | Uop Llc | Combination process for enhanced light olefin production |
| US20020198430A1 (en) * | 2000-07-12 | 2002-12-26 | Technip-Coflexip | Process and installation for recovery and purification of ethylene produced by pyrolysis of hydrocarbons, and gases obtained by this process |
| CN101205162A (en) * | 2006-12-21 | 2008-06-25 | 中国石油化工股份有限公司 | Combined technique for preparing olefins by using refinery C4 |
| CN101475429A (en) * | 2008-01-04 | 2009-07-08 | 中国石油化工股份有限公司 | Method for comprehensive utilization of cracking C4 |
| CN102070390A (en) * | 2011-01-12 | 2011-05-25 | 王伟跃 | Method for preparing propylene from refinery mixed C4 |
-
2014
- 2014-08-27 CN CN201410428789.0A patent/CN105367366B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2297301A1 (en) * | 2000-01-18 | 2001-07-18 | Uop Llc | Combination process for enhanced light olefin production |
| US20020198430A1 (en) * | 2000-07-12 | 2002-12-26 | Technip-Coflexip | Process and installation for recovery and purification of ethylene produced by pyrolysis of hydrocarbons, and gases obtained by this process |
| CN101205162A (en) * | 2006-12-21 | 2008-06-25 | 中国石油化工股份有限公司 | Combined technique for preparing olefins by using refinery C4 |
| CN101475429A (en) * | 2008-01-04 | 2009-07-08 | 中国石油化工股份有限公司 | Method for comprehensive utilization of cracking C4 |
| CN102070390A (en) * | 2011-01-12 | 2011-05-25 | 王伟跃 | Method for preparing propylene from refinery mixed C4 |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109369318A (en) * | 2018-12-07 | 2019-02-22 | 宁波旭合瑞石化工程有限公司 | A method of the raw material based on C5 alkene maximizes production propylene |
| CN109369318B (en) * | 2018-12-07 | 2021-05-21 | 宁波旭合瑞石化工程有限公司 | Method for maximizing production of propylene by using C5 olefin as main raw material |
| CN112679300A (en) * | 2019-10-18 | 2021-04-20 | 中国石油化工股份有限公司 | Method for preparing propylene from carbon four raw material |
| CN112759500A (en) * | 2019-10-21 | 2021-05-07 | 中国石油化工股份有限公司 | Method for producing propylene by using carbon tetrahydrocarbon |
| CN112759500B (en) * | 2019-10-21 | 2023-04-07 | 中国石油化工股份有限公司 | Method for producing propylene by using carbon tetrahydrocarbon |
| CN112694383A (en) * | 2019-10-22 | 2021-04-23 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by catalytic cracking of olefin |
| CN112707780A (en) * | 2019-10-24 | 2021-04-27 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene from raw materials with four or more carbon atoms |
| CN111233613A (en) * | 2020-04-01 | 2020-06-05 | 联泓新材料科技股份有限公司 | Hydrogenation device and hydrogenation method for producing ethylene and propylene |
| CN114426448A (en) * | 2020-09-09 | 2022-05-03 | 中国石油化工股份有限公司 | Method and device for increasing yield of propylene |
| CN114426449A (en) * | 2020-09-09 | 2022-05-03 | 中国石油化工股份有限公司 | Method and device for improving utilization rate of mixed carbon four |
| CN114456025A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Method and system for producing ethylene and propylene by catalyzing light gasoline |
| CN114456026A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Method and device for increasing yields of ethylene and 1-butene |
| CN114516776A (en) * | 2020-11-19 | 2022-05-20 | 中国石油化工股份有限公司 | Method and apparatus for producing ethylene and propylene |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105367366B (en) | 2017-10-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105367366A (en) | Method for producing ethylene and propylene by means of mixed C4 | |
| CN101475429B (en) | Method for comprehensive utilization of cracking C4 | |
| CN101492334B (en) | Method for improving mixed C4 chemical industry exploitation value | |
| CN100564331C (en) | Utilize refinery C four to produce the combination process of alkene | |
| CN102372573B (en) | Method for preparing propylene by using etherified C4 and ethylene | |
| CN101255086B (en) | Method for cracking C_4 and preparing olefin by refinery C_4 | |
| CN102070391A (en) | Method for preparing isobutylene by comprehensively using mixed C4 | |
| CN101279879B (en) | Method for producing propone by comprehensive utilization of mixed C4 | |
| CN101679146A (en) | Propylene production | |
| CN105367368B (en) | The method that high-purity isobutylene is prepared from C_4 hydrocarbon | |
| CN106608791A (en) | Method for preparing propylene through integrated utilization of C4 hydrocarbon | |
| CN101492335B (en) | Combination method for comprehensive utilization of mix C4 | |
| CN104945228A (en) | Method for preparing MTBE or isobutylene by adopting mixed butane | |
| CN103785482B (en) | A kind of deactivating process for the treatment of of olefin isomerization catalyst | |
| CN102351629B (en) | Method for producing propylene and high-octane gasoline from methanol | |
| CN102069007B (en) | The Catalysts and its preparation method of olefin cracking preparation of propylene | |
| CN102070390B (en) | The method of refinery's mixed c 4 propylene | |
| CN103864564A (en) | Technique for processing methanol-to-propylene by-products | |
| CN103772114A (en) | Method for concentrating butane through catalysis and isomerization | |
| CN104487549A (en) | More energy efficient c5 hydrogenation process | |
| CN104672046A (en) | Method of increasing ethylene and propylene yields by freshening C-4 olefins in catalytic cracking or pyrolysis process after separation | |
| CN104892339A (en) | Method for preparing n-butane by using iso-butane | |
| CN101225013A (en) | Separating device and method for preparing lower-carbon olefin gas product by methanol and dimethyl ether transformation | |
| CN104557362A (en) | System and method for preparing aromatic hydrocarbons and co-producing ethylene and propylene by transforming methanol and/or dimethyl ether | |
| CN104250192B (en) | The preparation method of a kind of propylene and divinyl |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |