CN103044180A - Method for preparing isobutylene by dehydrogenizing iso-butane - Google Patents
Method for preparing isobutylene by dehydrogenizing iso-butane Download PDFInfo
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- CN103044180A CN103044180A CN2012105802476A CN201210580247A CN103044180A CN 103044180 A CN103044180 A CN 103044180A CN 2012105802476 A CN2012105802476 A CN 2012105802476A CN 201210580247 A CN201210580247 A CN 201210580247A CN 103044180 A CN103044180 A CN 103044180A
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- isobutane
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- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 title claims abstract description 92
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 239000001282 iso-butane Substances 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 24
- 235000013847 iso-butane Nutrition 0.000 title abstract 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000001257 hydrogen Substances 0.000 claims abstract description 62
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 62
- 238000006243 chemical reaction Methods 0.000 claims abstract description 57
- 239000003054 catalyst Substances 0.000 claims abstract description 33
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 33
- 230000008929 regeneration Effects 0.000 claims abstract description 30
- 238000011069 regeneration method Methods 0.000 claims abstract description 30
- 239000002994 raw material Substances 0.000 claims abstract description 24
- 239000007787 solid Substances 0.000 claims abstract description 19
- 230000035484 reaction time Effects 0.000 claims abstract description 10
- 230000000694 effects Effects 0.000 claims description 11
- 150000001336 alkenes Chemical class 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 7
- 238000005984 hydrogenation reaction Methods 0.000 claims description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 2
- 238000003795 desorption Methods 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract 1
- 229910052593 corundum Inorganic materials 0.000 abstract 1
- 238000005265 energy consumption Methods 0.000 abstract 1
- 238000005342 ion exchange Methods 0.000 abstract 1
- 239000000463 material Substances 0.000 abstract 1
- 230000002035 prolonged effect Effects 0.000 abstract 1
- 229910001845 yogo sapphire Inorganic materials 0.000 abstract 1
- 239000011651 chromium Substances 0.000 description 11
- 239000007795 chemical reaction product Substances 0.000 description 8
- 239000007789 gas Substances 0.000 description 7
- 238000004587 chromatography analysis Methods 0.000 description 6
- 239000003915 liquefied petroleum gas Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000009849 deactivation Effects 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000005504 petroleum refining Methods 0.000 description 3
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000003672 processing method Methods 0.000 description 3
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000002779 inactivation Effects 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- JHPBZFOKBAGZBL-UHFFFAOYSA-N (3-hydroxy-2,2,4-trimethylpentyl) 2-methylprop-2-enoate Chemical compound CC(C)C(O)C(C)(C)COC(=O)C(C)=C JHPBZFOKBAGZBL-UHFFFAOYSA-N 0.000 description 1
- WJQOZHYUIDYNHM-UHFFFAOYSA-N 2-tert-Butylphenol Chemical compound CC(C)(C)C1=CC=CC=C1O WJQOZHYUIDYNHM-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 229910019923 CrOx Inorganic materials 0.000 description 1
- VHOQXEIFYTTXJU-UHFFFAOYSA-N Isobutylene-isoprene copolymer Chemical group CC(C)=C.CC(=C)C=C VHOQXEIFYTTXJU-UHFFFAOYSA-N 0.000 description 1
- 229920002367 Polyisobutene Polymers 0.000 description 1
- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- YBRBMKDOPFTVDT-UHFFFAOYSA-N tert-butylamine Chemical compound CC(C)(C)N YBRBMKDOPFTVDT-UHFFFAOYSA-N 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
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
Abstract
The invention provides a process method for preparing isobutylene by dehydrogenizing iso-butane. Particularly, solid Cr2O3-CaO-K2O-Al2O3 used as a catalyst is prepared by solid-state ion-exchange; after dehydrogenation reaction is performed for 5 to 30 minutes under the conditions of reaction temperature of 530 to 590 DEG C, reaction pressure of 0.1 to 0.5MPa, reaction quality space velocity of 1.0 to 1.5h<-1>, feeding of a reaction raw material (iso-butane) is stopped under the same reaction conditions, hydrogen is filled into a reactor according to hydrogen volume space velocity of 10 to 1,000h<-1> and the catalyst is subjected to hydrogen reduction regeneration; a ratio of hydrogen reduction regeneration time to reaction time is controlled according to a ratio of (1 to 3):1; and after hydrogen reduction regeneration is finished, feeding of the hydrogen is stopped, feeding of the hydrogen is switched into feeding of the raw material (iso-butane) and the operation is cycled and repeated. With adoption of the process method disclosed by the invention, online continuous reduction regeneration on the iso-butane dehydrogenization catalyst can be carried out, service life of the catalyst can be greatly prolonged, process flow is simplified, and energy consumption and material consumption of the reaction process are reduced.
Description
Technical field
The present invention relates to the preparation of iso-butylene, is the processing method that dehydrogenation of isobutane prepares iso-butylene specifically, with the extending catalyst life cycle, simplifies the reaction process flow process, reduces the method that the raw material Trimethylmethane decreases.
Background technology
Iso-butylene is a kind of very important organic chemical industry's intermediate, mainly for the preparation of methyl tertiary butyl ether (MTBE, the clean gasoline with high octane blend component), various organic raw material and the fine chemicals such as isoprene-isobutylene rubber, polyisobutene, methacrylic ester, tertiary butyl phenol, TERTIARY BUTYL AMINE, BDO, ABS resin.
Along with continually developing of iso-butylene derived product and derivative thereof, the demand expanding day of iso-butylene, conventional steam cracking process is because the restriction of himself production technology is restricted the iso-butylene volume increase.In addition, along with the development of gas industry, the liquefied petroleum gas (LPG) of petroleum refining industry is progressively dwindled as the market of domestic fuel, and the chemical utilization technology of exploitation liquefied petroleum gas (LPG) is that petroleum refining industry is increased the benefit and one of key of the level of resources utilization.Contain a large amount of Trimethylmethane resources in the liquefied petroleum gas (LPG), therefore developing dehydrogenation of isobutane prepares iso-butylene, is an important channel expanding the iso-butylene raw material sources and improve the petroleum refining industry benefit.
The existing industrialized dehydrogenation of isobutane of several covers prepares the iso-butylene technology in the world at present, comprises the FBD-4 of the star technique of catofin technique, Phillips company of oleflex technique, the ABB Lummus of American UOP company and Italian Snamprogetti SPA company and the Linde technique of German Linde company.The catalyzer that dehydrogenation of isobutane prepares iso-butylene mainly is divided into two large class, chromium-based catalysts and platinum family noble metal catalysts.The Catalysts and its preparation method of carried noble metal platinum on alumina supporter is disclosed such as USP4506032, USP4595673 etc.; Such as Hakuli etc. at the massfraction of 11%CrOx/SiO2(in Cr) on the catalyzer, obtained 18% iso-butylene yield in the time of 540 ℃, but the selectivity of iso-butylene lower (72%), and there is serious carbon distribution phenomenon, cause catalyst deactivation (A. Hakuli, et al. J. Catal., 1999,184:349-356).These traditional dehydrogenation of isobutane prepare the method for iso-butylene, and are high because of temperature of reaction, reaction velocity is low and the problem such as the easy carbon distribution of catalyst surface causes its target product selectivity low, and the easy inactivation of catalyzer.
Low-carbon alkanes oxydehydrogenation is a kind of thermopositive reaction, can carry out under lower temperature, again because the introducing of oxygen can be eliminated the catalyst surface carbon distribution, thereby the isobutene for oxo-dehydrogenation producing of isobutylene method is received publicity.As all disclosing catalyzer and the processing method of isobutene for oxo-dehydrogenation producing of isobutylene in the patents such as CN101138738B, CN1044787C, CN101439292A, CN101618319A.Yet in the presence of oxygen, deep oxidation reaction easily occurs in the target product alkene of isobutene for oxo-dehydrogenation and raw material Trimethylmethane, causes the problems such as the selectivity of raw material Trimethylmethane and target product alkene is low.
This shows, it is low-molecular olefine coking on catalyzer that dehydrogenation of isobutane prepares the principal element that iso-butylene causes catalyst deactivation, covers catalyst active center and causes its activity decreased.At present, the coke burning regeneration mode is adopted in the regeneration of open source literature report dehydrogenation of isobutane catalyzer, and its regeneration period is generally 9 hours.Adopt the mode of frequent coke burning regeneration, not only cause technical process complicated, and can cause the loss of raw material Trimethylmethane.And have not yet to see document and patent and openly report other regeneration.
Summary of the invention
The object of the present invention is to provide the processing method of a kind of hydrogen reducing regeneration, significant one way work-ing life of extending catalyst not only, and also technical process is simple, and the raw material Trimethylmethane loses little.
The contriver is by studying with the standby solid Cr of a kind of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3(Cr wherein
2O
3Content be that the content of 60-90%, the CaO of catalyst quality mark is 3-12%, the K of catalyst quality mark
2The content of O is 0.5-3.0%, the Al of catalyst quality mark
2O
3Content be the 5-36.5% of catalyst quality mark, prepared synthetic by the contriver) prepare isobutene catalyst for dehydrogenation of isobutane, discovery is under this catalyst action, the inactivation that dehydrogenation of isobutane prepares catalyzer in the isobutene reaction mainly is because the alkene that generates in the reaction process is adsorbed on the catalyst activity position, prolongation along with the reaction times, be adsorbed in the further polymerization reaction take place of alkene in alkene on the catalyst activity position and the reaction product, generating the macromole olefin polymer is the principal element of catalyst deactivation.The dehydrogenation of isobutane catalyzer also is olefin hydrogenation catalyst simultaneously, adopt hydrogen to carry out hydrogen reducing regeneration through the catalyzer of shorter reaction after the time for this reason, under dehydrogenation reaction conditions, the alkene that is adsorbed on the catalyst activity position is carried out hydrogenation reaction, making the conversion of olefines that is adsorbed on the catalyst activity position is corresponding alkane, thereby desorption gets off from the catalyst activity position, and catalyst activity stability is improved.
The present invention has following advantage:
1, hydrogen is a kind of in the dehydrogenation of isobutane reaction product, adopts hydrogen regeneration can directly utilize product separation system, reclaims residual raw materials Trimethylmethane in the reactor, but both decrease significant loss is simplified again the technical process of conventional regeneration mode;
2, the condition of hydrogen reducing regeneration is identical with reaction conditions, and reaction is switched easy handling with regeneration, and is easy to control and the smooth operation of reactive system.
Embodiment
Following example will be further described method provided by the invention, but therefore not limit the present invention.
With the standby solid Cr of a kind of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3Be catalyzer, at temperature of reaction 530-590 ℃, reaction pressure 0.1-0.5MPa, reaction mass air speed 1.0-1.5h
-1Condition under, after dehydrogenation reaction 5-30 minute, stopped reaction raw material isobutane feed under identical reaction conditions is pressed hydrogen volume air speed 10-1000 h
-1Speed pass into hydrogen to reactor, catalyzer is carried out hydrogen reducing regeneration; The hydrogen reducing recovery time is pressed 1-3:1 control with the ratio in reaction times; Behind the hydrogen reducing regeneration ending, stop hydrogen feed, switch to the raw material isobutane feed, so circulation repeatedly.
Embodiment 1
With the standby solid Cr of a kind of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3Be catalyzer, at 530 ℃ of temperature of reaction, reaction pressure 0.2MPa, reaction mass air speed 1.0h
-1Condition under, in dehydrogenation reaction after 5 minutes, stopped reaction raw material isobutane feed under identical reaction conditions passes into hydrogen by the speed of hydrogen volume air speed 10:1 to reactor, and catalyzer is carried out hydrogen reducing regeneration; The hydrogen reducing recovery time is pressed 1:1 control with the ratio in reaction times, and namely hydrogen reducing is 5 minutes; Behind the hydrogen reducing regeneration ending, stop hydrogen feed, switch to the raw material isobutane feed, so circulation repeatedly.Reaction product is collected with airbag, and gas chromatographic analysis the results are shown in Table 1.
