CN101165023B - Method for increasing selectivity and yield of ethylene and propylene - Google Patents
Method for increasing selectivity and yield of ethylene and propylene Download PDFInfo
- Publication number
- CN101165023B CN101165023B CN2006101173499A CN200610117349A CN101165023B CN 101165023 B CN101165023 B CN 101165023B CN 2006101173499 A CN2006101173499 A CN 2006101173499A CN 200610117349 A CN200610117349 A CN 200610117349A CN 101165023 B CN101165023 B CN 101165023B
- Authority
- CN
- China
- Prior art keywords
- reaction
- reaction zone
- catalyst
- propylene
- yield
- 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.)
- Active
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to one kind of ethylene and propylene producing process with high selectivity and high yield. The production process includes the following steps: 1. reaction of oxygen compound material in the first reaction region through contacting with catalyst to produce gas-solid mixture I, and separating in the fast separator I to obtain the catalyst I to be regenerated and the effluent I containing ethylene and propylene; 2. reaction of the effluent I in the second reaction region through contacting with catalyst II to produce gas-solid mixture II, separating in the fast separator II to obtain the catalyst II to be regenerated and the effluent II containing ethylene, propylene and C4 and C4+ hydrocarbons, and further separating to obtain effluent III of C4 and C4+ hydrocarbons, ethylene product and propylene product; 3. reaction of the effluent III in the third reaction region through contacting with catalyst III to produce gas-solid mixture III, and returning mixture III to the first reaction region; and 4. regenerating the catalysts, and returning the regenerated catalysts to the reaction regions separately. The production process may be applied in industrial production.
Description
Technical field
The present invention relates to a kind of method that improves ethene, propylene selectivity and yield, particularly react the method that compound butylene and ethene transposition and olefins by catalytic cracking technology improve ethene, propylene selectivity and yield about methyl alcohol or dimethyl ether catalysis.
Background technology
Petrochemical complex is a mainstay industry important in the national economy, for industry, agricultural, departments such as traffic and national defence provide a large amount of industrial chemicals, is one of related and branch of industry that drive property is stronger in the national economy.Propylene and ethene then are to constitute modern petrochemical complex of paramount importance two big basic materials.
Propylene is mainly used in produces polypropylene, isopropyl benzene, oxo-alcohols, vinyl cyanide, propylene oxide, vinylformic acid, Virahol etc., and wherein polypropylene accounts for the over half of world's propylene demand.At present, 67% propylene is produced the byproduct of ethene from steam cracking in the world, and 30% produces the byproduct of vapour, diesel oil from refinery catalytic cracking (FCC), and a small amount of (about 3%) is obtained by dehydrogenating propane and ethene-butylene metathesis reaction.Estimate that following propylene demand growth speed is faster than supply.
Higher in view of the growth rate of demand of propylene, and traditional production model presents the pressure of " supply falls short of demand ", and therefore replenishing the propylene demand need be by means of other various propylene enhancing technology.
All the time; coal or Sweet natural gas preparing synthetic gas, synthesising gas systeming carbinol and alkene isolation technique have had the mass-producing mature experience; but the process by methanol to olefins is breakpoint and the difficult point of synthetic gas to this industrial chain of alkene, and this solution of key technology can be for providing a new raw material route by non-oil resource production basic organic ethene, propylene.Especially in the last few years, it is high that the demand of ethene and propylene continues, and under the deficient day by day situation of petroleum resources.How to hew out a non-oil resource and produce the Coal Chemical Industry variation route of propylene, for greatly alleviating China's oil situation in short supply, promote the great-leap-forward development of the heavy chemical industry of China and the structural adjustment of raw material route, have important strategic meaning and society, economic benefit.
Document CN1166478A, disclose a kind of method of being produced low-carbon alkenes such as ethene, propylene by methyl alcohol or dme, this method is catalyzer with the aluminium phosphate molecular sieve, adopts the ciculation fluidized formula processing method of upstriker dense bed, in 500～570 ℃ of preferred temperature of reaction, air speed 2～6 hours
-1And under 0.01～0.05MPa condition, make methyl alcohol or dme cracking produce low-carbon alkenes such as ethene, propylene.There is the low technical disadvantages of purpose product selectivity in this method.
Document CN1356299A discloses a kind of processing method and system thereof that produces low-carbon alkene by methyl alcohol or dme.This process using silicoaluminophosphamolecular molecular sieves (SAPO-34) is as catalyzer, utilize the ultrashort contact reactor of gas-solid cocurrent flow descending formula fluidized-bed, catalyzer contacts in the ultrashort contact reactor of gas-solid cocurrent flow descending formula fluidized-bed with raw material, the reactant flow direction is descending; Catalyzer and reaction product go out to enter the gas-solid quick disconnector that is arranged on this reactor lower part behind the reactor and carry out sharp separation; Isolated catalyzer enters charcoal regeneration in the revivifier, and catalyzer is cyclic regeneration in system, and reaction cycle is carried out.This technology dme or conversion of methanol are greater than 98%.But there is the low technical disadvantages of propylene selectivity equally in this method.
Summary of the invention
Technical problem to be solved by this invention be had purpose product ethene in the technical literature in the past, propene yield is low and the low problem of selectivity, and a kind of method of new raising ethene, propylene selectivity and yield is provided.This method has purpose product ethene, propene yield height, the advantage that selectivity is good.
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 that improves ethene, propylene selectivity and yield, with the oxygenatedchemicals is raw material, may further comprise the steps: (a) raw material contacts by the interior catalyst I of first reaction zone and reaction zone, and reaction gas solid mixture I enters fast minute device I and separates the effluent I that obtains reclaimable catalyst I and contain ethene, propylene; (b) entering second reaction zone from the effluent I of step (a) contacts with catalyst I I in the reaction zone, reaction gas solid mixture II enters fast minute device II and separates the effluent II that obtains reclaimable catalyst II and contain ethene, propylene and carbon four and above hydrocarbon thereof, and effluent II obtains effluent III, ethylene product and the propylene product of carbon four and above hydrocarbon thereof after separating; (c) enter the 3rd reaction zone from the effluent III of step (b) and contact with catalyst I II in the reaction zone, the reaction gas solid mixture enters first reaction zone; (d) enter revivifier regeneration from the reclaimable catalyst I of step (a) and from the reclaimable catalyst II of step (b), the catalyzer after the regeneration returns first reaction zone and the 3rd reaction zone respectively; Wherein, the temperature of reaction of first reaction zone or second reaction zone is 300～580 ℃, and reaction pressure is 0.01～1.5MPa, 0.1～50 second duration of contact; The temperature of reaction of the 3rd reaction zone is 350～650 ℃, and reaction pressure is 0.01～1.5MPa, 0.1～30 second duration of contact.
Catalyst I or catalyst I I all are selected from least a or its composite molecular screen in silicon phosphorus aluminium type or the ZSM type molecular sieve in the technique scheme.Catalyst I or the equal preferred version of catalyst I I are selected from least a or its composite molecular screen in SAPO-34 molecular sieve or the ZSM-5 molecular sieve.The oxygenatedchemicals preferred version is selected from least a in methyl alcohol or the dme.The temperature of reaction preferable range of first reaction zone or second reaction zone is 400～550 ℃, and the reaction pressure preferable range is 0.02～1.0MPa, and duration of contact, preferable range was 0.3～30 second.The temperature of reaction preferable range of the 3rd reaction zone is 400～600 ℃, and the reaction pressure preferable range is 0.02～1.0MPa, and duration of contact, preferable range was 0.3～20 second.First reaction zone, second reaction zone or the 3rd reaction zone all are selected from fluidized-bed, fast fluidized bed or riser reactor.
Studies show that, adopting fluidized-bed or riser reactor to carry out in the reaction process of oxygenatedchemicals such as methyl alcohol or dimethyl ether catalysis reaction generation ethene and propylene, the catalyst activity of reactor exit only reach initial activity 1/3rd in addition still less, after reaction is carried out about 1.5 seconds, activity of such catalysts descends about 30%, therefore, in the second half section of reactor, catalyst activity and selectivity sharply descend, the katalysis variation, the catalyzed reaction proportion reduces in the reaction process, and heat cracking reaction and unfavorable secondary reaction increase.This has limited the raising of per pass conversion on the one hand, makes that on the other hand purpose product selectivity and yield are on the low side.Among the present invention, adopt multi-stage type or dynamic partition formula reactor and relay-type ground use catalyzer to reach the oil gas series connection, catalyzer relay, segmentation reaction, the purpose of shortening reaction times and raising catalyzer average behaviour.
