CN105817258B - It is a kind of for catalyst of iso-butane fluid bed dehydrogenation and preparation method thereof - Google Patents
It is a kind of for catalyst of iso-butane fluid bed dehydrogenation and preparation method thereof Download PDFInfo
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- CN105817258B CN105817258B CN201610343991.2A CN201610343991A CN105817258B CN 105817258 B CN105817258 B CN 105817258B CN 201610343991 A CN201610343991 A CN 201610343991A CN 105817258 B CN105817258 B CN 105817258B
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/03—Catalysts comprising molecular sieves not having base-exchange properties
- B01J29/0308—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41
- B01J29/0341—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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- C—CHEMISTRY; METALLURGY
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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
- C07C5/3332—Catalytic processes with metal oxides or metal sulfides
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- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/26—After treatment, characterised by the effect to be obtained to stabilize the total catalyst structure
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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Abstract
The present invention provides a kind of catalyst that isobutene is prepared for iso-butane fluid bed dehydrogenation and preparation method thereof.The catalyst is with Y2O3The SBA15 Al of modification2O3Composite oxides are carrier, Cr2O3For active component, A is coagent, and B is structural promoter；Auxiliary agent A is selected from a kind of III element A oxide, auxiliary agent B Y in a kind of IV element A oxide, carrier2O3Mass fraction for 1% ~ 5wt%, the mass fraction of SBA15 molecular sieves is 5wt% ~ 10wt%, remaining for aluminium oxide, Cr in final catalyst2O3Mass fraction for 10% ~ 15%, the mass fraction of auxiliary agent A is 1% ~ 3%, and the mass fraction of auxiliary agent B is 0.5% ~ 1.5%, and remaining is carrier.Catalyst provided by the invention has excellent dehydrogenation activity, mechanical strength and thermal stability, and industrial prospect is wide.
Description
Technical field
Generally, the present invention relates to catalyst fields.Specifically, the present invention relates to taken off for iso-butane fluidized bed catalytic
Hydrogen prepares catalyst of isobutene and preparation method thereof.
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.In recent years, with the swift and violent hair of petrochemical industry and its relevant industries
Exhibition, demand of the China to isobutene is also growing, by being volume increase isobutene by catalytic dehydrogenation of isobutane production isobutene
Effective way, but China was typically to use the low-carbon alkanes such as iso-butane as fuel in the past, this is largely reduced
The utility value of iso-butane, therefore, dehydrogenation of isobutane technology not only solve the problem of low-carbon alkanes utilization rate is low, and can be with
Greatly improve the yield of isobutene.
Dehydrogenating low-carbon alkane patented technology includes in the world：The Oleflex techniques of Uop Inc., ABB Lu Musi companies
Catofin techniques, the Star techniques of Kang Fei (Uhde) company, the FBD-4 techniques of Snamprogetti/Yarsintz companies,
The PDH techniques of Lin De/BASF AG.The technology development of China's catalytic dehydrogenation of isobutane relatively late, has related single at present
Position is being studied, but there has been no industrialization to report, domestic dehydrogenation of isobutane project uses foreign technology substantially.Dehydrogenation of isobutane
Can be divided into fixed-bed dehydrogenation, moving bed dehydrogenation and fluid bed dehydrogenation by the type of reactor of selection, be relatively fixed a dehydrogenation or
Person's moving bed De-hydrogen Technology, fluid bed dehydrogenation have many advantages, such as disposably to put into that low, continuity is strong, heat transfer efficiency is high, above-mentioned skill
Only FBD-4 techniques use fluidization in art, at present existing number set industrialized unit, and the catalyst used is contains auxiliary agent
Chromium oxide-aluminium oxide catalyst, catalyst be in microspheroidal, particle size be less than 10-4M, density are less than 2000kg/m3, have
Good fluidization characteristic and anti-erosion performance, catalyst are resistant to alkene and oxygenatedchemicals, but not preventing from heavy metal.
Patent US4746643 reports a kind of iso-butane fluid catalyst and preparation method thereof, and this method is spraying first
Drying prepares alumina support, and gained alumina support at a high temperature of more than 1100 DEG C is roasted and obtains the oxygen of δ, α crystalline phase
Change alumina supporter, then dip loading active component Cr2O3And auxiliary agent K2O finally coats SiO in fluidized bed plant2。
Patent CN104128175 reports a kind of method for preparing dehydrogenating low-carbon alkane fluid catalyst, catalyst
Quality percentage composition is：Cr2O3 5 ~ 40%, Al2O3 30 ~ 85%, MO 0.1 ~ 30%, Me2O 0.5 ~ 5%, wherein M be Mg,
The mixture of Zn or both, Me are the mixture of one or more of alkali metal, and catalyst preparation step includes carrier
The dipping of spray shaping and active component.
Invention content
For existing dehydrogenation of isobutane catalyst there are poor activity, chromic oxide content height, bad mechanical strength, hydrothermally stable not
The shortcomings of sufficient, the present invention provides one kind for fixed bed dehydrogenation of isobutane catalyst and preparation method thereof.The catalyst preparation
Process is simple, can iso-butane be efficiently changed into isobutene, has good prospects for commercial application.
Technical solution of the present invention is as follows：
A kind of catalyst for iso-butane fluid bed dehydrogenation, it is characterised in that：The catalyst is with Y2O3The SBA15- of modification
Al2O3Composite oxides are carrier, Cr2O3For active component, A is coagent, and B is structural promoter；Auxiliary agent A is selected from III A of one kind
Element oxide, auxiliary agent B Y in a kind of IV element A oxide, carrier2O3Mass fraction for 1% ~ 5wt%, the matter of SBA15
Amount score is 5wt% ~ 10wt%, remaining for aluminium oxide, Cr in final catalyst2O3Mass fraction for 10% ~ 15%, auxiliary agent A
Mass fraction is 1% ~ 3%, and the mass fraction of auxiliary agent B is 0.5% ~ 1.5%, and remaining is carrier.
More preferably, Y in carrier2O3Mass fraction for 2% ~ 3wt%, the mass fraction of SBA15 is 7wt% ~ 9wt%, remaining
For aluminium oxide, Cr in final catalyst2O3Mass fraction for 12% ~ 14%, the mass fraction of auxiliary agent A is 1.5% ~ 2%, auxiliary agent B
Mass fraction is 0.75% ~ 1.25%, and remaining is carrier；
Auxiliary agent A in the present invention is Ga2O3, auxiliary agent B SiO2；
Catalyst preparation of the present invention comprises the steps of：
(1) by hydrated alumina, hydration SBA15, containing Y2O3Compound be proportionally added into a certain amount of deionized water, stir
Uniformly, it then adds in binding agent and is beaten into suspension at a high speed；
(2) by step（1）In suspension be spray-dried to obtain microballoon, then by microballoon be placed in tube furnace and
Carrier is fired under the mixed atmosphere of vapor and air；
(3) the compound containing Cr, Ga is dissolved in deionized water and is made into certain density maceration extract, then by step（2）In
Carrier be soaked for a period of time in excessive above-mentioned maceration extract, separation maceration extract after the completion of dipping is dry；
(4) above-mentioned dried catalyst in fluidizer is fluidized, then spray into containing for certain volume on device top
The ethanol solution of silicon compound, after spraying, when fluidizer temperature being increased to required calcination temperature and maintaining one section
Between obtain final catalyst；
Step（1）Described in hydrated alumina be a kind of or their mixing visitd in aluminium stone, boehmite
Object, containing Y2O3Compound for yttrium nitrate, binding agent is nitric acid, addition（In terms of 65wt% concentrated nitric acids）For above-mentioned three kinds of solids
The 3% ~ 7% of gross mass.
