CN1611472A - Method for producing propene for C4 and more olefin catalytic cracking - Google Patents
Method for producing propene for C4 and more olefin catalytic cracking Download PDFInfo
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- CN1611472A CN1611472A CNA200310108178XA CN200310108178A CN1611472A CN 1611472 A CN1611472 A CN 1611472A CN A200310108178X A CNA200310108178X A CN A200310108178XA CN 200310108178 A CN200310108178 A CN 200310108178A CN 1611472 A CN1611472 A CN 1611472A
- Authority
- CN
- China
- Prior art keywords
- molecular sieve
- catalytic cracking
- zsm
- propylene
- above olefin
- Prior art date
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Links
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 26
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 16
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims description 19
- 238000004519 manufacturing process Methods 0.000 title abstract description 5
- 239000002808 molecular sieve Substances 0.000 claims abstract description 44
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000000034 method Methods 0.000 claims abstract description 25
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 23
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 18
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 20
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 13
- 239000000377 silicon dioxide Substances 0.000 claims description 13
- 239000013078 crystal Substances 0.000 claims description 11
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 8
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 5
- 239000005977 Ethylene Substances 0.000 claims description 4
- 238000010504 bond cleavage reaction Methods 0.000 claims description 2
- 230000003197 catalytic effect Effects 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 238000004230 steam cracking Methods 0.000 claims description 2
- 238000012216 screening Methods 0.000 claims 1
- 239000003054 catalyst Substances 0.000 abstract description 9
- 230000008929 regeneration Effects 0.000 abstract description 2
- 238000011069 regeneration method Methods 0.000 abstract description 2
- KMWBBMXGHHLDKL-UHFFFAOYSA-N [AlH3].[Si] Chemical compound [AlH3].[Si] KMWBBMXGHHLDKL-UHFFFAOYSA-N 0.000 abstract 1
- 238000009776 industrial production Methods 0.000 abstract 1
- 239000002994 raw material Substances 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 7
- 239000002245 particle Substances 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 2
- 239000011230 binding agent Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000001125 extrusion Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 1
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- IYABWNGZIDDRAK-UHFFFAOYSA-N allene Chemical compound C=C=C IYABWNGZIDDRAK-UHFFFAOYSA-N 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000012299 nitrogen atmosphere Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Catalysts (AREA)
Abstract
The invention relates to a kind of method for manufacturing propylene by catalytic cracking alkene of no less than tetra carbon, which mainly solves the short catalyst regeneration period problem and the stability problems uninvolved in previous technique. The invention uses minor crystalline grain and molecular sieve with high silicon-aluminium ratio as the catalyst for catalytic cracking with alkene that no less than tetra carbon to manufacture propylene. According to the technique scheme that described above, the invention can solve the problems mentioned above excellently, and can be used in industrial production of manufacturing propylene by catalytic cracking with alkene.
Description
Technical field
The present invention relates to the method for carbon four and above olefin catalytic cracking to produce propylene thereof.
Background technology
In the world wide, the appreciable C of quantity is arranged at present
4And C
4Above olefin feedstock.Be subjected to the influence of factors such as the variation in Chemicals market and transportation cost, it is a kind of approach that utilizes preferably that these raw materials are carried out deep processing on the spot.C wherein
4And C
4It is a kind of promising technology that above conversion of olefines becomes propylene.This technology can be utilized superfluous, that added value is lower relatively C on the one hand
4And C
4Above olefin feedstock can obtain broad-spectrum propylene product again on the other hand.
Document WO 9929805 has proposed a kind of utilization and has contained C
4And C
4The method of above olefin production propylene.Catalyzer uses SiO in the document
2/ Al
2O
3Than 600～2000 high silica alumina ratio ZSM-5 molecular sieve, temperature of reaction is 540～580 ℃, the liquid volume air speed of raw material 10～30 hours
-1The ZSM-5 molecular sieve that uses in the document is the business-like molecular sieve of ZEOCATP2-2 (Chemie Ueticon AG of Switzerland), the grain size of not mentioned molecular sieve, and also the silica alumina ratio of molecular sieve is higher.Use the hybrid C 4 behind the refinery MTBE to be raw material in the document, olefin(e) centent 52%, and deviate from diolefin through selective hydrogenation, and the propene yield initial stage is 29.2%, reacts after 500 hours, propene yield is 23.1%.
