CN103785388A - Propane dehydrogenation catalyst containing V and preparation method thereof - Google Patents
Propane dehydrogenation catalyst containing V and preparation method thereof Download PDFInfo
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- CN103785388A CN103785388A CN201210427677.4A CN201210427677A CN103785388A CN 103785388 A CN103785388 A CN 103785388A CN 201210427677 A CN201210427677 A CN 201210427677A CN 103785388 A CN103785388 A CN 103785388A
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Abstract
The invention discloses a propane dehydrogenation catalyst, which employs silica as a carrier, Pt as a dehydrogenation active component, and Sn and V as auxiliary agents. The catalyst comprises, by weight, 0.1-2% preferably 0.2-0.8%, of dehydrogenation active component, and comprises, calculated by the weight of the carrier, 0.1-10% preferably 1-5%, of the auxiliary agent Sn, and 0.1-10% preferably 1-5% of the auxiliary agent V. A preparation method of the propane dehydrogenation catalyst is by loading auxiliary agents Sn and V and the active component Pt by using silica gel as a carrier through an impregnation method. The method can substantially increase the activity stability and olefin selectivity of the catalyst.
Description
Technical field
The present invention relates to a kind of V propane dehydrogenation catalyst and preparation method thereof that contains, particularly a kind of have high olefin optionally containing V propane dehydrogenation catalyst and preparation method thereof take silica as carrier.
Background technology
Since entering the new century, world's petrochemical material and petroleum chemicals demand will sustainable growths, to continue to increase as the demand of petrochemical industry basic material propylene, and conventional steam cracking and FCC technology production capacity can not meet the propylene demand of rapid growth, its market occurred global in short supply.And day by day deficient along with petroleum resources, the production of propylene has been that raw material changes to the diversified technology path of raw material sources from simple dependence oil, the particularly technology path take low-carbon alkanes as waste alkene.In recent years, dehydrogenating propane was produced the technology of propylene and had been obtained large development, and it is very fast that particularly the technology of dehydrogenating propane (PDH) propylene processed had the regional development of resources advantage in recent years in the Middle East etc., becomes the third-largest propylene production.
Propane catalytic dehydrogenating reaction is subject to thermodynamics equilibrium limit, must under the harsh conditions of high temperature, low pressure, carry out.Too high reaction temperature, makes Deposition During Propane Pyrolysis reaction and degree of depth dehydrogenation aggravation, selectively declines; Accelerate catalyst surface carbon deposit simultaneously, make rapid catalyst deactivation.Due to the shortening of catalyst life under lower conversion of propane and harsh reaction condition, PDH method is restricted in the time of commercial Application.Therefore the catalyst for preparing propylene with propane dehydrogenation that, exploitation has high activity, high selectivity and a high stability becomes the key of this technology.CN1201715 patent discloses the Pt-Sn-K/Al for low-carbon alkanes (C1 ~ C5) dehydrogenation
2o
3the preparation method of catalyst.CN1579616 patent report with the macropore of researching and developing voluntarily, low heap ratio, there is the γ-Al of double-pore structure
2o
3bead is carrier, for the catalyst of linear alkanes dehydrogenation, by the modulation of catalyst, can improve the reactivity worth of dehydrogenating low-carbon alkane.USP4,914,075, USP4,353,815, USP4,420,649, USP4,506,032, USP4,595,673, EP562906, EP98622 etc. have reported for propane and other dehydrogenating low-carbon alkane Pt catalyst based, have high alkane conversion and olefine selective.Although these catalyst can reach higher alkane conversion and olefine selective under some reaction condition, due to the own character of alumina support, all can not obtain higher olefine selective.And because reaction is subject to thermodynamics control, conversion ratio is not generally higher than 40%, and raw material need recycle, now, high selectivity of product can be brought obvious economic benefit at product yield and separation process.The existing a large amount of reports of dehydrogenating propane research of the Pt-Sn class catalyst that is carrier about aluminium oxide both at home and abroad, focus mostly at aspects such as catalyst preparation, alkali metal allotments.
At present, the existing a large amount of reports of the dehydrogenating propane research of the Pt-Sn class catalyst that is carrier about aluminium oxide both at home and abroad, focus mostly at aspects such as catalyst preparation, alkali metal allotments.But the Pt-Sn class catalyst take silica as carrier but rarely has report, this is mainly because the inactive surfaces of silica makes Sn easily be reduced to zeroth order, forms alloy with Pt, has reduced the selective of the activity stability of catalyst and product.If can solve the problem that the Pt-Sn class catalyst take silica as carrier exists, and can suppress the advantage of cracking reaction in conjunction with the low acidity of silica supports itself, the Pt-Sn class catalyst take silica as carrier must have broad application prospects.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of preparation method of the alkane dehydrogenating catalyst take silica as carrier.The method can significantly improve the selective of the activity stability of catalyst and alkene.
A kind of propane dehydrogenation catalyst, take silica as carrier, take Pt as dehydrogenation active component, take Sn and V as auxiliary agent, in catalyst, dehydrogenation active component weight content is 0.1% ~ 2%, be preferably 0.2% ~ 0.8%, by vehicle weight, the content of auxiliary agent Sn is 0.1% ~ 10%, is preferably 1% ~ 5%, the content of auxiliary agent V is 0.1% ~ 10%, is preferably 1% ~ 5%.In catalyst of the present invention, preferred promoter V is 2 with Sn atomicity ratio.
A preparation method for propane dehydrogenation catalyst, take silica gel as carrier, adopts infusion process load auxiliary agent Sn, V and active component Pt, preferably load auxiliary agent Sn, V and active component Pt successively.
In propane dehydrogenation catalyst preparation method of the present invention, silica supports can adopt existing silica gel product, as macro porous silica gel, Kiselgel A or Type B silica gel etc., and the method preparation that also can know by professional and technical personnel in the field.Silica supports can be the suitable shape such as spherical, bar shaped, microballoon or abnormity, and particle equivalent diameter is generally 10 μ m-5000 μ m, and preferred particle size is 100 μ m-2000 μ m.
In propane dehydrogenation catalyst preparation method of the present invention, auxiliary agent Sn is incorporated in catalyst with dipping method.Sn predecessor can be cationic tin salt, as nitric acid tin, butter of tin, tin acetate etc., can be also stannic acid metalloid salt, as sodium stannate, potassium stannate etc., is preferably butter of tin.The dipping process of auxiliary agent Sn can adopt method well known to those skilled in the art.As adopt following process: first adopt the solution impregnation silica-gel carrier containing auxiliary agent Sn, dip time 1h ~ 72h, preferably 2h ~ 24h.Dry after dipping tin, baking temperature is 60 ℃ ~ 150 ℃, and be 1h ~ 24h drying time, is preferably dry 4h ~ 8h at 80 ℃ ~ 120 ℃.Sintering temperature is 400 ℃ ~ 800 ℃, and roasting time 2h ~ 24h is preferably roasting 4h ~ 8h at 500 ℃ ~ 700 ℃.
In propane dehydrogenation catalyst preparation method of the present invention, auxiliary agent V is incorporated in catalyst with dipping method.The predecessor of auxiliary agent is for containing this promoter metal salt.The dipping process of auxiliary agent can adopt method well known to those skilled in the art.As adopt following process: first adopt the solution impregnation silica-gel carrier containing auxiliary agent, dip time 1h ~ 72h, preferably 2h ~ 24h.Then dry, roasting, baking temperature is 60 ℃ ~ 150 ℃, be 1h ~ 24h drying time, is preferably dry 4h ~ 8h at 80 ℃ ~ 120 ℃.Sintering temperature is 400 ℃ ~ 800 ℃, and roasting time 2h ~ 24h is preferably roasting 4h ~ 8h at 500 ℃ ~ 700 ℃.
In propane dehydrogenation catalyst preparation method of the present invention, the introducing method of active component Pt is method well known to those skilled in the art.The predecessor of Pt can be for chloroplatinic acid, also can be the organic complex salt containing Pt.Maceration extract can be the aqueous solution, can be also the organic solution containing Pt.As adopt following process: first adopt the solution impregnation modified silica gel carrier containing Pt, dip time 1h ~ 72h, preferably 2h ~ 24h.After dipping tin, comprise dry and calcination steps, baking temperature is 60 ℃ ~ 150 ℃, and be 1h ~ 24h drying time, is preferably dry 4h ~ 8h at 80 ℃ ~ 120 ℃.Sintering temperature is 500 ℃ ~ 900 ℃, and roasting time 2h-24h is preferably roasting 4h ~ 8h at 600 ℃ ~ 800 ℃.
In propane dehydrogenation catalyst preparation method of the present invention, the catalyst after above-mentioned load active component Pt needs steam dechlorination.Steam dechlorination, for to process 1h ~ 20h at 400 ℃ ~ 800 ℃, is preferably at 500 ℃ ~ 700 ℃ and processes 2h ~ 10h, and the atmosphere of dechlorination is the nitrogen of molar content 5% ~ 50% steam, is preferably the nitrogen of molar content 10% ~ 30% steam.After dechlorination, the content of chlorine element is less than 0.15wt%.
Compared with prior art, the propane dehydrogenation catalyst tool that the inventive method obtains has the following advantages:
1, high oxide and its reduction-state standard electrode EMF of the second auxiliary agent V adding are less than Sn
2+the standard electrode EMF of/Sn, and hydrogenolysis is a little less than ability, is all difficult to reduction in thermodynamics, dynamics, once but Sn is reduced, V
2o
5distinctive active variable valency state property matter makes it very easily generate electron hole, thereby has had excellent electronics transferring power character, thereby obtains Sn element electronics, keeps Sn
2+exist;
2, the specific area that silica supports is larger and the surface nature of inertia, being conducive to active metal disperses, suppress the generation of the side reactions such as cracking, carbon distribution, can effectively improve olefine selective and catalyst stability, while being beneficial to catalyst regeneration, active metal disperses again simultaneously;
3, method for preparing catalyst is simple, and technology maturation is conducive to the industrial production of catalyst.
The specific embodiment
Enforcement below by dehydrogenating propane is described further technology of the present invention.
Example 1
Take commercially available silica gel (pore volume 0.71cm3/g, specific area 474m
2/ g, following examples are all used this silica gel) 30g, dripping deionized water to just moistening, the volume that consumes water is 48mL.Account for silica supports 3wt% by Sn content, take containing the butter of tin of 0.9gSn and be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned carrier silica gel and flood, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 500 ℃.Take cerous nitrate by above-mentioned Sn molal quantity equivalent, be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned sample and flood, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 500 ℃.By final catalyst Pt content 0.6wt%, take containing the chloroplatinic acid of Pt0.18g and be dissolved in deionized water, be settled to 48mL, be added in the sample after above-mentioned dipping Sn, Ce, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 600 ℃.Above-mentioned steps gained sample, at 600 ℃, is processed 6h containing under the nitrogen atmosphere of 20% steam, and gained catalyst is designated as C-1.
Appreciation condition: catalyst quality 3.0g, hydrogen atmosphere reduction, the mass space velocity of propane is 3h
-1, reaction pressure 0.1MPa, reaction temperature is 630 ℃.Following examples gained evaluating catalyst condition is identical, and evaluation result is in table 1.
Example 2
Take commercially available silica gel 30g, drip deionized water to just moistening, the volume that consumes water is 48mL.Account for silica supports 3wt% by Sn content, take containing the butter of tin of 0.9gSn and be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned carrier silica gel and flood, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 500 ℃.Take above-mentioned Sn molal quantity as radix, take ammonium metavanadate by Sn:V=1:2, be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned sample and flood, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 500 ℃.By final catalyst Pt content 0.6wt%, take containing the chloroplatinic acid of Pt0.18g and be dissolved in deionized water, be settled to 48mL, be added in the sample after above-mentioned dipping Sn, V, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 600 ℃.Above-mentioned steps gained sample, at 600 ℃, is processed 6h containing under the nitrogen atmosphere of 20% steam, and gained catalyst is designated as C-2.
