CN106582607B - The catalyst of dehydrogenation of isobutane - Google Patents
The catalyst of dehydrogenation of isobutane Download PDFInfo
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- CN106582607B CN106582607B CN201510673375.9A CN201510673375A CN106582607B CN 106582607 B CN106582607 B CN 106582607B CN 201510673375 A CN201510673375 A CN 201510673375A CN 106582607 B CN106582607 B CN 106582607B
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/20—Vanadium, niobium or tantalum
- B01J23/22—Vanadium
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- 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
- C07C5/3335—Catalytic processes with metals
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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
- C07C2521/04—Alumina
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- C07C2521/08—Silica
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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/06—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of zinc, cadmium or mercury
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of rare earths
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/20—Vanadium, niobium or tantalum
- C07C2523/22—Vanadium
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Abstract
The present invention relates to the catalyst of dehydrogenation of isobutane, preparation method and application, mainly solve the problems, such as that Catalyst Conversion is lower in the prior art.The present invention by using preparing isobutene through dehydrogenation of iso-butane catalyst, including carrier, active component and auxiliary agent, the catalyst is carrier at least one of SiO2, Al2O3 and ZnO, using vanadium as active component, with one or more of technical solutions for auxiliary agent of rare earth metal, it preferably solves the technical problem, can be used under carbon dioxide atmosphere in the industrial production of preparing isobutene through dehydrogenation of iso-butane.
Description
Technical field
The present invention relates to a kind of dehydrogenation of isobutane catalyst, preparation method and applications.
Background technique
Isobutene is a kind of very important industrial chemicals, and in Chemical Manufacture, the purposes of isobutene is very extensive, can be with
For synthesizing methyl tertbutyl ether (MTBE), ethyl tert-butyl ether (ETBE) (ETBE), butyl rubber, ABS resin etc..With isobutene
The production-scale expansion of downstream product, the demand of isobutene also constantly increase.The isobutene amount that conventional method obtains cannot
Meets the needs of market.In addition, the C4 resource in China is very rich, but compared with American-European countries China C4 resource utilization ratio
It is lower less than 40%, the only half or so of American-European countries, and be concentrated mainly on being used as using upper, most alkane for alkene
Fuel brings the great wasting of resources.The isobutene of the dehydrogenation of isobutane production high added value of relative low price can be solved
Certainly the shortage of isobutene can generate bigger economic benefit again.
Preparing isobutene through dehydrogenation of iso-butane is broadly divided into catalytic dehydrogenation, dioxygen oxidation dehydrogenation and three kinds of carbon dioxide atmosphere dehydrogenation
Method.Catalytic dehydrogenation of isobutane has realized industrialization at present, but the reaction is limited by thermodynamical equilibrium, and energy consumption is bigger.
The dehydrogenation of iso-butane dioxygen oxidation can bring deep oxidation, and product distribution is uncontrolled, lead to problems such as selectivity low.Carbon dioxide
Preparing isobutene through dehydrogenation of iso-butane combines the advantages of catalytic dehydrogenation and dioxygen oxidation dehydrogenation under atmosphere, is a kind of with potential competition
The new method of ability.Inverse water gas reaction occurs for the hydrogen that carbon dioxide can be generated with dehydrogenation, to break thermodynamical equilibrium
Limitation keeps dehydrogenation reaction mobile to product；Or directly with iso-butane oxidative dehydrogenation can occur for carbon dioxide.Above-mentioned two
The equilibrium conversion of iso-butane can be improved in kind mechanism.In addition, carbon dioxide is as main greenhouse gases, in reaction process
In be changed into more active and be industrially easier the carbon monoxide utilized, not only reduced greenhouse emissions but also taken full advantage of carbon money
Source has certain social value.