In addition, consider that catalyzer from revivifier is used for the active higher of ethene that methyl alcohol or dimethyl ether catalysis reaction generate and propylene, the present invention is before the regenerated catalyst effecting reaction, elder generation's (the 3rd reactor) in bed formula reactor carries out the modulation of catalyst activity, it is best to make the catalyst activity that arrives subsequent reaction zone (first reaction zone) preserve, favourable to improving the ethylene, propylene yield.
Adopt technical scheme of the present invention, all adopt the SAPO-34 molecular sieve catalyst at first reaction zone and second reactor, riser reactor, the 3rd reaction zone adopts the SAPO-34 molecular sieve catalyst, fluidized-bed reactor, first reaction zone and the 3rd reaction zone temperature of reaction are 400～550 ℃, and reaction pressure is 0.02～1.0MPa, and be 0.3～30 second duration of contact.The temperature of reaction of second reactor is 400～580 ℃, and reaction pressure is 0.02～1.0MPa, and be that ethene and propylene diene yield can reach more than 80%, have obtained better technical effect under 0.3～30 second condition duration of contact.
The invention will be further elaborated below by embodiment, but should be by any way as restriction of the present invention.
Embodiment
[embodiment 1]
With methyl alcohol is raw material, and first reaction zone and second reaction zone all adopt riser reactor, is catalyzer with the SAPO-34 molecular sieve, 450 ℃ of the first reaction zone temperature of reaction, and be 2 seconds duration of contact, reaction pressure is 0.05MPa; 480 ℃ of the second reaction zone temperature of reaction, be 3 seconds duration of contact, reaction pressure is 0.02MPa; 450 ℃ of the 3rd district's reaction zone temperature of reaction, be 3 seconds duration of contact, reaction pressure is 0.03MPa.In the experiment, the first reaction zone reaction gas mixtures is with after solid catalyst separates, gas phase directly enters the reaction of second reaction zone, enter the 3rd reaction zone from the reaction product of second reaction zone carbon four and above hydro carbons thereof after separating, the 3rd reaction zone gas-solid mixture directly enters first reaction zone, reaction result is: methanol conversion 100%, yield of ethene 47.1%, propene yield 35.6%.
[embodiment 2]
With the dme is raw material, and first reaction zone and second reaction zone all adopt riser reactor, is catalyzer with the SAPO-34 molecular sieve, 400 ℃ of the first reaction zone temperature of reaction, and be 1 second duration of contact, reaction pressure is 0.4MPa; 500 ℃ of the second reaction zone temperature of reaction, be 5 seconds duration of contact, reaction pressure is 0.3MPa; 400 ℃ of the 3rd district's reaction zone temperature of reaction, be 1 second duration of contact, reaction pressure is 0.04MPa.In the experiment, the first reaction zone reaction gas mixtures is with after solid catalyst separates, gas phase directly enters the reaction of second reaction zone, enter the 3rd reaction zone from the reaction product of second reaction zone carbon four and above hydro carbons thereof after separating, the 3rd reaction zone gas-solid mixture directly enters first reaction zone, reaction result is: dimethyl ether conversion rate 99%, yield of ethene 48.3%, propene yield 36.2%.
[embodiment 3]
With methyl alcohol and dme is raw material, and the weight ratio of methyl alcohol and dme is 1: 1, and first reaction zone and second reaction zone all adopt fast fluidized bed reactor, with the SAPO-34 molecular sieve is catalyzer, 500 ℃ of the first reaction zone temperature of reaction, be 3 seconds duration of contact, reaction pressure is 1.2MPa; 550 ℃ of the second reaction zone temperature of reaction, be 6 seconds duration of contact, reaction pressure is 1.0MPa; 500 ℃ of the 3rd district's reaction zone temperature of reaction, be 5 seconds duration of contact, reaction pressure is 1.2MPa.In the experiment, the first reaction zone reaction gas mixtures is with after solid catalyst separates, gas phase directly enters the reaction of second reaction zone, enter the 3rd reaction zone from the reaction product of second reaction zone carbon four and above hydro carbons thereof after separating, the 3rd reaction zone gas-solid mixture directly enters first reaction zone, reaction result is: methyl alcohol and dimethyl ether conversion rate 100%, yield of ethene 51.8%, propene yield 31.5%.