Example 3
Take commercially available silica gel 30g, drip deionized water to just moistening, the volume that consumes water is 48mL.Account for silica supports 1wt% by Sn content, take containing the butter of tin of 0.3gSn and be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned carrier silica gel and flood, aging 3 hours, 100 ℃ were dried 4 hours, roasting 4 hours in 600 ℃.Take above-mentioned Sn molal quantity as radix, take ammonium metavanadate by Sn:V=1:2, be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned sample and flood, aging 3 hours, 100 ℃ were dried 8 hours, roasting 4 hours in 600 ℃.By final catalyst Pt content 0.4wt%, take containing the chloroplatinic acid of Pt0.12g and be dissolved in deionized water, be settled to 48mL, be added in the sample after above-mentioned dipping Sn, V, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 600 ℃.Above-mentioned steps gained sample, at 600 ℃, is processed 6h containing under the nitrogen atmosphere of 20% steam, and gained catalyst is designated as C-3.
Example 4
Take commercially available silica gel 30g, drip deionized water to just moistening, the volume that consumes water is 48mL.Account for silica supports 5wt% by Sn content, take containing the butter of tin of 1.5gSn and be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned carrier silica gel and flood, aging 3 hours, 120 ℃ were dried 4 hours, roasting 4 hours in 600 ℃.Take above-mentioned Sn molal quantity as radix, take ammonium metavanadate by Sn:V=1:2, be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned sample and flood, aging 3 hours, 100 ℃ were dried 8 hours, roasting 4 hours in 600 ℃.By final catalyst Pt content 0.8wt%, take containing the chloroplatinic acid of Pt0.24g and be dissolved in deionized water, be settled to 48mL, be added in the sample after above-mentioned dipping Sn, V, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 600 ℃.Above-mentioned steps gained sample, at 600 ℃, is processed 6h containing under the nitrogen atmosphere of 30% steam, and gained catalyst is designated as C-4.
Example 5
Take commercially available silica gel 30g, drip deionized water to just moistening, the volume that consumes water is 48mL.Account for silica supports 3wt% by Sn content, take containing the butter of tin of 0.9gSn and be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned carrier silica gel and flood, aging 3 hours, 120 ℃ were dried 4 hours, roasting 4 hours in 600 ℃.Take above-mentioned Sn molal quantity as radix, take ammonium metavanadate by Sn:V=1:2, be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned sample and flood, aging 3 hours, 100 ℃ were dried 8 hours, roasting 4 hours in 600 ℃.By final catalyst Pt content 0.2wt%, take containing the chloroplatinic acid of Pt0.24g and be dissolved in deionized water, be settled to 48mL, be added in the sample after above-mentioned dipping Sn, V, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 700 ℃.Above-mentioned steps gained sample is processed 6h at 600 ℃ containing under the nitrogen atmosphere of 30% steam, and gained catalyst is designated as C-5.
Example 6
Take commercially available silica gel 30g, drip deionized water to just moistening, the volume that consumes water is 48mL.Account for silica supports 3wt% by Sn content, take containing the butter of tin of 0.9gSn and be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned carrier silica gel and flood, aging 3 hours, 100 ℃ were dried 8 hours, roasting 4 hours in 500 ℃.Take cerous nitrate by above-mentioned Sn molal quantity equivalent, be dissolved in deionized water, be settled to 48mL.Be added in above-mentioned sample and flood, aging 3 hours, 100 ℃ were dried 6 hours, roasting 4 hours in 600 ℃.By final catalyst Pt content 0.4wt%, take containing the chloroplatinic acid of Pt0.12g and be dissolved in deionized water, be settled to 48mL, be added in the sample after above-mentioned dipping Sn, Ce, aging 3 hours, 80 ℃ were dried 8 hours, roasting 4 hours in 600 ℃.Above-mentioned steps gained sample, at 600 ℃, is processed 6h containing under the nitrogen atmosphere of 20% steam, and gained catalyst is designated as C-6.