Carbon dioxide atmosphere preparing isobutene through dehydrogenation of iso-butane is taken seriously extensively, for example, Shimada et al. is using activity
The ferric oxide catalyst of charcoal load, the conversion ratio of iso-butane is about 23% under the conditions of reaction temperature is 600 DEG C, is selectively about
80%, and catalyst inactivation is fast, after reaction 3 hours iso-butane conversion ratio be down to 13% (Applied Catalysis A:
General, 1998 volume 168 page 243~250).Ogonowski seminar VMgO catalyst is 600 in reaction temperature
DEG C when, conversion ratio 13%, selectivity for 80% (Catalysis Communications, 2009 volume 11 the 132nd~136
Page).Chinese patent CN 102631914A is prepared for the vanadium pentoxide catalyst that mesoporous carbon is carrier, is 610 in reaction temperature
The conversion ratio of iso-butane is about 32% under the conditions of DEG C, selectivity about 91.4%.In terms of comprehensive, high conversion rate, alkene choosing are developed
Selecting property height and low-cost catalyst are still crucial.
Summary of the invention
The first technical problem to be solved by the present invention is the problem that catalyst iso-butane conversion ratio is lower in the prior art,
A kind of catalyst of new preparing isobutene through dehydrogenation of iso-butane is provided.The catalyst has the characteristics that higher olefins selectivity.
The second technical problem to be solved by the present invention is to provide the corresponding catalyst of one of one kind and solution technical problem
Preparation method.
The third technical problem to be solved by the present invention is to provide a kind of application of catalyst for solving one of technical problem.
One of to solve above-mentioned technical problem, The technical solution adopted by the invention is as follows: the catalyst of dehydrogenation of isobutane, packet
Carrier, active component and auxiliary agent are included, the catalyst is carrier at least one of SiO2, Al2O3 and ZnO, is with vanadium
Active component, with the one or more of rare earth metal for auxiliary agent.
In above-mentioned technical proposal, the rare earth metal is not particularly limited, such as, but not limited to heavy rare earth metal element
Middle Y, Yb, Ho, Er etc..But it is preferred that the rare earth includes Y and Yb simultaneously, there is collaboration both in terms of isobutene conversion at this time
Effect.
In above-mentioned technical proposal, the mass percentage of vanadium is preferably 0.5~30%, more preferable 2~15% in terms of V2O5.
In above-mentioned technical proposal, the mass percentage of auxiliary agent in terms of the trivalent of rare earth preferably 0.2~
4.5%.
To solve above-mentioned technical problem two, The technical solution adopted by the invention is as follows: the skill of one of above-mentioned technical problem
The preparation method of catalyst described in art scheme, comprising the following steps:
1) aequum carrier is successively mixed with the solution containing vanadium and the solution containing auxiliary agent, or by aequum carrier and simultaneously
Solution mixing containing vanadium and containing auxiliary agent；
2) roasting obtains the catalyst.
In above-mentioned technical proposal, the solution preferably uses the solvent of water, one skilled in the art will appreciate that according to vanadium is contained
Compound and property containing auxiliary compound adjust pH to form solution so that above compound is dissolved in the water with acid or alkali.
Carrier can successively be mixed with the solution containing vanadium and the solution containing auxiliary agent, sequencing there is no limit, or with it is same
When containing vanadium and containing auxiliary agent mixed solution mixing.
When using carrier with solution hybrid mode containing vanadium and containing auxiliary agent, the preparation method of mixed solution be can be but unlimited
In:
A, the compound of the desired amount of vanadium is dissolved in the water and is dissolved in beaker with suitable oxalic acid aqueous solution, obtained
To the aqueous solution containing vanadium；
B, the desired amount of rare earth compound is added in the aqueous solution containing vanadium in step a, stirring and dissolving is obtained containing vanadium and auxiliary agent
Aqueous solution；
In above-mentioned technical proposal, the compound of vanadium is not particularly limited, such as, but not limited to ammonium metavanadate, vanadic sulfate and
One kind of vanadyl oxalate, the rare earth compound is it is not also specifically limited, such as, but not limited to nitrate, chlorate etc..
In above-mentioned technical proposal, maturing temperature is preferably 550~750 DEG C, and more preferable 600~700 DEG C.
In above-mentioned technical proposal, calcining time is preferably 2~10 hours, and more preferably 4~6 hours.
In above-mentioned technical proposal, one skilled in the art will appreciate that being preferably that there is drying between step 1) and step 2)
The step of.
In above-mentioned technical proposal, dry temperature is preferably 85~145 DEG C.