Proposing a kind of among the document CN 1274342A is raw material with the hydro carbons, produces the method for ethene and propylene by catalyzed conversion.It is the mesopore zeolite of 5～6.5 dusts that catalyzer adopts the aperture, does not mention the size of molecular sieve in the document, does not also have the data of catalyst stability among the embodiment.
Proposed a kind of among the document EP 0109059A1 C
4～C
12Conversion of olefines is the technology of propylene.Catalyzer uses SiO in the document
2/ Al
2O
3Than the ZSM-5 molecular sieve that is less than or equal to 220, temperature of reaction is 400～600 ℃, and the alkene air speed was greater than 50 hours
-1Investigated the influence of the raw material, temperature of reaction, air speed of various artificial preparations in this patent in more detail to catalytic cracking reaction.Yet the lower (SiO of silica alumina ratio of the ZSM-5 molecular sieve catalyst that uses in the document
2/ Al
2O
3Smaller or equal to 220), and all do not carry out the study on the stability of catalyzer among the embodiment in the above-mentioned document, just provide the initial activity of catalyzer.
Proposed a kind of in the document WO 90/11338 C
4～C
12Alkane is converted into C
2～C
4The technology of alkene.A kind of technology of hydrocarbon polymer being produced gaseous olefin through catalyzed conversion has been proposed among the EP 0305720.
Summary of the invention
Technical problem to be solved by this invention is that to overcome the catalyst regeneration cycle that exists in the document in the past short or do not relate to the problem of stability, and a kind of new carbon four and the method for above olefin catalytic cracking to produce propylene thereof are provided.This method has purpose product propene yield height, simultaneously the good characteristics of catalyst stability.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: the method for a kind of carbon four and above olefin catalytic cracking to produce propylene thereof, and with silica alumina ratio SiO
2/ Al
2O
3Be that 100～1000 ZSM type molecular sieve is a catalyzer, material carbon four and above alkene thereof are 400～600 ℃ in temperature of reaction, and reaction pressure is 0～0.15MPa, and weight space velocity WHSV is 1～30 hour
-1Scission reaction takes place under the condition generate propylene, the crystal grain diameter of wherein used ZSM type molecular sieve is for being less than or equal to 1 μ.
Carbon four and above olefin feedstock thereof are from the C-4-fraction of steam cracking device in the mixed c 4 of plant catalytic cracker or the ethylene plant in the technique scheme.The temperature of reaction preferable range is 500～580 ℃, and weight space velocity WHSV preferable range is 2～20 hours
-1, silica alumina ratio SiO
2/ Al
2O
3Preferable range is 200～800, and more preferably scope is 230～600; ZSM type molecular sieve preferred version is for being selected from ZSM-5 molecular sieve or ZSM-11 molecular sieve, and more preferably scheme is for being selected from the ZSM-5 molecular sieve.The crystal grain diameter preferable range of used ZSM type molecular sieve is 0.01～1 micron, and more preferably scope is 0.1～0.5 micron.
The Preparation of catalysts method of using among the present invention is: earlier according to proportion ingredient, and crystallization under 80～180 ℃ of temperature, agitation condition, the synthetic molecular sieve, through the stripper plate agent, the exchange back adds Al
2O
3Or SiO
2As binding agent, by extrusion moulding, the consumption of binding agent is generally 0～70% (weight).Silica alumina ratio (the SiO of the ZSM type zeolite that uses in the catalyzer of the present invention
2/ Al
2O
3) reaction there is certain influence.In general, the catalyzer of low silica alumina ratio helps improving the conversion of olefines rate, and the catalyzer of high silica alumina ratio more helps improving the selectivity of propylene.
