CN102070390A - Method for preparing propylene from refinery mixed C4 - Google Patents
Method for preparing propylene from refinery mixed C4 Download PDFInfo
- Publication number
- CN102070390A CN102070390A CN2011100053467A CN201110005346A CN102070390A CN 102070390 A CN102070390 A CN 102070390A CN 2011100053467 A CN2011100053467 A CN 2011100053467A CN 201110005346 A CN201110005346 A CN 201110005346A CN 102070390 A CN102070390 A CN 102070390A
- Authority
- CN
- China
- Prior art keywords
- propylene
- catalytic cracking
- mixed
- tower
- refinery
- 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
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
- Y02P20/10—Process efficiency
Abstract
The invention discloses a method for preparing propylene from refinery mixed C4, which mainly solves the problems of low added value of the refinery mixed C4, low utilization efficiency of most of components, high energy consumption and the like existing in the prior art. According to the technical scheme, the method is realized by the following steps of: (1) allowing the refinery mixed C4 to pass through a catalytic distillation tower to isomerize butylene-1 into butylene-2, performing tower top separation to obtain light C4, and performing tower kettle separation to obtain heavy C4; (2) feeding the heavy C4 into a catalytic cracking reactor, wherein most of the butylene-2 is converted; (3) compressing a catalytic cracking reaction product and allowing the product to pass through a rectification unit to obtain a main polymer grade propylene product, a cracked gasoline byproduct, unreacted C4 and a C2<-> fraction; and (4) circulating most of the unreacted C4 and the C2<-> fraction to the catalytic cracking reactor. The method can be applied to the industrial field for producing the propylene.
Description
Technical field
The present invention relates to the method for a kind of refinery mixed c 4 system propylene.
Background technology
Mixed c 4 is one of main by product of refinery.Refinery's mixed c 4 is mainly from catalytic cracking unit (FCC), and other devices are few as viscosity breaking, thermally splitting and coking by-product mixed c 4 total amount.The by-product mixed c 4 total amount of catalytic cracking unit with form different and different according to cracking level and catalyzer.Generally, the mixed c 4 amount of catalytic cracking unit by-product is approximately the 9%-12% (weight) of device fresh feed, its compositing characteristic is butane (especially Trimethylmethane) content height, butadiene content is considerably less, and butylene is about about 50% (weight), and the typical case forms (weight) and is: Trimethylmethane: 34%, normal butane: 10%, iso-butylene: 15%, butene-1: 13%, butene-2: 28%.Most refinery utilizes ether-based device to separate and has utilized iso-butylene wherein, after this content of alkene is approximately about 45% (weight) in the remaining mixed c 4, the typical case of mixed c 4 composition (weight) is after the etherificate: Trimethylmethane: 40%, normal butane: 11%, butene-1: 17%, butene-2: 28%.Therefore, if this kind material directly carries out catalytic cracking reaction, under quite lower temperature of reaction, the butane in the reaction raw materials can't carry out cracking, have a large amount of invalid materials to exist in the device, cause plant investment increase, energy consumption to increase.
At present, the mixed c 4 major part after the domestic refinery etherificate is used as fuel and uses, and chemical utilization is worth very low.By the end of the year 2009, Chinese crude oil time processing ability reaches 4.77 hundred million tons, and over the past two years, China be constructed and put into operation and the oil-refining capacity of building can reach 5000 surplus ten thousand tons.Therefore, will there be future a large amount of refineries mixed c 4 to occur, and how improve after refinery's etherificate the chemical utilization of mixed c 4 and be worth and have great realistic meaning.
Utilizing mixed c 4 after refinery's etherificate to produce propylene is to have one of solution than hi-tech economy, particularly under the background environment of soaring oil prices.Propylene is one of basic Organic Chemicals, is mainly used in many products such as producing polypropylene, isopropyl benzene, propylene oxide, vinyl cyanide, vinylformic acid, to the national economy important influence.In recent years, propylene year demand in continuous growth, its annual growth has surpassed the important light olefin of another one: the annual growth of ethene.Propylene mainly still obtains by preparing ethylene by steam cracking device and catalytic cracking unit, accounts for about 65% of propylene source.In addition, developed the technology of many production propylene both at home and abroad, for example technology such as dehydrogenating propane, preparing propylene from methanol.Utilize the mixed c 4 of refinery's by-product to produce propylene, not only improved the chemical industry added value of mixed c 4, and satisfied market the ever-increasing demand of propylene.