In above-mentioned technical proposal, drying time is preferably 24~36 hours.
To solve above-mentioned technical problem three, The technical solution adopted by the invention is as follows: above-mentioned catalyst is applied to dioxy
Change under carbon atmosphere in the reaction of preparing isobutene through dehydrogenation of iso-butane.
In above-mentioned technical proposal, the molar ratio of preferably carbon dioxide and iso-butane is 1~10.
In above-mentioned technical proposal, the temperature of reaction is preferably 550~650 DEG C.
In above-mentioned technical proposal, the mass space velocity of iso-butane 0.2~2 hour -1.
Iso-butane conversion ratio, selective isobutene calculate as follows:
For the present invention under experiment condition of the invention, the conversion ratio of iso-butane keeps higher while also with higher different
Butylene selectivity, achieves preferable technical effect.
The present invention will be further described below by way of examples:
Specific embodiment
[embodiment 1]
1, catalyst preparation
The ammonium metavanadate that will be equivalent to 10 grams of V2O5 and the yttrium nitrate for being equivalent to 2 grams of Y2O3 are dissolved in 25 milliliter 0.25 and rub
You/liter oxalic acid aqueous solution in, mix with 88 grams of SiO2 carriers, at room temperature stand 4 hours, then at 120 DEG C dry 28 hours,
Roast catalyst needed for being made 6 hours, in 600 DEG C of muffle furnaces finally for convenient for comparing, the composition of catalyst is listed in table 1.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 6.0,
Reaction temperature is 580 DEG C, and the mass space velocity of iso-butane is 0.5 hour -1, and reaction pressure is normal pressure.
For convenient for comparing, catalyst activity evaluation the results are shown in Table 2.
[comparative example 1]
1, catalyst preparation
The ammonium metavanadate that will be equivalent to 12 grams of V2O5 is dissolved in the oxalic acid aqueous solution of 25 milliliter of 0.25 mol/L, with 88
The mixing of gram SiO2 carrier, stands 4 hours at room temperature, 28 hours dry then at 120 DEG C, finally roasts 6 in 600 DEG C of muffle furnaces
Catalyst needed for hour is made, for convenient for comparing, the composition of catalyst is listed in table 1.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 6.0,
Reaction temperature is 580 DEG C, and the mass space velocity of iso-butane is 0.5 hour -1, and reaction pressure is normal pressure.
For convenient for comparing, catalyst activity evaluation the results are shown in Table 2.
[comparative example 2]
1, catalyst preparation
The yttrium nitrate that will be equivalent to 12 grams of Y2O3 is dissolved in the oxalic acid aqueous solution of 25 milliliter of 0.25 mol/L, with 88 grams
The mixing of SiO2 carrier, stands 4 hours at room temperature, 28 hours dry then at 120 DEG C, and finally roasting 6 is small in 600 DEG C of muffle furnaces
When be made needed for catalyst, for convenient for comparing, the composition of catalyst is listed in table 1.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 6.0,
Reaction temperature is 580 DEG C, and the mass space velocity of iso-butane is 0.5 hour -1, and reaction pressure is normal pressure.
For convenient for comparing, catalyst activity evaluation the results are shown in Table 2.
[embodiment 2]
1, catalyst preparation
The ammonium metavanadate that will be equivalent to 10 grams of V2O5 and the ytterbium nitrate for being equivalent to 2 grams of Yb2O3 are dissolved in 25 milliliter 0.25 and rub
You/liter oxalic acid aqueous solution in, mix with 88 grams of SiO2 carriers, at room temperature stand 4 hours, then at 120 DEG C dry 28 hours,
Roast catalyst needed for being made 6 hours, in 600 DEG C of muffle furnaces finally for convenient for comparing, the composition of catalyst is listed in table 1.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 6.0,
Reaction temperature is 580 DEG C, and the mass space velocity of iso-butane is 0.5 hour -1, and reaction pressure is normal pressure.
For convenient for comparing, catalyst activity evaluation the results are shown in Table 2.