Step（1）Described in suspension solid content for 25wt% ~ 55wt%, dynamic viscosity is 40mPas ~ 80m
Pa·s。
Step（2）Described in spray drying for pressure spray dryer, the microspherulite diameter of spray shaping is 20 ~ 200 μm, is mixed
The volume fraction for closing vapor in atmosphere is 10% ~ 30%, and calcination temperature is 800 DEG C, roasting time 4h, the volume of mixed atmosphere
Air speed is 500h-1~2000h-1。
Step（3）Described in the compound containing Cr be chromic nitrate, chromium acetate, chromium trioxide, one kind in ammonium dichromate,
Compound containing Ga is gallium nitrate, and the content of chromium compound is 17wt% ~ 35wt% in maceration extract, the content of gallium nitrate for 1wt% ~
3wt%, the dip time excessively impregnated are 10min, and drying temperature is 120 DEG C, drying time 30min.
Step（4）Described in siliceous compound for ethyl orthosilicate, mass fraction in ethanol is 3% ~ 6%,
The volume of the ethanol solution of penetrating is add in powder total suction 95% ~ 105%, and required calcination temperature is 750 DEG C, during maintenance
Between be 4h.
Catalyst provided by the invention is with Y2O3The SBA15-Al of modification2O3Composite oxides are carrier, and SBA15 has adjusted
The acidity of alumina support makes it be more suitable for dehydrogenation of isobutane and reacts, Y in carrier2O3Significantly improve the hydro-thermal of catalyst
Stability；Coagent Ga2O3With active component Cr2O3With coordinating effect, catalyst activity is not only increased, and reduce
Cr2O3Load capacity, the last structural promoter SiO coated in catalyst surface2The wear resistence of catalyst greatly improved.This
The catalyst that invention provides has more preferably activity, wear-resisting property, hydrothermal stability, can iso-butane be efficiently changed into isobutyl
Alkene is the ideal fluid catalyst of industrialization.
Specific embodiment
With reference to specific case study on implementation the present invention is furture elucidated the catalyst, the example enumerated is used for illustrating to urge
The composition of agent, preparation process, but the present invention is not limited with more preferably catalyst composition, preparation process.
Embodiment 1
Weigh 5kg hydrations SBA15（Containing 1.75kgSBA15）、2.54kg Y(NO3)3·6H2O, 34.8kg visits aluminium stone（Contain
22.5kgAl2O3）It is added in 168.6kg deionized waters and stirs evenly, be then slowly added to 2.85kg concentrated nitric acids while stirring,
It is beaten half an hour at a high speed, then pressure spray dryer is molded to obtain 20-200 μm of microballoon.Above-mentioned microballoon is placed in perpend Muffle
In stove, then roasted in the case where vapor volume fraction is 10% vapor-air Mixture atmosphere, calcination temperature is 800 DEG C, roasting
The burning time is 4h, and mixed atmosphere volume space velocity is 2000h-1, carrier is obtained after the completion of roasting.
Weigh the CrO of 20g3, 3.53g Ga (NO3)3It is dissolved in 117.6g deionized waters, is uniformly mixing to obtain maceration extract,
30 grams of carriers is taken to impregnate 10min in above-mentioned maceration extract, then detach maceration extract, microballoon at 120 DEG C is dried into 30min, is connect
It and fluidizes dried microballoon in fluidizer, the 3wt% ethyl orthosilicate ethanol solutions of 15ml are sprayed into from device top,
Temperature is risen to 750 DEG C after penetrating and 4h is maintained to obtain final catalyst A.
Embodiment 2
Weigh 12.8kg hydrations SBA15,3.39kg Y (NO3)3·6H2O, 34.2kg visits aluminium stone（Al containing 22.2kg2O3）、
31.8kg boehmites（Al containing 22.2kg2O3）It is added in 149.6kg deionized waters and stirs evenly, then delay while stirring
It is slow to add in 2.45kg concentrated nitric acids, it is beaten half an hour at a high speed, then pressure spray dryer is molded to obtain 20-200 μm of microballoon.It will be upper
It states microballoon to be placed in perpend Muffle furnace, then be roasted in the case where vapor volume fraction is 30% vapor-air Mixture atmosphere,
Calcination temperature is 800 DEG C, roasting time 4h, and mixed atmosphere volume space velocity is 500h-1, carrier is obtained after the completion of roasting.
Weigh the Cr (CH of 20g3COO)3, 0.571g Ga (NO3)3It is dissolved in 57.1g deionized waters, is uniformly mixing to obtain
Maceration extract takes 30 grams of carriers to impregnate 10min in above-mentioned maceration extract, then detaches maceration extract, and microballoon is dry at 120 DEG C
30min then fluidizes dried microballoon in fluidizer, and the 5wt% ethyl orthosilicate second of 18ml is sprayed into from device top
Temperature is risen to 750 DEG C after penetrating and 4h is maintained to obtain final catalyst B by alcoholic solution.
Embodiment 3
Weigh 5.7kg hydrations SBA15,2.12kg Y (NO3)3·6H2O, 31.9kg boehmites are added to 132.5kg
It is stirred evenly in deionized water, is then slowly added to 1.99kg concentrated nitric acids while stirring, is beaten half an hour at a high speed, then pressure is sprayed
Mist drying and moulding obtains 20-200 μm of microballoon.Above-mentioned microballoon is placed in perpend Muffle furnace, then in vapor volume fraction
To be roasted under 20% vapor-air Mixture atmosphere, calcination temperature is 800 DEG C, roasting time 4h, and mixed atmosphere volume is empty
Speed is 1000h-1, carrier is obtained after the completion of roasting.
Weigh (the NH of 20g4)2Cr2O4, 2g Ga (NO3)3It is dissolved in 80g deionized waters, is uniformly mixing to obtain maceration extract,
30 grams of carriers is taken to impregnate 10min in above-mentioned maceration extract, then detach maceration extract, microballoon at 120 DEG C is dried into 30min, is connect
It and fluidizes dried microballoon in fluidizer, the 6wt% ethyl orthosilicate ethanol solutions of 13ml are sprayed into from device top,
Temperature is risen to 750 DEG C after penetrating and 4h is maintained to obtain final catalyst C.
Embodiment 4
Weigh 5kg hydrations SBA15（Containing 1.75kgSBA15）、2.54kg Y(NO3)3·6H2O, 34.8kg visits aluminium stone（Contain
22.5kgAl2O3）It is added in 168.6kg deionized waters and stirs evenly, be then slowly added to 2.85kg concentrated nitric acids while stirring,
It is beaten half an hour at a high speed, then pressure spray dryer is molded to obtain 20-200 μm of microballoon.Above-mentioned microballoon is placed in perpend Muffle
In stove, then roasted in the case where vapor volume fraction is 15% vapor-air Mixture atmosphere, calcination temperature is 800 DEG C, roasting
The burning time is 4h, and mixed atmosphere volume space velocity is 1300h-1, carrier is obtained after the completion of roasting.
Weigh the CrO of 20g3, 2.5g Ga (NO3)3It is dissolved in 100g deionized waters, is uniformly mixing to obtain maceration extract, take 30
Gram carrier impregnates 10min in above-mentioned maceration extract, then detaches maceration extract, by microballoon at 120 DEG C dry 30min, then will
Dried microballoon fluidizes in fluidizer, and the 5.6wt% ethyl orthosilicate ethanol solutions of 14.6ml are sprayed into from device top,
Temperature is risen to 750 DEG C after penetrating and 4h is maintained to obtain final catalyst D.
Evaluating catalyst
The abrasion of gained catalyst are determined using mono- 1BF type powder abrasion instruments of Beijing Zhong Yililang scientific ＆ technical corporation ZYLL
Rate, and activity rating has been carried out, experimental procedure is：5ml catalyst is loaded in quartz ampoule fixed bed reactors, is warming up to 560
DEG C, it is then purged with N2, the iso-butane that mass fraction is 99.0% is passed through after purging, iso-butane flow is 18ml/
Min starts timing, collects 20min reaction products and carries out chromatogram ration analysis, the results are shown in Table 1.
1. catalyst activity test result of table
Catalyst stability is investigated：Catalyst A is placed in quartz tube reactor, the water that volume fraction is 20% is passed through and steams
Gas-air Mixture atmosphere is warming up to 870 DEG C of aging 2h, and dehydrogenation reaction is then carried out under reaction condition similar to the above, knot
Fruit is as shown in table 2.
2. catalyst activity correction data of table
From table 2 it can be seen that catalyst provided by the invention has excellent dehydrogenation activity and hydrothermal stability.
Claims (8)
1. a kind of catalyst for iso-butane fluid bed dehydrogenation, it is characterised in that：The catalyst is with Y2O3The SBA15- of modification
Al2O3Composite oxides are carrier, Cr2O3For active component, A is coagent, and B is structural promoter；Y in carrier2O3Quality
Score is 1% ~ 5wt%, and the mass fractions of SBA15 molecular sieves is 5wt% ~ 10wt%, remaining for aluminium oxide, in final catalyst
Cr2O3Mass fraction for 10% ~ 15%, the mass fraction of auxiliary agent A is 1% ~ 3%, and the mass fraction of auxiliary agent B is 0.5% ~ 1.5%, remaining
Under be carrier；
The auxiliary agent A is Ga2O3, auxiliary agent B SiO2。
2. catalyst according to claim 1, it is characterised in that：Y in carrier2O3Mass fraction for 2% ~ 3wt%, SBA15 points
The mass fraction of son sieve is remaining for aluminium oxide for 7% ~ 9%, Cr in final catalyst2O3Mass fraction for 12% ~ 14%, auxiliary agent
The mass fraction of A is 1.5% ~ 2%, and the mass fraction of auxiliary agent B is 0.75% ~ 1.25%, and remaining is carrier.
3. the preparation method of catalyst according to claim 1, it is characterised in that：The method for preparing catalyst includes following
Step：
（1）By hydrated alumina, hydration SBA15, containing Y2O3Compound be proportionally added into a certain amount of deionized water, stirring is equal
It is even, it then adds in binding agent and is beaten into suspension at a high speed；
（2）By step（1）In suspension be spray-dried to obtain microballoon, then by microballoon be placed in tube furnace and water steam
Carrier is fired under the mixed atmosphere of gas and air；
（3）Compound containing Cr, Ga is dissolved in deionized water and is made into certain density maceration extract, then by step（2）In
Carrier is soaked for a period of time in excessive above-mentioned maceration extract, separation maceration extract after the completion of dipping, dry；
(4) by step（3）In dried catalyst fluidized in fluidizer, then spray into certain volume on device top
Fluidizer temperature after spraying, is increased to one section of required calcination temperature and maintenance by the ethanol solution of silicon-containing compound
Time obtains final catalyst.
4. the preparation method of catalyst according to claim 3, it is characterised in that：The hydrated alumina be visit aluminium stone,
A kind of or their mixture in boehmite, containing Y2O3Compound for yttrium nitrate, binding agent is nitric acid, is added
Enter amount and hydrated alumina, hydration SBA15 are calculated as, containing Y with 65wt% concentrated nitric acids2O3Three kinds of solid gross masses of compound 3% ~ 7%.
5. the preparation method of catalyst according to claim 3, it is characterised in that：The solid content of the suspension for 25wt% ~
55wt%, dynamic viscosity are 40mPas ~ 80m Pas.
6. the preparation method of catalyst according to claim 3, it is characterised in that：The spray drying is done for press atomization
Dry, the microspherulite diameter of spray shaping is 20 ~ 200 μm, and the volume fraction of vapor is 10% ~ 30% in mixed atmosphere, calcination temperature
It it is 800 DEG C, roasting time 4h, the volume space velocity of mixed atmosphere is 500h-1~2000h-1。
7. the preparation method of catalyst according to claim 3, it is characterised in that the compound containing Cr is chromium acetate, three oxidations
One kind in chromium, ammonium dichromate, the compound containing Ga are gallium nitrate, and the content of chromium compound is 17wt% ~ 35wt% in maceration extract,
The content of gallium nitrate is 1wt% ~ 3wt%, and the dip time excessively impregnated is 10min, and drying temperature is 120 DEG C, and drying time is
30min。
8. the preparation method of catalyst according to claim 3, it is characterised in that：The siliceous compound is positive silicic acid
Ethyl ester, mass fraction in ethanol are 3% ~ 6%, the volume of the ethanol solution of penetrating be addition microballoon total suction 95% ~
105%, required calcination temperature is 750 DEG C, is held time as 4h.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3845514A1 (en) * | 2020-01-02 | 2021-07-07 | Indian Oil Corporation Limited | A catalyst composition for oxidative dehydrogenation of alkane |
| RU2776581C2 (en) * | 2020-01-02 | 2022-07-22 | Индиан Оил Корпорейшн Лимитед | Catalyst for oxidative alkane dehydration |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20210387167A1 (en) * | 2018-10-05 | 2021-12-16 | Sabic Global Technologies B.V. | Catalyst for paraffin dehydrogenation |
| CN112495422B (en) * | 2020-12-03 | 2022-02-22 | 昆明理工大学 | Method for preparing silicon-based chromium catalyst by in-situ roasting, product and application thereof |
| CN115957738B (en) * | 2023-01-03 | 2024-05-10 | 大连理工大学 | Preparation method and application of catalyst for preparing propylene by propane dehydrogenation |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4746643A (en) * | 1985-06-17 | 1988-05-24 | Snamprogetti S.P.A. | Method for the preparation of a catalyst for the dehydrogenation of C3 -C5 paraffins |
| CN103055953A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Low-carbon alkane dehydrogenation catalyst carrier and preparation method thereof |
| CN104275179A (en) * | 2013-07-09 | 2015-01-14 | 中国石油化工股份有限公司 | Light alkane dehydrogenation catalyst and preparation method |
| CN104607168A (en) * | 2015-01-05 | 2015-05-13 | 中国石油大学(华东) | Catalyst used for alkane catalytic dehydrogenation and preparation method thereof |
| CN105435773A (en) * | 2015-12-15 | 2016-03-30 | 复旦大学 | Catalyst for preparing isobutene through isobutane dehydrogenation and preparation method thereof |
-
2016
- 2016-05-23 CN CN201610343991.2A patent/CN105817258B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4746643A (en) * | 1985-06-17 | 1988-05-24 | Snamprogetti S.P.A. | Method for the preparation of a catalyst for the dehydrogenation of C3 -C5 paraffins |
| CN103055953A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Low-carbon alkane dehydrogenation catalyst carrier and preparation method thereof |
| CN104275179A (en) * | 2013-07-09 | 2015-01-14 | 中国石油化工股份有限公司 | Light alkane dehydrogenation catalyst and preparation method |
| CN104607168A (en) * | 2015-01-05 | 2015-05-13 | 中国石油大学(华东) | Catalyst used for alkane catalytic dehydrogenation and preparation method thereof |
| CN105435773A (en) * | 2015-12-15 | 2016-03-30 | 复旦大学 | Catalyst for preparing isobutene through isobutane dehydrogenation and preparation method thereof |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2803505C2 (en) * | 2018-10-05 | 2023-09-14 | Сабик Глоубл Текнолоджиз Б.В. | Paraffin dehydrogenation catalyst |
| EP3845514A1 (en) * | 2020-01-02 | 2021-07-07 | Indian Oil Corporation Limited | A catalyst composition for oxidative dehydrogenation of alkane |
| RU2776581C2 (en) * | 2020-01-02 | 2022-07-22 | Индиан Оил Корпорейшн Лимитед | Catalyst for oxidative alkane dehydration |
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