The reactivity worth of table 1 catalyst
| Catalyst | Conversion of propane, % | Propylene Selectivity, % |
| C-1 | 31.4 | 99.1 |
| C-2 | 32.8 | 97.6 |
| C-3 | 31.7 | 97.2 |
| C-4 | 33.5 | 95.9 |
| C-5 | 29.2 | 97.9 |
| C-6 | 32.7 | 98.7 |
Claims (10)
1. a propane dehydrogenation catalyst, it is characterized in that: this catalyst is take silica as carrier, take Pt as dehydrogenation active component, take Sn and V as auxiliary agent, in catalyst, dehydrogenation active component weight content is 0.1% ~ 2%, by vehicle weight, the content of auxiliary agent Sn is 0.1% ~ 10%, and the content of auxiliary agent V is 0.1% ~ 10%.
2. catalyst according to claim 1, is characterized in that: dehydrogenation active component content is 0.2% ~ 0.8%, and the content of auxiliary agent Sn is 1% ~ 5%, and the content of auxiliary agent V is 1% ~ 5%.
3. the preparation method of catalyst described in claim 1, is characterized in that: take silica gel as carrier, adopt infusion process load auxiliary agent Sn, V and active component Pt.
4. method according to claim 3, is characterized in that: silica-gel carrier is spherical, bar shaped, microballoon or abnormity, and particle equivalent diameter is 10 μ m-5000 μ m.
5. method according to claim 3, is characterized in that: the first auxiliary agent Sn is incorporated in catalyst with dipping method, and Sn predecessor is cation pink salt or stannic acid metalloid salt.
6. according to the method described in claim 3 or 6, it is characterized in that: the dipping of auxiliary agent Sn adopts following process: first adopt the solution impregnation silica-gel carrier containing auxiliary agent Sn, dip time 1h ~ 72h; After dipping tin, comprise dry and roasting, baking temperature is 60 ℃ ~ 150 ℃, and be 1h ~ 24h drying time; Sintering temperature is 400 ℃ ~ 800 ℃, roasting time 2h ~ 24h.
7. method according to claim 3, it is characterized in that: auxiliary agent V dipping adopts following process: first adopt the solution impregnation silica-gel carrier containing auxiliary agent, dip time 1h ~ 72h, then dry, roasting, baking temperature is 60 ℃ ~ 150 ℃, be 1h ~ 24h drying time, and sintering temperature is 400 ℃ ~ 800 ℃, roasting time 2h ~ 24h.
8. method according to claim 3, it is characterized in that: the dipping of active component Pt adopts following process: first adopt the solution impregnation modified silica gel carrier containing Pt, dip time 1h ~ 72h, after dipping tin, be dried and roasting, baking temperature is 60 ℃ ~ 150 ℃, be 1h ~ 24h drying time, and sintering temperature is 500 ℃ ~ 900 ℃, roasting time 2h ~ 24h.
9. method according to claim 3, it is characterized in that: the catalyst after load active component Pt need to carry out steam dechlorination processing, steam dechlorination for to process 1h ~ 20h at 400 ℃ ~ 800 ℃, and the atmosphere of dechlorination is the nitrogen of molar content 5% ~ 50% steam.
10. according to the method described in claim 3 or 9, it is characterized in that: after dechlorination, the content of chlorine element is less than 0.15wt%.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103990466A (en) * | 2014-05-20 | 2014-08-20 | 浙江大学 | V-Fe-series catalyst capable of carrying out catalytic oxidation on propane for preparing propylene and carbon monoxide and preparation method of V-Fe-series catalyst |
| CN106807405A (en) * | 2015-11-30 | 2017-06-09 | 中国科学院大连化学物理研究所 | The preparation method and its catalyst of a kind of catalyst for preparing propylene by dehydrogenating propane |
| US10358398B2 (en) | 2016-05-17 | 2019-07-23 | Iowa State University Research Foundation, Inc. | Dehydrogenation of propane using a metal-containing catalyst on a support |
| CN110496617A (en) * | 2018-05-17 | 2019-11-26 | 中国石油化工股份有限公司 | The method of dehydrogenation of isobutane catalyst and preparation method thereof and preparing isobutene through dehydrogenation of iso-butane |
| CN110496636A (en) * | 2018-05-17 | 2019-11-26 | 中国石油化工股份有限公司 | The method of dehydrogenation of isobutane catalyst and preparation method thereof and preparing isobutene through dehydrogenation of iso-butane |
| CN110496637A (en) * | 2018-05-17 | 2019-11-26 | 中国石油化工股份有限公司 | The method of dehydrogenation of isobutane catalyst and preparation method thereof and preparing isobutene through dehydrogenation of iso-butane |
| CN112138657A (en) * | 2019-06-27 | 2020-12-29 | 中国石油化工股份有限公司 | Propane dehydrogenation catalyst with spherical silica gel particle as carrier and preparation method and application thereof |
| WO2024008171A1 (en) * | 2022-07-07 | 2024-01-11 | 润和科华催化剂(上海)有限公司 | Transition-metal-based dehydrogenation catalyst for low-carbon alkane, and preparation method therefor and use thereof |
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| CN103990466A (en) * | 2014-05-20 | 2014-08-20 | 浙江大学 | V-Fe-series catalyst capable of carrying out catalytic oxidation on propane for preparing propylene and carbon monoxide and preparation method of V-Fe-series catalyst |
| CN103990466B (en) * | 2014-05-20 | 2016-08-17 | 浙江大学 | Catalytic oxidation of propane V-Fe catalyst series preparing propylene and carbon monoxide and preparation method thereof |
| CN106807405A (en) * | 2015-11-30 | 2017-06-09 | 中国科学院大连化学物理研究所 | The preparation method and its catalyst of a kind of catalyst for preparing propylene by dehydrogenating propane |
| CN106807405B (en) * | 2015-11-30 | 2019-02-19 | 中国科学院大连化学物理研究所 | A kind of preparation method and its catalyst of the catalyst for preparing propylene by dehydrogenating propane |
| US10358398B2 (en) | 2016-05-17 | 2019-07-23 | Iowa State University Research Foundation, Inc. | Dehydrogenation of propane using a metal-containing catalyst on a support |
| CN110496636A (en) * | 2018-05-17 | 2019-11-26 | 中国石油化工股份有限公司 | The method of dehydrogenation of isobutane catalyst and preparation method thereof and preparing isobutene through dehydrogenation of iso-butane |
| CN110496617A (en) * | 2018-05-17 | 2019-11-26 | 中国石油化工股份有限公司 | The method of dehydrogenation of isobutane catalyst and preparation method thereof and preparing isobutene through dehydrogenation of iso-butane |
| CN110496637A (en) * | 2018-05-17 | 2019-11-26 | 中国石油化工股份有限公司 | The method of dehydrogenation of isobutane catalyst and preparation method thereof and preparing isobutene through dehydrogenation of iso-butane |
| CN110496636B (en) * | 2018-05-17 | 2021-10-19 | 中国石油化工股份有限公司 | Isobutane dehydrogenation catalyst, preparation method thereof and method for preparing isobutene through isobutane dehydrogenation |
| CN110496637B (en) * | 2018-05-17 | 2021-10-19 | 中国石油化工股份有限公司 | Isobutane dehydrogenation catalyst, preparation method thereof and method for preparing isobutene through isobutane dehydrogenation |
| CN110496617B (en) * | 2018-05-17 | 2021-12-21 | 中国石油化工股份有限公司 | Isobutane dehydrogenation catalyst, preparation method thereof and method for preparing isobutene through isobutane dehydrogenation |
| CN112138657A (en) * | 2019-06-27 | 2020-12-29 | 中国石油化工股份有限公司 | Propane dehydrogenation catalyst with spherical silica gel particle as carrier and preparation method and application thereof |
| WO2024008171A1 (en) * | 2022-07-07 | 2024-01-11 | 润和科华催化剂(上海)有限公司 | Transition-metal-based dehydrogenation catalyst for low-carbon alkane, and preparation method therefor and use thereof |
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