[embodiment 3]
1, catalyst preparation
It will be equivalent to the ammonium metavanadate of 10 grams of V2O5, be equivalent to the yttrium nitrate of 1 gram of Y2O3 and be equivalent to the nitre of 1 gram of Yb2O3
Sour ytterbium is dissolved in the oxalic acid aqueous solution of 25 milliliter of 0.25 mol/L, is mixed with 88 grams of SiO2 carriers, and it is small to stand 4 at room temperature
When, it is 28 hours dry then at 120 DEG C, finally roast in 600 DEG C of muffle furnaces and required catalyst is made within 6 hours, for convenient for comparing,
The composition of catalyst is listed in table 1.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 6.0,
Reaction temperature is 580 DEG C, and the mass space velocity of iso-butane is 0.5 hour -1, and reaction pressure is normal pressure.
For convenient for comparing, catalyst activity evaluation the results are shown in Table 2.
The result shows that Y and Yb has synergistic effect in terms of improving catalyst activity and selectivity.
[embodiment 4]
1, catalyst preparation
The ammonium metavanadate that will be equivalent to 10 grams of V2O5 and the holmium nitrate for being equivalent to 2 grams of Ho2O3 are dissolved in 25 milliliter 0.25 and rub
You/liter oxalic acid aqueous solution in, mix with 8 grams of SiO2 carriers, at room temperature stand 4 hours, then at 120 DEG C dry 28 hours,
Roast catalyst needed for being made 6 hours, in 600 DEG C of muffle furnaces finally for convenient for comparing, the composition of catalyst is listed in table 1.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 6.0,
Reaction temperature is 580 DEG C, and the mass space velocity of iso-butane is 0.5 hour -1, and reaction pressure is normal pressure.
For convenient for comparing, catalyst activity evaluation the results are shown in Table 2.
[embodiment 5]
1, catalyst preparation
The ammonium metavanadate that will be equivalent to 10 grams of V2O5 and the erbium nitrate for being equivalent to 2 grams of Er 2O3 are dissolved in 25 milliliter 0.25 and rub
You/liter oxalic acid aqueous solution in, mix with 88 grams of SiO2 carriers, at room temperature stand 4 hours, then at 100 DEG C dry 24 hours,
Roast catalyst needed for being made 4 hours, in 600 DEG C of muffle furnaces finally for convenient for comparing, the composition of catalyst is listed in table 1.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 5.0,
Reaction temperature is 590 DEG C, and the mass space velocity of iso-butane is 1.0 hours -1, and reaction pressure is normal pressure.
For convenient for comparing, catalyst activity evaluation the results are shown in Table 2.
[embodiment 6]
1, catalyst preparation
The ammonium metavanadate that will be equivalent to 30 grams of V2O5 and the yttrium nitrate for being equivalent to 0.5 gram of Y2O3 are dissolved in 45 milliliter 0.25 and rub
You/liter oxalic acid aqueous solution in, mix with 69.5 grams of Al2O3 carriers, stands 4 hours at room temperature, dried then at 80 DEG C 36 small
When, finally roast catalyst needed for being made in 800 DEG C of muffle furnaces 2 hours.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 1.0,
Reaction temperature is 650 DEG C, and the mass space velocity of iso-butane is 0.5 hour -1, and reaction pressure is normal pressure.
Reaction result are as follows: iso-butane conversion ratio is 35.9%, selective isobutene 87.2%.
[embodiment 7]
1, catalyst preparation
The ammonium metavanadate that will be equivalent to 1 gram of V2O5 and the yttrium nitrate for being equivalent to 4.5 grams of Y2O3 are dissolved in 25 milliliter 0.25 and rub
You/liter oxalic acid aqueous solution in, mix with 94.5 grams of ZnO carriers, stands 4 hours at room temperature, dried then at 150 DEG C 24 small
When, finally roast catalyst needed for being made in 550 DEG C of muffle furnaces 10 hours.
2, evaluating catalyst
Catalyst obtained carries out activity rating in fixed bed reactors according to the above method, and process is as follows:
The stainless steel tube that the internal diameter of reactor is 8 millimeters, it is 400 millimeters long.Carbon dioxide and iso-butane molar ratio are 10.0,
Reaction temperature is 560 DEG C, and the mass space velocity of iso-butane is 0.5 hour -1, and reaction pressure is normal pressure.