The present invention improves the stability of catalyzer by the method that adopts the grain size of controlling ZSM type molecular sieve.Because the molecular sieve pore passage of little crystal grain is shorter, diffusional resistance is little, helps the diffusion of reactant and product, therefore can reduce the generation because of the long side reaction that causes of the residence time; The outer specific surface that small crystal grain molecular sieve is bigger also has bigger appearance carbon ability in addition; Simultaneously small crystal grain molecular sieve also more helps the uniform distribution of framework aluminum, thereby the acid site that forms disperses more, evenly.Just because of above-mentioned reason, small crystal grain molecular sieve has had better anti-carbon deposition ability and stability.At 500 ℃, weight space velocity 10 hours
-1Condition under, the initial stage yield of purpose product propylene reaches 37.9%, react 24 days (576 hours) after, propene yield has been obtained better technical effect still greater than 30%.
Description of drawings
Accompanying drawing 1 is a catalyst A-1, B-1, the examination beta stability line of C-1.
Accompanying drawing 2 is the different air speed examination of a catalyzer D-1 curve.
Accompanying drawing 3 is checked and rated curve for catalyzer D-1 to take out surplus mixed c 4 raw material.
Accompanying drawing 4 is the examination curve of catalyzer E-1.
The invention will be further elaborated below by embodiment.
Embodiment
[embodiment 1～3]
The size of zeolite crystal has remarkable influence to the stability of catalyzer.According to the proportioning and the synthetic respectively A of crystallization condition of table 1, B, the ZSM-5 molecular sieve of three kinds of particle diameters of C.
Table 1
| Molecular sieve | Proportioning | Crystallization condition | Particle diameter (SEM) |
| ????A | ?600SiO 2∶Al 2O 3∶30TPABr∶26OH -1∶7600H 2O | 180 ℃, 24 hours | The 20-30 micron |
| ????B | ?600SiO 2∶Al 2O 3∶30TPABr∶80NaCl∶26OH -1∶7600H 2O | 160 ℃, 48 hours | 1 micron |
| ????C | ?600SiO 2∶Al 2O 3∶30TPABr∶80NaCl∶26OH -1∶7600H 2O | 140 ℃, 60 hours | 0.2 micron |
TPABr is a 4-propyl bromide.
5 gram ZSM-5 molecular sieve-4 As are placed 200 milliliters, 5% weight NH
4NO
3In the solution, exchange is 2 hours under 85～90 ℃ of temperature, repeats 3 times.Exchange is after washing, 120 ℃ of oven dry obtain the ZSM-5 molecular sieve of Hydrogen.After the ZSM-5 molecular sieve of 4 gram Hydrogens adds the silicon sol mixing of 6.7 grams 40%, extrusion moulding.Through 120 ℃ of oven dry, make the A-1 catalyzer after 400 ℃ of roastings again.Adopt same quadrat method, use molecular sieve B, C makes catalyst B-1 and catalyzer C-1.
The activation 2 hours under 500 ℃, nitrogen atmosphere of reaction procatalyst.The C that uses in the experiment
4Raw material is from the surplus mixed c 4 of taking out in the ethylene plant.The raw material composition sees Table 2.
Take out surplus mixed c 4 and form table 2 ethylene plant
| Project | Raw material is formed (weight %) |
| Trimethylmethane | ????1.81 |
| Normal butane | ????5.05 |
| Propadiene | ????0.12 |
| Acetylene | ????0.08 |
| Anti-butylene | ????11.25 |
| Butene-1 | ????32.07 |
| Iso-butylene | ????43.39 |
| Maleic | ????6.20 |
| ????C 4More than | ????0.04 |
Adopt A-1 respectively, B-1 and C-1 catalyzer are raw material to take out surplus mixed c 4, and at 550 ℃, weight space velocity is 16 hours
-1Condition under react, the results are shown in Figure 1.As seen from Figure 1, the molecular sieve of little crystal grain has stability preferably.
[embodiment 4～6]
Prepare the method for molecular sieve C with reference to table 1, change the silica alumina ratio of molecular sieve, according to SiO
2/ Al
2O
3=450 proportioning, preparation molecular sieve D, the particle diameter of molecular sieve D is 0.5 micron, prepares catalyzer D-1 according to the identical method of embodiment 1-3 then.