Embodiment 2
With the standby solid Cr of a kind of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3Be catalyzer, at 550 ℃ of temperature of reaction, reaction pressure 0.1MPa, reaction mass air speed 1.0h
-1Condition under, in dehydrogenation reaction after 10 minutes, stopped reaction raw material isobutane feed under identical reaction conditions passes into hydrogen by the speed of hydrogen volume air speed 100:1 to reactor, and catalyzer is carried out hydrogen reducing regeneration; The hydrogen reducing recovery time is pressed 2:1 control with the ratio in reaction times, and namely hydrogen reducing is 20 minutes; Behind the hydrogen reducing regeneration ending, stop hydrogen feed, switch to the raw material isobutane feed, so circulation repeatedly.Reaction product is collected with airbag, and gas chromatographic analysis the results are shown in Table 1.
Embodiment 3
With the standby solid Cr of a kind of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3Be catalyzer, at 580 ℃ of temperature of reaction, reaction pressure 0.5MPa, reaction mass air speed 1.5h
-1Condition under, in dehydrogenation reaction after 15 minutes, stopped reaction raw material isobutane feed under identical reaction conditions passes into hydrogen by the speed of hydrogen volume air speed 200:1 to reactor, and catalyzer is carried out hydrogen reducing regeneration; The hydrogen reducing recovery time is pressed 2:1 control with the ratio in reaction times, and namely hydrogen reducing is 30 minutes; Behind the hydrogen reducing regeneration ending, stop hydrogen feed, switch to the raw material isobutane feed, so circulation repeatedly.Reaction product is collected with airbag, and gas chromatographic analysis the results are shown in Table 1.
Embodiment 4
With the standby solid Cr of a kind of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3Be catalyzer, at 570 ℃ of temperature of reaction, reaction pressure 0.3MPa, reaction mass air speed 1.3h
-1Condition under, in dehydrogenation reaction after 5 minutes, stopped reaction raw material isobutane feed under identical reaction conditions passes into hydrogen by the speed of hydrogen volume air speed 500:1 to reactor, and catalyzer is carried out hydrogen reducing regeneration; The hydrogen reducing recovery time is pressed 3:1 control with the ratio in reaction times, and namely hydrogen reducing is 15 minutes; Behind the hydrogen reducing regeneration ending, stop hydrogen feed, switch to the raw material isobutane feed, so circulation repeatedly.Reaction product is collected with airbag, and gas chromatographic analysis the results are shown in Table 1.
Embodiment 5
With the standby solid Cr of a kind of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3Be catalyzer, at 560 ℃ of temperature of reaction, reaction pressure 0.3MPa, reaction mass air speed 1.5h
-1Condition under, in dehydrogenation reaction after 30 minutes, stopped reaction raw material isobutane feed under identical reaction conditions passes into hydrogen by the speed of hydrogen volume air speed 1000:1 to reactor, and catalyzer is carried out hydrogen reducing regeneration; The hydrogen reducing recovery time is pressed 1:1 control with the ratio in reaction times, and namely hydrogen reducing is 30 minutes; Behind the hydrogen reducing regeneration ending, stop hydrogen feed, switch to the raw material isobutane feed, so circulation repeatedly.Reaction product is collected with airbag, and gas chromatographic analysis the results are shown in Table 1.
Embodiment 6 Comparative Examples
With the standby solid Cr of a kind of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3Be catalyzer, at 560 ℃ of temperature of reaction, reaction pressure 0.1MPa, reaction mass air speed 1.0h
-1Condition under, carry out dehydrogenation reaction, reaction product is collected with airbag, gas chromatographic analysis the results are shown in Table 1.
Table 1 dehydrogenation of isobutane prepares the isobutene catalyst Evaluation results
Annotate: X-is the Trimethylmethane transformation efficiency, %; S-product selective isobutene, %.
Claims (4)
1. a dehydrogenation of isobutane prepares the method for iso-butylene, it is characterized in that: adopt hydrogen to carry out hydrogen reducing regeneration through the catalyzer of shorter reaction after the time, under dehydrogenation reaction conditions, the alkene that is adsorbed on the catalyst activity position is carried out hydrogenation reaction, making the conversion of olefines that is adsorbed on the catalyst activity position is corresponding alkane, thereby desorption gets off from the catalyst activity position, and catalyst activity stability is improved.
2. described dehydrogenation of isobutane prepares the method for iso-butylene according to claim 1, it is characterized in that: the catalyzer that dehydrogenation of isobutane prepares iso-butylene is for the standby solid Cr of solid ionic exchange system
2O
3– CaO-K
2O-Al
2O
3Oxide compound.
3. described dehydrogenation of isobutane prepares the method for iso-butylene according to claim 1, and it is characterized in that: the reaction conditions that dehydrogenation of isobutane prepares iso-butylene is: temperature of reaction 530-590 ℃, reaction pressure 0.1-0.5MPa, reaction mass air speed 1.0-1.5h
-1
4. described dehydrogenation of isobutane prepares the method for iso-butylene according to claim 1, and it is characterized in that: 5-30 minute dehydrogenation reaction time, then stopped reaction raw material isobutane feed under identical reaction conditions is pressed hydrogen volume air speed 10-1000 h
-1Speed pass into hydrogen to reactor, catalyzer is carried out hydrogen reducing regeneration; The hydrogen reducing recovery time is pressed 1-3:1 control with the ratio in reaction times; Behind the hydrogen reducing regeneration ending, stop hydrogen feed, switch to the raw material isobutane feed, so circulation repeatedly.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103706378A (en) * | 2013-12-25 | 2014-04-09 | 上海华畅环保设备发展有限公司 | Treatment method and device for concentrating, drying and detoxifying dead catalyst entrained in isobutylene during preparation of isobutylene by isobutane dehydrogenation |
| CN104098420A (en) * | 2014-08-08 | 2014-10-15 | 淄博华拓工程技术服务有限公司 | Method for preparing isobutylene with isobutane through chlorination |
| CN105817271A (en) * | 2016-04-11 | 2016-08-03 | 广东工业大学 | Regeneration method of dehydrogenation catalyst for low-carbon alkane |
| CN106348995A (en) * | 2016-08-28 | 2017-01-25 | 山东成泰化工有限公司 | Preparation method of high-purity isobutene |
| CN110937975A (en) * | 2018-09-21 | 2020-03-31 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| CN116474679A (en) * | 2023-04-27 | 2023-07-25 | 宁波昊德化学工业股份有限公司 | Method and equipment for producing isobutene |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103706378A (en) * | 2013-12-25 | 2014-04-09 | 上海华畅环保设备发展有限公司 | Treatment method and device for concentrating, drying and detoxifying dead catalyst entrained in isobutylene during preparation of isobutylene by isobutane dehydrogenation |
| WO2015096316A1 (en) * | 2013-12-25 | 2015-07-02 | 上海华畅环保设备发展有限公司 | Treating method and device for concentrating, drying and regenerating waste catalyst entrained in isobutylene in preparation of isobutylene by dehydrogenation of isobutane |
| CN103706378B (en) * | 2013-12-25 | 2016-08-17 | 上海华畅环保设备发展有限公司 | Dead catalyst concentrate drying that in preparing isobutene through dehydrogenation of iso-butane, isobutene. is carried secretly and the processing method and processing device of removing toxic substances |
| CN104098420A (en) * | 2014-08-08 | 2014-10-15 | 淄博华拓工程技术服务有限公司 | Method for preparing isobutylene with isobutane through chlorination |
| CN104098420B (en) * | 2014-08-08 | 2016-01-20 | 淄博华拓工程技术服务有限公司 | A kind of method of Trimethylmethane chloro preparing isobutene |
| CN105817271A (en) * | 2016-04-11 | 2016-08-03 | 广东工业大学 | Regeneration method of dehydrogenation catalyst for low-carbon alkane |
| CN106348995A (en) * | 2016-08-28 | 2017-01-25 | 山东成泰化工有限公司 | Preparation method of high-purity isobutene |
| CN110937975A (en) * | 2018-09-21 | 2020-03-31 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| CN116474679A (en) * | 2023-04-27 | 2023-07-25 | 宁波昊德化学工业股份有限公司 | Method and equipment for producing isobutene |
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