[embodiment 4]
With methyl alcohol and dme is raw material, and the weight ratio of methyl alcohol and dme is 2: 1, and first reaction zone and second reaction zone all adopt fast fluidized bed reactor, with the SAPO-11 molecular sieve is catalyzer, 530 ℃ of the first reaction zone temperature of reaction, be 5 seconds duration of contact, reaction pressure is 0.7MPa; 580 ℃ of the second reaction zone temperature of reaction, be 8 seconds duration of contact, reaction pressure is 0.5MPa; 530 ℃ of the 3rd district's reaction zone temperature of reaction, be 4 seconds duration of contact, reaction pressure is 0.7MPa.In the experiment, the first reaction zone reaction gas mixtures is with after solid catalyst separates, gas phase directly enters the reaction of second reaction zone, enter the 3rd reaction zone from the reaction product of second reaction zone carbon four and above hydro carbons thereof after separating, the 3rd reaction zone gas-solid mixture directly enters first reaction zone, reaction result is: methyl alcohol and dme total conversion rate 100%, yield of ethene 14.5%, propene yield 46.9%.
[embodiment 5]
With methyl alcohol and dme is raw material, the weight ratio of methyl alcohol and dme is 2: 1, first reaction zone adopts fast fluidized bed reactor, second reaction zone all adopts riser reactor, with the ZSM-5 molecular sieve is catalyzer, 460 ℃ of the first reaction zone temperature of reaction, be 10 seconds duration of contact, reaction pressure is 0.4MPa; 510 ℃ of the second reaction zone temperature of reaction, be 3 seconds duration of contact, reaction pressure is 0.2MPa; 450 ℃ of the 3rd district's reaction zone temperature of reaction, be 6 seconds duration of contact, reaction pressure is 0.4MPa.In the experiment, the first reaction zone reaction gas mixtures is with after solid catalyst separates, gas phase directly enters the reaction of second reaction zone, enter the 3rd reaction zone from the reaction product of second reaction zone carbon four and above hydro carbons thereof after separating, the 3rd reaction zone gas-solid mixture directly enters first reaction zone, reaction result is: methyl alcohol and dimethyl ether conversion rate 100%, yield of ethene 18.6%, propene yield 52.3%.
[embodiment 6]
With methyl alcohol is raw material, and first reaction zone and second reaction zone all adopt riser reactor, is catalyzer with the ZSM-35 molecular sieve, 300 ℃ of the first reaction zone temperature of reaction, and be 4 seconds duration of contact, reaction pressure is 0.05MPa; 550 ℃ of the second reaction zone temperature of reaction, be 3 seconds duration of contact, reaction pressure is 0.03MPa; 300 ℃ of the 3rd district's reaction zone temperature of reaction, be 15 seconds duration of contact, reaction pressure is 0.05MPa.In the experiment, the first reaction zone reaction gas mixtures is with after solid catalyst separates, gas phase directly enters the reaction of second reaction zone, enter the 3rd reaction zone from the reaction product of second reaction zone carbon four and above hydro carbons thereof after separating, the 3rd reaction zone gas-solid mixture directly enters first reaction zone, reaction result is: methanol conversion 99%, yield of ethene 15.8%, propene yield 41.6%.
[embodiment 7]
With methyl alcohol is raw material, and first reaction zone and second reaction zone all adopt riser reactor, is catalyzer with the SAPO-34 molecular sieve, 480 ℃ of the first reaction zone temperature of reaction, and be 3 seconds duration of contact, reaction pressure is 0.07MPa; 480 ℃ of the second reaction zone temperature of reaction, be 3 seconds duration of contact, reaction pressure is 0.07MPa; 480 ℃ of the 3rd district's reaction zone temperature of reaction, be 6 seconds duration of contact, reaction pressure is 0.08MPa.In the experiment, the first reaction zone reaction gas mixtures is with after solid catalyst separates, gas phase directly enters the reaction of second reaction zone, enter the 3rd reaction zone from the reaction product of second reaction zone carbon four and above hydro carbons thereof after separating, the 3rd reaction zone gas-solid mixture directly enters first reaction zone, reaction result is: methanol conversion 100%, yield of ethene 47%, propene yield 34%.
