CN103044180B - A kind of method that dehydrogenation of isobutane prepares isobutene - Google Patents
A kind of method that dehydrogenation of isobutane prepares isobutene Download PDFInfo
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- CN103044180B CN103044180B CN201210580247.6A CN201210580247A CN103044180B CN 103044180 B CN103044180 B CN 103044180B CN 201210580247 A CN201210580247 A CN 201210580247A CN 103044180 B CN103044180 B CN 103044180B
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- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 title claims abstract description 87
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 239000001282 iso-butane Substances 0.000 title claims abstract description 43
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 61
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 61
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 57
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- 238000006243 chemical reaction Methods 0.000 claims abstract description 49
- 239000002994 raw material Substances 0.000 claims abstract description 24
- 230000008929 regeneration Effects 0.000 claims abstract description 24
- 238000011069 regeneration method Methods 0.000 claims abstract description 24
- 239000007787 solid Substances 0.000 claims abstract description 19
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052593 corundum Inorganic materials 0.000 claims abstract description 11
- 230000035484 reaction time Effects 0.000 claims abstract description 11
- 229910001845 yogo sapphire Inorganic materials 0.000 claims abstract description 11
- 238000011084 recovery Methods 0.000 claims abstract description 8
- 150000001336 alkenes Chemical class 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 10
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 238000005984 hydrogenation reaction Methods 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 claims 1
- 238000005342 ion exchange Methods 0.000 claims 1
- 239000002502 liposome Substances 0.000 abstract description 9
- 239000002105 nanoparticle Substances 0.000 abstract description 9
- 230000001172 regenerating effect Effects 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000000463 material Substances 0.000 abstract 1
- 238000006722 reduction reaction Methods 0.000 abstract 1
- 235000013847 iso-butane Nutrition 0.000 description 34
- 239000007789 gas Substances 0.000 description 12
- 239000011651 chromium Substances 0.000 description 10
- 239000007795 chemical reaction product Substances 0.000 description 8
- 238000004587 chromatography analysis Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 230000002779 inactivation Effects 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000003795 chemical substances by application Substances 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
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 3
- 239000003915 liquefied petroleum gas Substances 0.000 description 3
- 238000005504 petroleum refining Methods 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 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
- 230000008901 benefit Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- QDOXWKRWXJOMAK-UHFFFAOYSA-N dichromium trioxide Chemical compound O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- WJQOZHYUIDYNHM-UHFFFAOYSA-N 2-tert-Butylphenol Chemical compound CC(C)(C)C1=CC=CC=C1O WJQOZHYUIDYNHM-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 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
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- CERQOIWHTDAKMF-UHFFFAOYSA-M Methacrylate Chemical compound CC(=C)C([O-])=O CERQOIWHTDAKMF-UHFFFAOYSA-M 0.000 description 1
- 229920002367 Polyisobutene Polymers 0.000 description 1
- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 description 1
- -1 alkane Hydrocarbon Chemical class 0.000 description 1
- 229920005549 butyl rubber Polymers 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 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
- 230000008021 deposition Effects 0.000 description 1
- 230000018109 developmental process Effects 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
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 description 1
- 229910052697 platinum Inorganic materials 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
- 238000001179 sorption measurement Methods 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
- 229910052905 tridymite Inorganic materials 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention reside in the process that a kind of dehydrogenation of isobutane of offer prepares isobutene.Solid Cr is specifically prepared with solid liposome nanoparticle2O3 –CaO‑K2O‑Al2O3For catalyst, in 530 590 DEG C of reaction temperature, the 0.5MPa of reaction pressure 0.1, the 1.5h of reaction mass air speed 1.0‑1Under conditions of, after dehydrogenation reaction 5 30 minutes, stop reaction raw materials isobutane feed under identical reaction conditions, by the h of hydrogen volume air speed 10 1000‑1Speed be passed through hydrogen to reactor, to catalyst carry out hydrogen reducing regeneration；The ratio in hydrogen reducing recovery time and reaction time presses 13:1 control；After hydrogen reducing regeneration ending, stop hydrogen charging, switch to raw material isobutane feed, so circulate repeatedly.Using present invention process method, on-line continuous reducing/regenerating can be carried out with dehydrogenation of isobutane catalyst, increase substantially catalyst service life, simplification of flowsheet, reduction reaction process energy consumption and material consumption.
Description
Technical field
The present invention relates to the preparation of isobutene, specifically dehydrogenation of isobutane prepares the process of isobutene, to prolong
Long catalyst usage cycles, simplify reaction process flow, the method that reduction raw material iso-butane is damaged.
Background technology
Isobutene is a kind of very important organic chemical industry's intermediate, mainly for the preparation of methyl tertiary butyl ether(MTBE)（MTBE is high
Octane number clean gasoline blend component）, butyl rubber, polyisobutene, methacrylate, tertiary butyl phenol, tert-butylamine, 1,4- fourths two
The various Organic Ingredients such as alcohol, ABS resin and fine chemicals.
With continually developing for isobutene downstream product and its derivative, the demand of isobutene expands day by day, conventional
Steam cracking process, due to the restriction of its own production technology, makes isobutene volume increase be restricted.In addition, with natural gas work
The development of industry, the liquefied petroleum gas of petroleum refining industry progressively reduces as the market of domestic fuel, exploitation liquefied petroleum gas
Chemical utilization technology is one of key that petroleum refining industry is increased the benefit with the level of resources utilization.Containing big in liquefied petroleum gas
Iso-butane resource is measured, therefore exploitation dehydrogenation of isobutane prepares isobutene, is to expand isobutene raw material sources and raising petroleum refining
One important channel of industrial efficiency.
Existing a few industrialized dehydrogenation of isobutane of set prepare isobutene technology in the world at present, including Uop Inc. of the U.S.
Oleflex techniques, ABB Lummus catofin techniques, the star techniques of Phillips companies and Italy
The FBD-4 of Snamprogetti SPA companies and the Linde techniques of Linde companies of Germany.Dehydrogenation of isobutane prepares isobutene
Catalyst is broadly divided into two major classes, chromium-based catalysts and platinum-group noble metals catalyst.Such as USP4506032, USP4595673 public affairs
Catalyst of carried noble metal platinum and preparation method thereof is on the alumina support opened；Such as Hakuli is in 11%CrOx/SiO2
（Mass fraction in terms of Cr）On catalyst, 18% isobutene yield is obtained at 540 DEG C, but the selectivity of isobutene is relatively low
（72%）, and there is serious carbon deposition phenomenon, cause catalyst inactivation (A. Hakuli, et al. J. Catal., 1999,
184:349-356）.The method that these traditional dehydrogenation of isobutane prepare isobutene, because reaction temperature is high, reaction velocity is low and catalysis
The problems such as easy carbon distribution in agent surface, causes its target product selectivity low, and catalyst easy in inactivation.
Low-carbon alkanes oxidative dehydrogenation is a kind of exothermic reaction, can be carried out at a lower temperature, and due to the introducing of oxygen
Catalyst surface carbon distribution can be eliminated, so that isobutene for oxo-dehydrogenation producing of isobutylene method attracts attention.Such as
Oxidation of isobutane is all disclosed in the patents such as CN101138738B, CN1044787C, CN101439292A, CN101618319A
Dehydrogenation prepares the catalyst and process of isobutene.However, in the presence of oxygen, the target product of isobutene for oxo-dehydrogenation
Deep oxidation reaction easily occurs for alkene and raw material iso-butane, causes the selectivity of raw material iso-butane and target product olefins low
Problem.
As can be seen here, dehydrogenation of isobutane, which prepares isobutene, causes the principal element of catalyst inactivation to be that low-molecular olefine is being urged
Coking in agent, covering catalyst active center causes its activity reduction.At present, open source literature report dehydrogenation of isobutane catalyst
Regeneration use coke burning regeneration mode, its regeneration period is generally 9 hours.By the way of frequent coke burning regeneration, not only lead
Cause technological process complicated, and the loss of raw material iso-butane can be caused.And have not yet to see document and patent to disclose report other
Regeneration.
The content of the invention
It is an object of the invention to provide a kind of process of hydrogen reducing regeneration, it not only can significantly extend catalyst
The single trip use life-span, and technological process is simple, and raw material isobutane losses are small.
Inventor prepares solid Cr by studying with a kind of solid liposome nanoparticle2O3 –CaO-K2O-Al2O3（Wherein Cr2O3
Content be catalyst quality fraction 60-90%, CaO content be catalyst quality fraction 3-12%, K2O content is to urge
0.5-3.0%, Al of agent mass fraction2O3Content be catalyst quality fraction 5-36.5%, by inventor prepare synthesize）
Isobutene catalyst is prepared for dehydrogenation of isobutane, is found under the catalyst action, dehydrogenation of isobutane is prepared in isobutene reaction
The inactivation of catalyst mainly due to the olefin adsorption generated in course of reaction catalyst activity position on, with the reaction time
Polymerisation further occurs for alkene in extension, the alkene being adsorbed on catalyst activity position and reaction product, generates macromolecular
Olefin polymer is the principal element of catalyst inactivation.Dehydrogenation of isobutane catalyst is also simultaneously olefin hydrogenation catalyst, is this
Hydrogen reducing regeneration is carried out to the catalyst after the shorter reaction time using hydrogen, under dehydrogenation reaction conditions to adsorbing
Alkene on catalyst activity position carries out hydrogenation reaction, alkene of the absorption on catalyst activity position is converted into corresponding alkane
Hydrocarbon, so as to be desorbed from catalyst activity position, is improved catalyst activity stability.
The present invention has following advantage：
1st, hydrogen is one kind in dehydrogenation of isobutane reaction product, and product separation system can be directly utilized using hydrogen regeneration,
Residual raw materials iso-butane in reactor is reclaimed, significant loss can be both greatly lowered, simplifies the technique stream of conventional regeneration mode again
Journey；
2nd, the condition of hydrogen reducing regeneration is identical with reaction condition, and reaction and regeneration switching are easily operated, and are easy to reaction
The control of system and steady operating.
Embodiment
Following example will be further described to the method that provides of the present invention, but and be not so limited the present invention.
Solid Cr is prepared with a kind of solid liposome nanoparticle2O3 –CaO-K2O-Al2O3For catalyst, in reaction temperature 530-
590 DEG C, reaction pressure 0.1-0.5MPa, reaction mass air speed 1.0-1.5h-1Under conditions of, after dehydrogenation reaction 5-30 minutes,
Stop reaction raw materials isobutane feed under identical reaction conditions, by hydrogen volume air speed 10-1000 h-1Speed to reaction
Device is passed through hydrogen, and hydrogen reducing regeneration is carried out to catalyst；The ratio in hydrogen reducing recovery time and reaction time presses 1-3:1 control
System；After hydrogen reducing regeneration ending, stop hydrogen charging, switch to raw material isobutane feed, so circulate repeatedly.
Embodiment 1
Solid Cr is prepared with a kind of solid liposome nanoparticle2O3 –CaO-K2O-Al2O3For catalyst, in reaction temperature 530
DEG C, reaction pressure 0.2MPa, reaction mass air speed 1.0h-1Under conditions of, after dehydrogenation reaction 5 minutes, bar is reacted in identical
Stop reaction raw materials isobutane feed under part, by hydrogen volume air speed 10:1 speed is passed through hydrogen to reactor, to catalyst
Carry out hydrogen reducing regeneration；The ratio in hydrogen reducing recovery time and reaction time presses 1:1 control, i.e. hydrogen reducing 5 minutes；Hydrogen
After reducing/regenerating terminates, stop hydrogen charging, switch to raw material isobutane feed, so circulate repeatedly.Reaction product airbag
Collect, gas chromatographic analysis the results are shown in Table 1.
Embodiment 2
Solid Cr is prepared with a kind of solid liposome nanoparticle2O3 –CaO-K2O-Al2O3For catalyst, in reaction temperature 550
DEG C, reaction pressure 0.1MPa, reaction mass air speed 1.0h-1Under conditions of, after dehydrogenation reaction 10 minutes, bar is reacted in identical
Stop reaction raw materials isobutane feed under part, by hydrogen volume air speed 100:1 speed is passed through hydrogen to reactor, to catalyst
Carry out hydrogen reducing regeneration；The ratio in hydrogen reducing recovery time and reaction time presses 2:1 control, i.e. hydrogen reducing 20 minutes；Hydrogen
After gas reducing/regenerating terminates, stop hydrogen charging, switch to raw material isobutane feed, so circulate repeatedly.Reaction product gas
Bag is collected, and gas chromatographic analysis the results are shown in Table 1.
Embodiment 3
Solid Cr is prepared with a kind of solid liposome nanoparticle2O3 –CaO-K2O-Al2O3For catalyst, in reaction temperature 580
DEG C, reaction pressure 0.5MPa, reaction mass air speed 1.5h-1Under conditions of, after dehydrogenation reaction 15 minutes, bar is reacted in identical
Stop reaction raw materials isobutane feed under part, by hydrogen volume air speed 200:1 speed is passed through hydrogen to reactor, to catalyst
Carry out hydrogen reducing regeneration；The ratio in hydrogen reducing recovery time and reaction time presses 2:1 control, i.e. hydrogen reducing 30 minutes；Hydrogen
After gas reducing/regenerating terminates, stop hydrogen charging, switch to raw material isobutane feed, so circulate repeatedly.Reaction product gas
Bag is collected, and gas chromatographic analysis the results are shown in Table 1.
Embodiment 4
Solid Cr is prepared with a kind of solid liposome nanoparticle2O3 –CaO-K2O-Al2O3For catalyst, in reaction temperature 570
DEG C, reaction pressure 0.3MPa, reaction mass air speed 1.3h-1Under conditions of, after dehydrogenation reaction 5 minutes, bar is reacted in identical
Stop reaction raw materials isobutane feed under part, by hydrogen volume air speed 500:1 speed is passed through hydrogen to reactor, to catalyst
Carry out hydrogen reducing regeneration；The ratio in hydrogen reducing recovery time and reaction time presses 3:1 control, i.e. hydrogen reducing 15 minutes；Hydrogen
After gas reducing/regenerating terminates, stop hydrogen charging, switch to raw material isobutane feed, so circulate repeatedly.Reaction product gas
Bag is collected, and gas chromatographic analysis the results are shown in Table 1.
Embodiment 5
Solid Cr is prepared with a kind of solid liposome nanoparticle2O3 –CaO-K2O-Al2O3For catalyst, in reaction temperature 560
DEG C, reaction pressure 0.3MPa, reaction mass air speed 1.5h-1Under conditions of, after dehydrogenation reaction 30 minutes, bar is reacted in identical
Stop reaction raw materials isobutane feed under part, by hydrogen volume air speed 1000:1 speed is passed through hydrogen to reactor, to catalysis
Agent carries out hydrogen reducing regeneration；The ratio in hydrogen reducing recovery time and reaction time presses 1:1 control, i.e. hydrogen reducing 30 minutes；
After hydrogen reducing regeneration ending, stop hydrogen charging, switch to raw material isobutane feed, so circulate repeatedly.Reaction product is used
Airbag is collected, and gas chromatographic analysis the results are shown in Table 1.
The comparative example of embodiment 6
Solid Cr is prepared with a kind of solid liposome nanoparticle2O3 –CaO-K2O-Al2O3For catalyst, in reaction temperature 560
DEG C, reaction pressure 0.1MPa, reaction mass air speed 1.0h-1Under conditions of, dehydrogenation reaction is carried out, reaction product is collected with airbag,
Gas chromatographic analysis, the results are shown in Table 1.
The dehydrogenation of isobutane of table 1 prepares isobutene catalyst Evaluation results
Note：X- is iso-butane conversion ratio, %；S- product selective isobutenes, %.
Claims (3)
1. a kind of method that dehydrogenation of isobutane prepares isobutene, it is characterised in that：Dehydrogenation reaction conditions are：Reaction temperature 530-
590 DEG C, reaction pressure 0.1-0.5MPa, the mass space velocity 1.0-1.5h of reaction raw materials iso-butane-1；The dehydrogenation used for
Cr2O3–CaO-K2O-Al2O3Oxide；
After 5-30 minutes dehydrogenation reaction time, then stop reaction raw materials isobutane feed under identical reaction conditions, together
When be passed through hydrogen to reactor, to catalyst carry out hydrogen reducing regeneration, under dehydrogenation reaction conditions to adsorb catalyst live
Property position on alkene carry out hydrogenation reaction, make absorption catalyst activity position on alkene be converted into corresponding alkane so that from
Catalyst activity is desorbed on position, is improved catalyst activity stability；After hydrogen reducing regeneration ending, stop hydrogen
Charging, switches to raw material isobutane feed and carries out dehydrogenation reaction, so circulation repeatedly.
2. according to the method described in claim 1, it is characterised in that：The catalyst that dehydrogenation of isobutane prepares isobutene is with solid-state
Ion exchange prepares solid Cr2O3–CaO-K2O-Al2O3Oxide.
3. according to the method described in claim 1, it is characterised in that：By hydrogen volume air speed 10-1000h-1Speed to reaction
Device is passed through hydrogen, and hydrogen reducing regeneration is carried out to catalyst；The ratio in hydrogen reducing recovery time and reaction time presses 1-3:1 control
System.
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| CN201210580247.6A CN103044180B (en) | 2012-12-28 | 2012-12-28 | A kind of method that dehydrogenation of isobutane prepares isobutene |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
| 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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| Publication number | Priority date | Publication date | Assignee | Title |
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| JPS5932447B2 (en) * | 1982-04-12 | 1984-08-09 | 三菱瓦斯化学株式会社 | Method for producing olefin |
| DE3416672A1 (en) * | 1984-05-05 | 1985-11-07 | Veba Oel AG, 4650 Gelsenkirchen | METHOD FOR DEHYDRATING HYDROCARBONS |
| US5461179A (en) * | 1993-07-07 | 1995-10-24 | Raytheon Engineers & Constructors, Inc. | Regeneration and stabilization of dehydrogenation catalysts |
| US5476981A (en) * | 1993-12-29 | 1995-12-19 | Sun Company, Inc. (R&M) | Oxidative dehydrogenation of hydrocarbons with solid superacid catalyst |
| DE102007036750A1 (en) * | 2007-08-03 | 2009-02-05 | Uhde Gmbh | Regeneration of catalysts for the dehydrogenation of alkanes |
| CN102794167A (en) * | 2012-06-15 | 2012-11-28 | 北京石油化工学院 | Catalyst for preparing isobutene by isobutane dehydrogenation and preparation method for catalyst |
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