Reaction result are as follows: iso-butane conversion ratio is 18.5%, selective isobutene 92.6%.
Table 1
| V2O5 | Y2O3 | Yb2O3 | Ho2O3 | Er2O3 | Carrier | |
| Embodiment 1 | 10 | 2 | - | - | - | 88 |
| Comparative example 1 | 12 | - | - | - | - | 88 |
| Comparative example 2 | - | 12 | - | - | - | 88 |
| Embodiment 2 | 10 | - | 2 | - | - | 88 |
| Embodiment 3 | 10 | 1 | 1 | - | - | 88 |
| Embodiment 4 | 7 | - | - | 2 | - | 88 |
| Embodiment 5 | 7 | - | - | - | 2 | 88 |
Note: catalyst composition is indicated in table 1 with weight percentage.
Table 2
| Iso-butane conversion ratio/% | Selective isobutene/% | |
| Embodiment 1 | 38.6 | 91.7 |
| Comparative example 1 | 19.5 | 89.1 |
| Comparative example 2 | 10.8 | 94.9 |
| Embodiment 2 | 34.2 | 92.3 |
| Embodiment 3 | 45.7 | 91.2 |
| Embodiment 4 | 30.7 | 92.1 |
| Embodiment 5 | 31.4 | 91.9 |
Claims (8)
1. the catalyst of dehydrogenation of isobutane, including carrier, active component and auxiliary agent, it is characterised in that: the catalyst with
SiO2、Al2O3It is carrier at least one of ZnO, using vanadium as active component, using rare earth metal yttrium and ytterbium as auxiliary agent, wherein vanadium
Mass percentage with V2O5It is calculated as 0.5~30%, the mass percentage of auxiliary agent is calculated as 0.2 with the trivalent of rare earth
~4.0%.
2. the preparation method of catalyst described in claim 1, comprising the following steps:
1) aequum carrier is successively mixed with the solution containing vanadium and the solution containing auxiliary agent, or by aequum carrier and simultaneously containing vanadium
With the solution mixing containing auxiliary agent；
2) roasting obtains the catalyst.
3. preparation method according to claim 2, it is characterised in that maturing temperature is 550~750 DEG C.
4. preparation method according to claim 2, it is characterised in that calcining time is 2~10 hours.
5. preparation method according to claim 2, it is characterised in that have dry step between step 1) and step 2).
6. preparation method according to claim 5, it is characterised in that dry temperature is 85~145 DEG C.
7. preparation method according to claim 5, it is characterised in that drying time is 24~36 hours.
8. catalyst described in claim 1 is applied under carbon dioxide atmosphere in the reaction of preparing isobutene through dehydrogenation of iso-butane.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101165031A (en) * | 2006-10-16 | 2008-04-23 | 罗门哈斯公司 | Integrated catalytic process for converting alkanes to alkenes and catalysts useful for same |
| CN102614864A (en) * | 2012-03-01 | 2012-08-01 | 河南科技大学 | Iso-butane dehydrogenation catalyst and preparation method thereof |
| CN103933964A (en) * | 2014-04-17 | 2014-07-23 | 陕西师范大学 | Preparation method of vanadium-base catalyst for ethylbenzene dehydrogenation to prepare styrene by virtue of oxidation of CO2 |
| CN104549218A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalyst for preparing olefin from low carbon alkane through dehydrogenation and preparation method of catalyst |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101165031A (en) * | 2006-10-16 | 2008-04-23 | 罗门哈斯公司 | Integrated catalytic process for converting alkanes to alkenes and catalysts useful for same |
| CN102614864A (en) * | 2012-03-01 | 2012-08-01 | 河南科技大学 | Iso-butane dehydrogenation catalyst and preparation method thereof |
| CN104549218A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalyst for preparing olefin from low carbon alkane through dehydrogenation and preparation method of catalyst |
| CN103933964A (en) * | 2014-04-17 | 2014-07-23 | 陕西师范大学 | Preparation method of vanadium-base catalyst for ethylbenzene dehydrogenation to prepare styrene by virtue of oxidation of CO2 |
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