[embodiment 8]
With the dme is raw material, and first reaction zone and second reaction zone all adopt riser reactor, is catalyzer with the SAPO-34 molecular sieve, 500 ℃ of the first reaction zone temperature of reaction, and be 3 seconds duration of contact, reaction pressure is 0.2MPa; 500 ℃ of the second reaction zone temperature of reaction, be 3 seconds duration of contact, reaction pressure is 0.2MPa; 500 ℃ of the 3rd district's reaction zone temperature of reaction, be 2 seconds duration of contact, reaction pressure is 0.2MPa.In the experiment, the first reaction zone reaction gas mixtures is with after solid catalyst separates, gas phase directly enters the reaction of second reaction zone, enter the 3rd reaction zone from the reaction product of second reaction zone carbon four and above hydro carbons thereof after separating, the 3rd reaction zone gas-solid mixture directly enters first reaction zone, reaction result is: dimethyl ether conversion rate 100%, yield of ethene 19.7%, propene yield 50.3%.
[comparative example 1]
With reference to each step of embodiment 7, total residence time and reaction conditions just adopt single riser reactor to react, and reaction result is: methanol conversion 99%, yield of ethene 43.1%, propene yield 30.8%.
[comparative example 2]
With reference to each step and the reaction conditions of embodiment 8, total residence time and reaction conditions just adopt single riser reactor to react, and reaction result is: dimethyl ether conversion rate 98%, yield of ethene 15.1%, propene yield 42.8%.
Claims (6)
1. a method that improves ethene, propylene selectivity and yield is a raw material with the oxygenatedchemicals, may further comprise the steps:
A) raw material contacts by the interior catalyst I of first reaction zone and reaction zone, and reaction gas solid mixture I enters fast minute device I and separates the effluent I that obtains reclaimable catalyst I and contain ethene, propylene;
B) entering second reaction zone from the effluent I of step (a) contacts with catalyst I I in the reaction zone, reaction gas solid mixture II enters fast minute device II and separates the effluent II that obtains reclaimable catalyst II and contain ethene, propylene and carbon four and above hydrocarbon thereof, and effluent II obtains effluent III, ethylene product and the propylene product of carbon four and above hydrocarbon thereof after separating;
C) enter the 3rd reaction zone from the effluent III of step (b) and contact with catalyst I II in the reaction zone, the reaction gas solid mixture enters first reaction zone;
D) enter revivifier regeneration from the reclaimable catalyst I of step (a) and from the reclaimable catalyst II of step (b), the catalyzer after the regeneration returns first reaction zone and the 3rd reaction zone respectively;
Wherein, the temperature of reaction of first reaction zone or second reaction zone is 300～580 ℃, and reaction pressure is 0.01～1.5MPa, 0.1～50 second duration of contact; The temperature of reaction of the 3rd reaction zone is 350～650 ℃, and reaction pressure is 0.01～1.5MPa, 0.1～30 second duration of contact.
2. according to the method for the described raising ethene of claim 1, propylene selectivity and yield, it is characterized in that catalyst I, catalyst I I or catalyst I II all are selected from least a or its composite molecular screen in silicon phosphorus aluminium type or the ZSM type molecular sieve.
3. according to the method for the described raising ethene of claim 2, propylene selectivity and yield, it is characterized in that described catalyst I, catalyst I I or catalyst I II all are selected from least a or its composite molecular screen in SAPO-34 molecular sieve or the ZSM-5 molecular sieve.
4. according to the method for the described raising ethene of claim 1, propylene selectivity and yield, it is characterized in that oxygenatedchemicals is selected from least a in methyl alcohol or the dme.
5. according to the method for the described raising ethene of claim 1, propylene selectivity and yield, the temperature of reaction that it is characterized in that first reaction zone or second reaction zone is 400～550 ℃, and reaction pressure is 0.02～1.0MPa, 0.3～30 second duration of contact; The temperature of reaction of the 3rd reaction zone is 400～600 ℃, and reaction pressure is 0.02～1.0MPa, 0.3～20 second duration of contact.