Adopting the D-1 catalyzer, is raw material to take out surplus mixed c 4, and at 550 ℃, adopting weight space velocity respectively is 2 hours
-1, 16 hours
-1, 19 hours
-1Condition react, the results are shown in Figure 2.
[embodiment 7]
Adopting the D-1 catalyzer, is raw material to take out surplus mixed c 4, changes temperature of reaction, and at 580 ℃, weight space velocity is 16 hours
-1, condition under react, the results are shown in Figure 3.
[embodiment 8]
Prepare the method for molecular sieve C with reference to table 1, change the silica alumina ratio of molecular sieve, according to SiO
2/ Al
2O
3=230 proportioning, preparation molecular sieve E, the particle diameter of molecular sieve E is 0.1 micron, prepares catalyzer E-1 according to embodiment 1～3 identical method then.
Adopting the E-1 catalyzer, is raw material to take out surplus mixed c 4, and at 500 ℃, weight space velocity is 10 hours
-1, condition under react, the results are shown in Figure 4.
Claims (7)
1, the method for a kind of carbon four and above olefin catalytic cracking to produce propylene thereof is with silica alumina ratio SiO
2/ Al
2O
3Be that 100～1000 ZSM type molecular sieve is a catalyzer, material carbon four and above alkene thereof are 400～600 ℃ in temperature of reaction, and reaction pressure is 0～0.15MPa, and weight space velocity WHSV is 1～30 hour
-1Scission reaction takes place under the condition generate propylene, the crystal grain diameter that it is characterized in that used ZSM type molecular sieve is for being less than or equal to 1 micron.
2,, it is characterized in that carbon four and above olefin feedstock thereof C-4-fraction from steam cracking device in the mixed c 4 of plant catalytic cracker or the ethylene plant according to the method for described carbon four of claim 1 and above olefin catalytic cracking to produce propylene thereof.
3, according to the method for described carbon four of claim 1 and above olefin catalytic cracking to produce propylene thereof, it is characterized in that temperature of reaction is 500～580 ℃, weight space velocity WHSV is 2～20 hours
-1, silica alumina ratio SiO
2/ Al
2O
3Be 200～800, ZSM type molecular screening is from ZSM-5 molecular sieve or ZSM-11 molecular sieve.
4,, it is characterized in that ZSM type molecular sieve is the ZSM-5 molecular sieve according to the method for described carbon four of claim 3 and above olefin catalytic cracking to produce propylene thereof.
5, according to the method for described carbon four of claim 3 and above olefin catalytic cracking to produce propylene thereof, it is characterized in that silica alumina ratio SiO
2/ Al
2O
3Be 230～600.
6, according to the method for described carbon four of claim 1 and above olefin catalytic cracking to produce propylene thereof, the crystal grain diameter that it is characterized in that ZSM type molecular sieve is 0.01～1 micron.
7, according to the method for described carbon four of claim 6 and above olefin catalytic cracking to produce propylene thereof, the crystal grain diameter that it is characterized in that ZSM type molecular sieve is 0.1～0.5 micron.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200310108178XA CN1274645C (en) | 2003-10-27 | 2003-10-27 | Method for producing propene for C4 and more olefin catalytic cracking |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200310108178XA CN1274645C (en) | 2003-10-27 | 2003-10-27 | Method for producing propene for C4 and more olefin catalytic cracking |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1611472A true CN1611472A (en) | 2005-05-04 |
| CN1274645C CN1274645C (en) | 2006-09-13 |
Family
ID=34758500
Family Applications (1)
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|---|---|---|---|
| CNB200310108178XA Expired - Lifetime CN1274645C (en) | 2003-10-27 | 2003-10-27 | Method for producing propene for C4 and more olefin catalytic cracking |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100368359C (en) * | 2005-08-15 | 2008-02-13 | 中国石油化工股份有限公司 | Production system for increasing production of propylene |
| CN100368358C (en) * | 2005-08-15 | 2008-02-13 | 中国石油化工股份有限公司 | Method for producing propylene continuously in switch mode |
| CN100398499C (en) * | 2005-08-15 | 2008-07-02 | 中国石油化工股份有限公司 | Method for producing propylene by using cracking olefin of carbon four and higher |
| CN100460368C (en) * | 2005-08-15 | 2009-02-11 | 中国石油化工股份有限公司 | Production system of propylene |
| CN100460367C (en) * | 2005-08-15 | 2009-02-11 | 中国石油化工股份有限公司 | Method for producing propylene by using cracking olefin of carbon four and higher |
| US8137631B2 (en) | 2008-12-11 | 2012-03-20 | Uop Llc | Unit, system and process for catalytic cracking |
| CN101619011B (en) * | 2008-06-30 | 2012-07-25 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by catalytic cracking |
| CN102603457A (en) * | 2012-01-17 | 2012-07-25 | 马俊杰 | Production device and process for generating propylene by utilizing C3 and C4 in liquid gas deep processing |
| US8246914B2 (en) | 2008-12-22 | 2012-08-21 | Uop Llc | Fluid catalytic cracking system |
| US8889076B2 (en) | 2008-12-29 | 2014-11-18 | Uop Llc | Fluid catalytic cracking system and process |
| CN106608779A (en) * | 2015-10-21 | 2017-05-03 | 中国石油化工股份有限公司 | Method for producing propylene through catalytic cracking |
| CN107915564A (en) * | 2016-10-10 | 2018-04-17 | 中国石油化工股份有限公司 | The method of four~carbon of carbon, eight olefins by catalytic cracking |
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| CN101172922B (en) * | 2006-11-02 | 2010-05-12 | 中国石油化工股份有限公司 | Method for producing propylene with C_4 alkene catalytic pyrolysis |
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2003
- 2003-10-27 CN CNB200310108178XA patent/CN1274645C/en not_active Expired - Lifetime
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100368359C (en) * | 2005-08-15 | 2008-02-13 | 中国石油化工股份有限公司 | Production system for increasing production of propylene |
| CN100368358C (en) * | 2005-08-15 | 2008-02-13 | 中国石油化工股份有限公司 | Method for producing propylene continuously in switch mode |
| CN100398499C (en) * | 2005-08-15 | 2008-07-02 | 中国石油化工股份有限公司 | Method for producing propylene by using cracking olefin of carbon four and higher |
| CN100460368C (en) * | 2005-08-15 | 2009-02-11 | 中国石油化工股份有限公司 | Production system of propylene |
| CN100460367C (en) * | 2005-08-15 | 2009-02-11 | 中国石油化工股份有限公司 | Method for producing propylene by using cracking olefin of carbon four and higher |
| CN101619011B (en) * | 2008-06-30 | 2012-07-25 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by catalytic cracking |
| US8137631B2 (en) | 2008-12-11 | 2012-03-20 | Uop Llc | Unit, system and process for catalytic cracking |
| US8246914B2 (en) | 2008-12-22 | 2012-08-21 | Uop Llc | Fluid catalytic cracking system |
| US8889076B2 (en) | 2008-12-29 | 2014-11-18 | Uop Llc | Fluid catalytic cracking system and process |
| CN102603457A (en) * | 2012-01-17 | 2012-07-25 | 马俊杰 | Production device and process for generating propylene by utilizing C3 and C4 in liquid gas deep processing |
| CN102603457B (en) * | 2012-01-17 | 2014-01-08 | 马俊杰 | Production device and process for generating propylene by utilizing C3 and C4 in liquid gas deep processing |
| CN106608779A (en) * | 2015-10-21 | 2017-05-03 | 中国石油化工股份有限公司 | Method for producing propylene through catalytic cracking |
| CN106608779B (en) * | 2015-10-21 | 2019-02-19 | 中国石油化工股份有限公司 | The method of catalytic cracking for producing propylene |
| CN107915564A (en) * | 2016-10-10 | 2018-04-17 | 中国石油化工股份有限公司 | The method of four~carbon of carbon, eight olefins by catalytic cracking |
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| Publication number | Publication date |
|---|---|
| CN1274645C (en) | 2006-09-13 |
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