Document ZL200510110295 has introduced a kind of technology of utilizing producing propylene ethane by carbon-containing olefin catalytic cracking.By selecting molecular sieve catalyst for use, under no shared material condition, carbonaceous olefin mixture is carried out catalytic pyrolysis, the weight yield of propylene, ethene is not less than 60% (with respect to alkene total amount in the fresh feed) in the products therefrom.The catalytic pyrolysis product further separates through the later separation unit, obtains the propylene that weight concentration is 90-99%, ethene, recycled propane, pyrolysis gasoline and the C of 90-99% respectively
4-C
5Cut, the wherein C of 20-80% (weight ratio)
4-C
5The cut circulation enters reactor.Concentration of olefin in this processing requirement raw material is higher, if raw material is the mixed c 4 after refinery's etherificate, with causing a large amount of inert raw material Trimethylmethanes to accumulate, has improved plant investment and plant energy consumption inevitably in system.
Document EP 109059 has been introduced a kind of C
4-C
12Mixed olefins prepares the technology of propylene and ethylene, and this technology does not have shared material equally, and the raw material mixed olefins is directly greater than 50hr
-1Weight space velocity under carry out scission reaction.This production technique is not very high to the selectivity of propylene, and to C
5The selectivity of above cut is on the contrary greater than 33%.In addition, this technology is not separated inertia alkane yet, will cause plant investment and energy consumption to waste greatly.
The described technology of above-mentioned document all is under the condition of no shared raw material mixed olefins to be carried out catalytic pyrolysis, produces propylene and ethylene.Because the separation of inertialess alkane in the technology, the olefin(e) centent in the two processing requirement raw materials is higher.If the raw material of these two process application is the mixed c 4 after refinery's etherificate, will be unfavorable for utilizing substantially this mixed c 4, and will strengthens plant investment and plant energy consumption.
Summary of the invention
The present invention relates to a kind of method of utilizing refinery's mixed c 4 system propylene, be mainly used in by refinery's mixed c 4 and produce propylene.
The objective of the invention is to produce propylene by the mixed c 4 that refinery's by product is preferably after the etherificate, technical problem to be solved be low, the most of component utilising efficiency of the chemical utilization added value of refinery's mixed c 4 in the conventional art low, utilize problem such as energy consumption height, a kind of new method of producing propylene by refinery's mixed c 4 is provided.Present method has been utilized the alkene in the mixed c 4 substantially, has reduced the inert component Trimethylmethane in the device simultaneously, has greatly reduced plant investment and comprehensive energy consumption.In addition, the C of most of unreacted carbon four and scission reaction generation
2 -The cut circulation fully transforms the alkene in the carbon four on the one hand, and maximization improves the yield of propylene, has reduced the olefin partial pressures in the reaction raw materials on the other hand, helps the scission reaction of alkene.At last, present method is separated the Trimethylmethane that obtains higher concentration, can further obtain the Trimethylmethane product of extreme high purity with less cost.Therefore, present method has the comprehensive utilization ratio height and the chemical industry added value advantages of higher of propene yield height, refinery's mixed c 4.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: the method for a kind of refinery mixed c 4 system propylene may further comprise the steps:
(1) refinery's mixed c 4 is by a catalytic distillation tower, and butene-1 is tautomerized to butene-2, and cat head separation simultaneously obtains light carbon four, and the tower still obtains heavy carbon four;
(2) heavy carbon four enters a catalytic cracking reaction device, and butene-2 is wherein transformed by major part;
(3) catalytic cracking reaction products obtains major product polymerization-grade propylene, byproduct pyrolysis gasoline, unreacted carbon four and C respectively by rectification cell after compression
2 -Cut;
(4) most unreacted carbon four of circulation and C
2 -Cut is to the catalytic cracking reaction device.
In the technique scheme, refinery's mixed c 4 is preferably the mixed c 4 behind the ether-based device, iso-butylene content trace, and Trimethylmethane content is greater than 35%.
Catalytic distillation is preferably and adopts shared raw material, and shared raw material is preferably hydrogen; Conversion zone is preferably the filling hydroisomerisation catalysts, and catalyzer is preferably alumina load metallic nickel, zinc and/or palladium.
Main ingredient in the light carbon four is preferably Trimethylmethane, and content is preferably more than 90% (weight); Main ingredient in the heavy carbon four is preferably butene-2, normal butane, and wherein butene-2 content is preferably more than 70% (weight).
The catalytic cracking reaction device is preferably the filling molecular sieve catalyst, and catalyzer is preferably ZSM, SAPO, β zeolite equimolecular sieve, more preferably type ZSM 5 molecular sieve or SAPO molecular sieve.
The catalytic cracking reaction device is preferably fixed-bed reactor or fluidized-bed reactor; Temperature of reaction is preferably 450-550 ℃, and reaction pressure is preferably 0.1-0.5MPa.
Rectification cell is preferably and comprises one section compression, soda-wash tower, depropanizing tower, debutanizing tower, second-compressed, deethanizing column and propylene rectification tower successively.
Be circulated to the unreacted C of catalytic cracking reaction device
4Proportion is preferably 10%-100% (volume), more preferably 33%-95% (volume).
Be circulated to the C of catalytic cracking reaction device
2 -The cut proportion is preferably 67-100% (volume), more preferably 80-95% (volume).
The inventive method is at first utilized the isoversion technology, and making the light constituent butene-1 isomerization in the mixed c 4 is the heavy constituent butene-2, helps the Trimethylmethane in the mixed c 4 after the separating plant etherificate, does not reduce the olefin(e) centent in the mixed c 4 simultaneously again.The light carbon of separating four that is mainly Trimethylmethane can further obtain the high purity Trimethylmethane of high added value by lower cost, and the heavy carbon of separating four that is mainly butene-2 can obtain the propylene of high added value by catalytic cracking reaction.In addition, because the inert component Trimethylmethane is separated, the invalid material in the device reduces, and the investment of device and working cost can reduce significantly.
At last, the present invention is the C of most of unreacted mixed c 4 and scission reaction generation
2 -The cut circulation enters reactor, fully transforms alkene wherein on the one hand, improves propene yield; Because scission reaction is the reaction that molecule increases, the dividing potential drop that reduces reactant helps promoting the carrying out of scission reaction on the other hand, so the circulation of these two strands of materials can reduce the dividing potential drop of alkene in the reaction raw materials, promotes the carrying out of olefin cracking reaction.Utilize method of the present invention, under the same device treatment scale situation, the yield of propylene of the present invention can improve about 50% compared to conventional art.Therefore, the propene yield height of the inventive method has made full use of refinery's mixed c 4 preferably, has improved the added value of refinery's mixed c 4, has obtained the good technical effect.
Description of drawings
Fig. 1 is the schematic flow sheet of technology of the present invention;
Fig. 2 is the schematic flow sheet of document ZL200510110295;
Fig. 1 numbers explanation:
A, catalytic distillation knockout tower; B, catalytic cracking reaction device; C1/C2: compressor; D, soda-wash tower; E, depropanizing tower; F, deethanizing column; G, debutanizing tower; H, propylene rectification tower.
1, mixed c 4; 2, light carbon four (Trimethylmethane); 3, heavy carbon four (butene-2+normal butane); 4, C
4 +Cut; 5, C
3 -Cut; 6, C
5 +Cut; 7, circulation C
48, circulation C
2 -Cut; 9, C
3Cut; 10, non-condensable gas; 11, polymerization-grade propylene; 12, liquefied gas (mixed c 4), 13: alkaline solution.
Fig. 2 numbers explanation:
I, reactor; J, process furnace; K, fractional distillating tube; L, gas-liquid separator; M, compressor; N, first knockout tower; O, second knockout tower; P, the 3rd knockout tower; Q, the 4th knockout tower.
1, raw material carbonaceous olefin mixture; 14, C
6Above cut; 15, gaseous ethene product; 16, pyrolysis gasoline; 17, round-robin C
4-C
5Cut; 18, the outer C of out-of-bounds
4-C
5Cut; 19, recycled propane; 20, liquid propylene product; 21, noncondensable gas.
Among Fig. 1, mix carbon 41 after refinery's etherificate and enter catalytic distillation knockout tower A, in this tower, butene-1 is turned to butene-2 by isomery, mixes simultaneously carbon four and is divided into two parts: the heavy carbon 43 (being mainly butene-2 and normal butane) of the light carbon 42 (being mainly iso-butane) of cat head and tower reactor. Light carbon 42 can further separate the highly purified iso-butane product of acquisition by lower cost. The heavy carbon 43 of tower reactor and unreacted carbon 47 and the circulation C of circulation2 -Cut 8 enters from the top of catalytic cracking reaction device B together, alkene generation cracking reaction in the reaction raw materials, product enters caustic wash tower D after compressing by one section compression unit C1, and the dried product of alkali cleaning is by depropanizing tower E, and the overhead product that obtains is C3 -Cut 5, tower kettle product are C4 +Cut 4. C3 -Cut 5 further compresses by compressor C2, enters then dethanizer F. That the deethanization cat head obtains is C2 -Cut 8, tower reactor obtains C3Cut 9. Most C2 -Cut 8 is recycled and enters the catalytic cracking reaction device. C3It is further refining that cut 9 enters propylene rectification tower H, and lateral line withdrawal function obtains the polymerization-grade propylene product. C4 +Cut enters debutanizing tower G, and cat head obtains unreacted C4, tower reactor obtains C5 +Cut 6. Most of unreacted C4Circulation enters the catalytic cracking reaction device, remaining unreacted C4After merging with the still liquid of propylene rectification tower H, go out the battery limit (BL) as liquefied gas product 12. C5 +Cut can be by hydrogenation directly as gasoline products or extracting aromatic component wherein.
The invention will be further elaborated below by embodiment.
Embodiment
[comparative example 1]
By shown in Figure 2, mixed c 4 composition (weight %) is after refinery's etherificate: Trimethylmethane: 40%, and normal butane: 15%, butene-1: 17%, butene-2: 28%.Catalyzer is the ZSM-5 molecular sieve of silica alumina ratio 200, and reactor is one section fixed-bed reactor, and reaction velocity is 30 hours
-1(weight hourly space velocity), temperature of reaction are 550 ℃, and reaction pressure is 0.05MPa, the C of 70 weight %
4Above cut circulation is as cracking stock, and the getable propylene product of device of year 100000 tons of mixed c 4 scales of processing is 1.2 ten thousand tons/year.
[embodiment 1]
By shown in Figure 1, mixed c 4 composition (weight %) is after refinery's etherificate: Trimethylmethane: 40%, and normal butane: 15%, butene-1: 17%, butene-2: 28%.The hydroisomerisation catalysts that catalytic distillation adopts is the alumina load metallic nickel.The catalytic cracking reaction device adopts fixed bed, and the catalyzer of filling is the ZSM-5 molecular sieve catalyst, and temperature of reaction is preferably 510 ℃, and reaction pressure is preferably 0.18MPa.Be circulated to the unreacted C of catalytic cracking reaction device
4Proportion is 95% (volume), is circulated to the C of catalytic cracking reaction device
2 -The cut proportion is 95% (volume), experimental results show that adopting the resulting propylene product of device of handling 100,000 tons of mixed c 4 scales year of the present invention is 2.0 ten thousand tons/year.
[embodiment 2]
By shown in Figure 1, mixed c 4 composition (weight %) is after refinery's etherificate: Trimethylmethane: 40%, and normal butane: 15%, butene-1: 17%, butene-2: 28%.The hydroisomerisation catalysts that catalytic distillation adopts is alumina load palladium metal and zinc.The catalytic cracking reaction device adopts fluidized-bed, and the catalyzer of filling is the SAPO-34 molecular sieve catalyst, and temperature of reaction is preferably 460 ℃, and reaction pressure is preferably 0.25MPa.Be circulated to the unreacted C of catalytic cracking reaction device
4Proportion is 80% (volume), is circulated to the C of catalytic cracking reaction device
2 -The cut proportion is 80% (volume), experimental results show that adopting the resulting propylene product of device of handling 100,000 tons of mixed c 4 scales year of the present invention is 1.8 ten thousand tons/year.
[embodiment 3]
By shown in Figure 1, mixed c 4 composition (weight %) is after refinery's etherificate: Trimethylmethane: 40%, and normal butane: 15%, butene-1: 17%, butene-2: 28%.The hydroisomerisation catalysts that catalytic distillation adopts is the alumina load metallic nickel.The catalytic cracking reaction device adopts fixed bed, and the catalyzer of filling is the ZSM-5 molecular sieve catalyst, and temperature of reaction is preferably 460 ℃, and reaction pressure is preferably 0.1MPa.Be circulated to the unreacted C of catalytic cracking reaction device
4Proportion is 66% (volume), is circulated to the C of catalytic cracking reaction device
2 -The cut proportion is 85% (volume), experimental results show that adopting the resulting propylene product of device of handling 100,000 tons of mixed c 4 scales year of the present invention is 1.7 ten thousand tons/year.
Claims (9)
1. the method for refinery's mixed c 4 system propylene may further comprise the steps:
(1) refinery's mixed c 4 is by a catalytic distillation tower, and butene-1 is tautomerized to butene-2, and cat head separation simultaneously obtains light carbon four, and the tower still obtains heavy carbon four;
(2) heavy carbon four enters a catalytic cracking reaction device, and butene-2 is wherein transformed by major part;
(3) catalytic cracking reaction products obtains major product polymerization-grade propylene, byproduct pyrolysis gasoline, unreacted carbon four and C respectively by rectification cell after compression
2 -Cut;
(4) most unreacted carbon four of circulation and C
2 -Cut is to the catalytic cracking reaction device.
2. according to the method for the described system propylene of claim 1, it is characterized in that refinery's mixed c 4 is the mixed c 4 behind the ether-based device, iso-butylene content trace, Trimethylmethane content is greater than 35%.
3. according to the method for the described system propylene of claim 1, it is characterized in that it is hydrogen that catalytic distillation adopts shared raw material; Conversion zone filling hydroisomerisation catalysts, catalyzer is alumina load metallic nickel, zinc and/or palladium.
4. according to the method for the described system propylene of claim 1, it is characterized in that the main ingredient in the light carbon four is a Trimethylmethane, content is greater than 90% (weight); Main ingredient in the heavy carbon four is butene-2, normal butane, and wherein butene-2 content is greater than 70% (weight).
5. according to the method for the described system propylene of claim 1, it is characterized in that catalytic cracking reaction device filling molecular sieve catalyst, catalyzer is ZSM, and SAPO, β zeolite equimolecular sieve are preferably type ZSM 5 molecular sieve or SAPO molecular sieve.
6. according to the method for claim 1 and 5 described system propylene, it is characterized in that the catalytic cracking reaction device is fixed-bed reactor or fluidized-bed reactor; Temperature of reaction is 450-550 ℃, and reaction pressure is 0.1-0.5MPa.
7. according to the method for the described system propylene of claim 1, it is characterized in that rectification cell comprises one section compression, soda-wash tower, depropanizing tower, debutanizing tower, second-compressed, deethanizing column and propylene rectification tower successively.
8. according to the method for the described system propylene of claim 1, it is characterized in that being circulated to the unreacted C of catalytic cracking reaction device
4Proportion is 10%-100% (volume), is preferably 33%-95% (volume).
9. according to the method for the described system propylene of claim 1, it is characterized in that being circulated to the C of catalytic cracking reaction device
2 -The cut proportion is 67-100% (volume), is preferably 80-95% (volume).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110005346.7A CN102070390B (en) | 2011-01-12 | 2011-01-12 | The method of refinery's mixed c 4 propylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110005346.7A CN102070390B (en) | 2011-01-12 | 2011-01-12 | The method of refinery's mixed c 4 propylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102070390A true CN102070390A (en) | 2011-05-25 |
| CN102070390B CN102070390B (en) | 2016-03-16 |
Family
ID=44029172
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110005346.7A Expired - Fee Related CN102070390B (en) | 2011-01-12 | 2011-01-12 | The method of refinery's mixed c 4 propylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102070390B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105367366A (en) * | 2014-08-27 | 2016-03-02 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by means of mixed C4 |
| CN107226776A (en) * | 2017-05-11 | 2017-10-03 | 黑龙江安瑞佳石油化工有限公司 | Feedstock pre-processing system and processing method |
| CN112225654A (en) * | 2020-11-02 | 2021-01-15 | 中国海洋石油集团有限公司 | Device and method for comprehensively utilizing mixed C4 |
| CN115340436A (en) * | 2021-05-14 | 2022-11-15 | 中国石油天然气集团有限公司 | Separation device and separation method for olefin catalytic cracking |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1762931A (en) * | 2005-10-28 | 2006-04-26 | 清华大学 | Method for producing propene using silicoaluminophosphate molecular sieve catalytic cracking |
| CN101198572A (en) * | 2005-04-15 | 2008-06-11 | Abb拉默斯环球有限公司 | Process for the double bond hydroisomerization of butenes |
| 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 |
| CN101279879A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for producing propone by comprehensive utilization of mixed C4 |
| CN101492335A (en) * | 2008-01-23 | 2009-07-29 | 中国石油化工股份有限公司 | Combination method for comprehensive utilization of mix C4 |
| CN101885660A (en) * | 2009-05-13 | 2010-11-17 | 中国石油化工股份有限公司 | C4 hydrocarbon catalysis and separation method capable of separating isobutene and butene-2 |
-
2011
- 2011-01-12 CN CN201110005346.7A patent/CN102070390B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101198572A (en) * | 2005-04-15 | 2008-06-11 | Abb拉默斯环球有限公司 | Process for the double bond hydroisomerization of butenes |
| CN1762931A (en) * | 2005-10-28 | 2006-04-26 | 清华大学 | Method for producing propene using silicoaluminophosphate molecular sieve catalytic cracking |
| 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 |
| CN101279879A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for producing propone by comprehensive utilization of mixed C4 |
| CN101492335A (en) * | 2008-01-23 | 2009-07-29 | 中国石油化工股份有限公司 | Combination method for comprehensive utilization of mix C4 |
| CN101885660A (en) * | 2009-05-13 | 2010-11-17 | 中国石油化工股份有限公司 | C4 hydrocarbon catalysis and separation method capable of separating isobutene and butene-2 |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105367366A (en) * | 2014-08-27 | 2016-03-02 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by means of mixed C4 |
| CN105367366B (en) * | 2014-08-27 | 2017-10-27 | 中国石油化工股份有限公司 | Utilize the method for mixing the production of carbon four ethene, propylene |
| CN107226776A (en) * | 2017-05-11 | 2017-10-03 | 黑龙江安瑞佳石油化工有限公司 | Feedstock pre-processing system and processing method |
| CN112225654A (en) * | 2020-11-02 | 2021-01-15 | 中国海洋石油集团有限公司 | Device and method for comprehensively utilizing mixed C4 |
| CN115340436A (en) * | 2021-05-14 | 2022-11-15 | 中国石油天然气集团有限公司 | Separation device and separation method for olefin catalytic cracking |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102070390B (en) | 2016-03-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102070391B (en) | The method of comprehensive utilization mixed c 4 preparing isobutene | |
| CN101492334B (en) | Method for improving mixed C4 chemical industry exploitation value | |
| CN101475429B (en) | Method for comprehensive utilization of cracking C4 | |
| CN101555197B (en) | Comprehensive use method of mixed C-4 | |
| CN104945228B (en) | A kind of method for preparing MTBE or isobutene with mixing butane | |
| CN101279879B (en) | Method for producing propone by comprehensive utilization of mixed C4 | |
| CN106608783B (en) | Method for preparing dimethylbenzene from methanol | |
| CN102285852B (en) | Utilize the method for refinery C four increasing output of ethylene and propylene | |
| CN101492335B (en) | Combination method for comprehensive utilization of mix C4 | |
| CN103420750A (en) | Method for preparing olefin from low-carbon alkane | |
| CN103772123B (en) | Method for increasing yield of BTX aromatics | |
| CN102070390B (en) | The method of refinery's mixed c 4 propylene | |
| CN101585747B (en) | Method for transforming oxygenates into propylene | |
| CN111116290B (en) | Energy expanding method for olefin cracking device | |
| CN100418938C (en) | Method for separating product of carbonaceous olefin catalytic cracking | |
| CN102603452A (en) | Method for preparing isoalkenes through isomerizing linear alkenes | |
| CN104672046A (en) | Method of increasing ethylene and propylene yields by freshening C-4 olefins in catalytic cracking or pyrolysis process after separation | |
| CN102286292B (en) | Method for increase production of propylene and ethylene by pyrolyzing C4 raffinate | |
| CN105085147B (en) | The method of preparing low-carbon olefin from oxygen-containing compounds | |
| CN107522586B (en) | Alkyne treatment method for butadiene preparation process by oxidative dehydrogenation of butene | |
| CN110437868B (en) | Method for producing high value-added product by using mixed C4 | |
| CN102285851A (en) | Method for increasing yields of ethylene and propylene | |
| CN103772121B (en) | The method of C9 and above heavy arene component cracking fecund trimethylbenzene | |
| CN102070389A (en) | Technology for preparing propylene by utilizing by-products in refinery | |
| CN102285857A (en) | Method for increasing yields of propylene and ethylene |
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 | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160316 Termination date: 20200112 |