6. according to the method for the described raising ethene of claim 1, propylene selectivity and yield, it is characterized in that first reaction zone, second reaction zone or the 3rd reaction zone all are selected from fluidized-bed, fast fluidized bed or riser reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2006101173499A CN101165023B (en) | 2006-10-20 | 2006-10-20 | Method for increasing selectivity and yield of ethylene and propylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2006101173499A CN101165023B (en) | 2006-10-20 | 2006-10-20 | Method for increasing selectivity and yield of ethylene and propylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101165023A CN101165023A (en) | 2008-04-23 |
| CN101165023B true CN101165023B (en) | 2010-12-01 |
Family
ID=39333904
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2006101173499A Active CN101165023B (en) | 2006-10-20 | 2006-10-20 | Method for increasing selectivity and yield of ethylene and propylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101165023B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101402538B (en) * | 2008-11-21 | 2013-01-09 | 中国石油化工股份有限公司 | Method for improving yield of light olefins |
| CN102276395B (en) * | 2010-06-11 | 2013-12-04 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene |
| CN103772109B (en) * | 2012-10-25 | 2016-09-07 | 中国石油化工股份有限公司 | The method of preparing propylene by methanol transformation coproduction ethylbenzene |
| CN114426442A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Method for preparing low-carbon olefin by using oxygen-containing compound |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1276775A (en) * | 1997-10-03 | 2000-12-13 | 埃克森化学专利公司 | Method for increasing light olefine yield by conversion of heavy hydrocarbon fraction of product to light olefines |
| CN1356299A (en) * | 2001-12-14 | 2002-07-03 | 清华大学 | Process and system for preparing low-carbon olefin from methanol or dimethylether |
| CN1419527A (en) * | 2000-03-08 | 2003-05-21 | 埃克森美孚化学专利公司 | Process to control conversion of C4+ and heavier stream to lighter products in oxygenate conversion reactions |
| CN1803738A (en) * | 2005-01-14 | 2006-07-19 | 环球油品公司 | Conversion of oxygenate to propylene using moving bed technology and a separate heavy olefin interconversion step |
-
2006
- 2006-10-20 CN CN2006101173499A patent/CN101165023B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1276775A (en) * | 1997-10-03 | 2000-12-13 | 埃克森化学专利公司 | Method for increasing light olefine yield by conversion of heavy hydrocarbon fraction of product to light olefines |
| CN1419527A (en) * | 2000-03-08 | 2003-05-21 | 埃克森美孚化学专利公司 | Process to control conversion of C4+ and heavier stream to lighter products in oxygenate conversion reactions |
| CN1356299A (en) * | 2001-12-14 | 2002-07-03 | 清华大学 | Process and system for preparing low-carbon olefin from methanol or dimethylether |
| CN1803738A (en) * | 2005-01-14 | 2006-07-19 | 环球油品公司 | Conversion of oxygenate to propylene using moving bed technology and a separate heavy olefin interconversion step |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101165023A (en) | 2008-04-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101165017B (en) | Production increasing method for propylene | |
| CN101165018B (en) | Method for producing ethylene and propylene | |
| CN101165026B (en) | Method for producing ethylene and propylene from methanol and dimethyl ether | |
| CN101165025B (en) | Method for producing ethylene and propylene from methanol or dimethyl ether | |
| CN101279879B (en) | Method for producing propone by comprehensive utilization of mixed C4 | |
| CN101165022B (en) | Method for increasing yield of ethylene and propylene | |
| CN101844089A (en) | Method for partially regenerating catalyst for preparing low-carbon alkenes from methanol or dimethyl ether | |
| CN101164687B (en) | Multi-reaction-area combination type reactor | |
| CN111423302A (en) | Method and device for preparing olefin from methanol | |
| CN101165023B (en) | Method for increasing selectivity and yield of ethylene and propylene | |
| CN101165020B (en) | Method for increasing yield of propylene | |
| CN101165019B (en) | Method for producing ethylene and propylene | |
| CN101148384B (en) | Method for producing ethylene and propylene from methanol and dimethyl ether | |
| CN101165027B (en) | Method for producing ethylene and propylene from oxygen-containing compounds | |
| CN101165021B (en) | Method for increasing yield of ethylene and propylene | |
| CN100430349C (en) | Method for producing propylene from methanol or dimethyl ether | |
| CN101891576A (en) | Process and device for preparing low-carbon olefin by methanol and/or dimethyl ether | |
| CN103553863B (en) | Method and system for preparing propylene by using methanol | |
| CN101165024B (en) | Method for increasing selectivity and yield of propylene | |
| CN110183300A (en) | A kind of process and system by the highly selective propylene processed of synthesis gas | |
| CN102060644B (en) | Method for preparing olefin by dehydration of methanol | |
| CN103694076B (en) | A kind of propylene production technology | |
| CN100567226C (en) | Produce the method for propylene | |
| CN101747137A (en) | Method for production of propylene with methanol or dimethyl ether | |
| CN101148383B (en) | Method for preparing ethylene and propylene from methanol and dimethyl ether |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |