CN105817271A - Regeneration method of dehydrogenation catalyst for low-carbon alkane - Google Patents
Regeneration method of dehydrogenation catalyst for low-carbon alkane Download PDFInfo
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/10—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using elemental hydrogen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- 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
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
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- 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
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
- B01J23/622—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead
- B01J23/626—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead with tin
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- B—PERFORMING OPERATIONS; TRANSPORTING
- 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
- B01J23/90—Regeneration or reactivation
- B01J23/96—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the noble metals
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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
- C07C5/3337—Catalytic processes with metals of the platinum group
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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
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals combined with metals, oxides or hydroxides provided for in groups C07C2523/02 - C07C2523/36
- C07C2523/56—Platinum group metals
- C07C2523/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
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- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- 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
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Abstract
The invention discloses a regeneration method of a dehydrogenation catalyst for low-carbon alkane, and belongs to the field of regeneration techniques of catalysts. The regeneration method of the dehydrogenation catalyst for the low-carbon alkane, which is provided by the invention, comprises the following processes: (1), introducing an inert gas into an inactivated dehydrogenation catalyst, and performing sweeping to lower the temperature to be 200 DEG C; (2), switching the inert gas to a gas mixture containing a reducing gas, and changing the temperature and sweeping to remove a carbon deposit by multiple procedures; (3), carrying out sweeping treatment again by using the inert gas. The catalyst treated by the three steps can be used for the dehydrogenation reaction of the low-carbon alkane continuously by switching a reaction gas. The regeneration method of the dehydrogenation catalyst for the low-carbon alkane, which is provided by the invention, avoids the use of an oxygen gas, so as to have high regeneration efficiency, reduce the reoccurring reaction time of the catalyst, and prevent the catalyst from being sintered; and the catalytic activity of the regenerated catalyst reaches the level of a fresh catalyst.
Description
Technical field
The invention belongs to catalyst regeneration techniques field, particularly to the renovation process of a kind of catalyst for dehydrogenation of low-carbon paraffin.
Background technology
Along with economic development, the demand of petrochemical industry basic material low-carbon alkene is constantly increased, cause the low-carbon alkene mainly obtained with process by-product/coproduction such as steam cracking and refinery's fluid catalytic crackings to be difficult to meet the market demand.At present, it is practicable solution by natural gas (conventional gas, shale gas, coal bed gas, combustible ice etc.), the low-carbon alkanes of by-product is converted into existing market propylene butene etc. in short supply.Therefore, catalyst for dehydrogenation of low-carbon paraffin and the production technology of exploitation efficient stable are necessary.
Dehydrogenating low-carbon alkane is strong endothermic reaction, is limited by thermodynamical equilibrium, and reaction temperature is high, and high temperature is easily caused alkane cracking and deep dehydrogenation produces surface carbon deposit, and this is the principal element causing catalysqt deactivation.Recapturing activity for eliminating surface carbon deposit, catalyst for dehydrogenation of low-carbon paraffin needs frequent regeneration to maintain long-time use continuously, and renovation process and technique are the emphasis of dehydrogenating low-carbon alkane research.At present in the patent of report, such as CN1141218A, CN1541140A, CN101940959A, CN103687666A, CN103801330A, CN104923258A and US005457077A, mainly it is passed through and carrys out removing carbon containing oxygen gas mixture, control to carry out catalyst for dehydrogenation of low-carbon paraffin regeneration by adjusting oxygen content, water vapour and oxygen-containing gas mixture ratio, HCl and oxygen-containing gas mixture ratio and compounding practice temperature in gas.
Reducibility gas equally removing carbon under high temperature, in the pyroreactions such as methane aromatizing, F-T synthesis, nitrogen oxide elimination, the reducing gas such as commonly used hydrogen regenerates the catalyst of carbon distribution inactivation.Under the same terms, oxygen removing carbon is thorough, but the supported catalyst agent carrier owing to being used has a constant volume charcoal ability, hydrogen etc., and reducibility gas partially removes carbon deposit can also recover catalyst activity；In addition, oxidizing atmosphere is easier to cause active metal sintering to make the irreversible inactivation of catalyst compared with reducing atmosphere, and oxidizing atmosphere regenerates after making charcoal and also needs to reducing catalyst again, front and back needs to switch repeatedly inert gas purge, operating procedure is many, it may have certain risk.The present invention utilizes reducing gas to eliminate carbon distribution first in dehydrogenating low-carbon alkane reacts, and simple to operate, the recovery time is short, avoids metal sintering simultaneously, can meet the needs of long period reaction.
Summary of the invention
It is an object of the invention to overcome shortcoming and deficiency present in above-mentioned prior art, it is provided that the renovation process of a kind of catalyst for dehydrogenation of low-carbon paraffin.The present invention is especially with regard to the renovation process of the noble metal-based catalysts of dehydrogenating propane, butane dehydrogenation and dehydrogenation of isobutane.Technical scheme uses reducing gas to carry out removing carbon thus regenerates catalyst for dehydrogenation of low-carbon paraffin.This method avoid metal sintering, regeneration efficiency is high, shortens the time that catalyst carries out reacting again, improves catalyst use efficiency.
The purpose of the present invention is achieved through the following technical solutions: the renovation process of a kind of catalyst for dehydrogenation of low-carbon paraffin, comprises the steps:
(1) dehydrogenation of inactivation is purged in noble gas it is cooled to 200 DEG C；
(2) switching noble gas is the gaseous mixture containing reducing gas, carrys out removing carbon through multi-step sequence alternating temperature purging；
(3) again process by inert gas purge；
Catalyst after above three step process i.e. can switch reaction gas and proceed dehydrogenating low-carbon alkane reaction.
In step (1) and step (3), described noble gas is one or more in nitrogen, helium and argon, and the air speed of described purging is 1000～20000ml/g/h.
In step (2), described reducibility gas is hydrogen, synthesis gas, CO or NH3In one or more, preferably hydrogen.
In gaseous mixture described in step (2), the volume content of reducing gas is 5～100v.%, and air speed is 2000～20000ml/g/h, and temperature is 200～650 DEG C, and the time is 0.5～6 hour.
The condition of the multi-step sequence alternating temperature purging described in step (2) is: temperature is 200～400 DEG C, and being passed through content is that 5～50v.% reducing gas carry out preliminary removing carbon, and the time is 0.5～2 hour；2～10 DEG C/min increases the temperature to 400～500 DEG C of charcoals that disappear further, and reducing gas content is maintained at 10～100v.%, and the time is 0.5～2 hour；Last 2～10 DEG C/min is warmed up to 500～650 DEG C of charcoals that disappear, and reducing gas content is maintained at 10～100v.%, and the time is 0.5～2 hour.
Dehydrogenation described in step (1) is platinum family loaded catalyst, the combination of the described platinum group one or several metals in ruthenium, rhodium, palladium, osmium, iridium, platinum, uses the mode of dipping, co-precipitation or ion exchange to introduce carrier；The carrier of described platinum family loaded catalyst is the high temperature resistant inorganic material of the mixture of the above material of the one or two kinds of in aluminium oxide, Alumina, clay or silicate, ceramic material, material with carbon element, silicon oxide, carborundum, ZSM5, MCM41, SBA15, magnesium oxide, chromium oxide, titanium oxide, zinc oxide, zirconium oxide, cerium oxide, boron nitride, complex.
As preferred embodiment, described platinum family loaded catalyst also includes auxiliary agent, described auxiliary agent includes in ii B, IIIA, IVA race metallic element selected from zinc, gallium, germanium, one or more combination of stannum, selected from lithium, sodium, potassium, rubidium, one or more combination of caesium in group ia metal element, selected from beryllium, magnesium, calcium, strontium, one or more combination of barium in group iia metallic element.
The renovation process of catalyst for dehydrogenation of low-carbon paraffin of the present invention, it is adaptable to the regeneration of the platinum family loaded catalyst used by the dehydrogenating low-carbon alkane of propane, butane or iso-butane.
The present invention has such advantages as relative to prior art and effect:
The present invention utilizes reducing gas to carry out the catalyst for dehydrogenation of low-carbon paraffin of regeneration of deactivated, and removing carbon is effective, prevents the sintering of active component to assemble, and in regenerative process, variations in temperature is little, it is easy to operation, reduces energy consumption, extends use cycle and the life-span of catalyst.
Detailed description of the invention
Below in conjunction with embodiment, the present invention is described in further detail, but embodiments of the present invention are not limited to this.
Fresh catalyst used in the embodiment of the present invention and comparative example and the dehydrogenating low-carbon alkane performance evaluation of regenerated catalyst are carried out on micro-reactor.Its appreciation condition is: reaction pressure is normal pressure, reactor feed gas is the gaseous mixture of hydrogen and propane, hydrogen and propane volume ratio are 3:1, unstripped gas air speed 15000ml/g/h, reaction temperature is 540 DEG C, reaction end gas forms through online its gas phase of Agilent chromatographic, calculates conversion of propane and Propylene Selectivity, and carbon deposit does not calculate in selectivity of product.All of catalyst carries out primary recycling after often reacting 8 hours, all use the performance data after reacting 4 hours to make comparisons.
Embodiment 1
(1)PtSn/Al2O3On catalyst 540 DEG C reaction 8 hours after switch nitrogen, air speed 6000ml/g/h, purging be cooled to 200 DEG C；
(2) 10%H of air speed 15000ml/g/h it is passed through2/N2Purging 0.5 hour, 5 DEG C/min increases the temperature to 450 DEG C and remains 0.5 hour, and 5 DEG C/min is warmed up to 540 DEG C of holdings 2 hours afterwards；
(3) again it is passed through reactor feed gas after switching nitrogen purging again to react, repeat the above steps, altogether regeneration 4 times.
The results are shown in Table 1, after reducing/regenerating 4 times, activity retains more than 85%, the oxidizing atmosphere regeneration that regeneration effect is substantially better than in comparative example 1.
Comparative example 1
(1)PtSn/Al2O3On catalyst 540 DEG C reaction 8 hours after switch nitrogen, air speed 6000ml/g/h, purging be cooled to room temperature；
(2) 10%O of air speed 6000ml/g/h it is passed through2/N2, 2 DEG C/min increases the temperature to 540 DEG C and remains 1 hour, switching nitrogen purging, is passed through the 10%H of air speed 15000ml/g/h2/N2Reductase 12 hour；
(3) switching nitrogen purging, is the most again passed through reactor feed gas and again reacts.Repeat the above steps, altogether regeneration 4 times.The results are shown in Table 1, after oxidation regeneration 4 times, activity only retains 51%.
Embodiment 2
PtGa/Al2O3Reducing atmosphere regeneration on catalyst, step, with embodiment 1, the results are shown in Table 2, PtGa/Al after reducing/regenerating 4 times2O3Activity still retain 73%.
Embodiment 3
PtZn/Al2O3Reducing atmosphere regeneration on catalyst, step, with embodiment 1, the results are shown in Table 3, PtZn/Al after reducing/regenerating 4 times2O3Activity still retain 83%.
Table 1PtSn/Al2O3On catalyst, reducing atmosphere is with oxidizing atmosphere reproduction ratio relatively
Table 2PtGa/Al2O3Reducing atmosphere regenerated outcome on catalyst
Table 3PtZn/Al2O3Reducing atmosphere regenerated outcome on catalyst
Data from the most each table can be seen that, catalyst for dehydrogenation of low-carbon paraffin after application the inventive method regeneration is compared the catalyst of oxidizing atmosphere regeneration and is had higher activity, it is clear that the method for the present invention can more efficiently regeneration catalyst for dehydrogenation of low-carbon paraffin.
Above-described embodiment is the present invention preferably embodiment; but embodiments of the present invention are also not restricted to the described embodiments; the change made under other any spirit without departing from the present invention and principle, modify, substitute, combine, simplify; all should be the substitute mode of equivalence, within being included in protection scope of the present invention.
Claims (8)
1. the renovation process of a catalyst for dehydrogenation of low-carbon paraffin, it is characterised in that: comprise the steps:
(1) dehydrogenation of inactivation is purged in noble gas it is cooled to 200 DEG C；
(2) switching noble gas is the gaseous mixture containing reducing gas, carrys out removing carbon through multi-step sequence alternating temperature purging；
(3) again process by inert gas purge；
Catalyst after above three step process i.e. can switch reaction gas and proceed dehydrogenating low-carbon alkane reaction.
The renovation process of catalyst for dehydrogenation of low-carbon paraffin the most according to claim 1, it is characterized in that: in step (1) and step (3), described noble gas is one or more in nitrogen, helium and argon, and the air speed of described purging is 1000～20000ml/g/h.
The renovation process of catalyst for dehydrogenation of low-carbon paraffin the most according to claim 1, it is characterised in that: in step (2), described reducibility gas is hydrogen, synthesis gas, CO or NH3In one or more.
The renovation process of catalyst for dehydrogenation of low-carbon paraffin the most according to claim 1, it is characterized in that: in the gaseous mixture described in step (2), the volume content of reducing gas is 5～100v.%, air speed is 2000～20000ml/g/h, temperature is 200～650 DEG C, and the time is 0.5～6 hour.
The renovation process of catalyst for dehydrogenation of low-carbon paraffin the most according to claim 1, it is characterized in that: the condition of the multi-step sequence alternating temperature purging described in step (2) is: temperature is 200～400 DEG C, being passed through content is that 5～50v.% reducing gas carry out preliminary removing carbon, and the time is 0.5～2 hour；2～10 DEG C/min increases the temperature to 400～500 DEG C of charcoals that disappear further, and reducing gas content is maintained at 10～100v.%, and the time is 0.5～2 hour；Last 2～10 DEG C/min is warmed up to 500～650 DEG C of charcoals that disappear, and reducing gas content is maintained at 10～100v.%, and the time is 0.5～2 hour.
The renovation process of catalyst for dehydrogenation of low-carbon paraffin the most according to claim 1, it is characterized in that: the dehydrogenation described in step (1) is platinum family loaded catalyst, the combination of the described platinum group one or several metals in ruthenium, rhodium, palladium, osmium, iridium, platinum, uses the mode of dipping, co-precipitation or ion exchange to introduce carrier；The carrier of described platinum family loaded catalyst is the high temperature resistant inorganic material of the mixture of the above material of the one or two kinds of in aluminium oxide, Alumina, clay or silicate, ceramic material, material with carbon element, silicon oxide, carborundum, ZSM5, MCM41, SBA15, magnesium oxide, chromium oxide, titanium oxide, zinc oxide, zirconium oxide, cerium oxide, boron nitride, complex.
The renovation process of catalyst for dehydrogenation of low-carbon paraffin the most according to claim 6, it is characterized in that: described platinum family loaded catalyst also includes auxiliary agent, described auxiliary agent includes in ii B, IIIA, IVA race metallic element selected from zinc, gallium, germanium, one or more combination of stannum, selected from lithium, sodium, potassium, rubidium, one or more combination of caesium in group ia metal element, selected from beryllium, magnesium, calcium, strontium, one or more combination of barium in group iia metallic element.
8. the application of the renovation process of the catalyst for dehydrogenation of low-carbon paraffin described in any one of claim 1～7, it is characterised in that: it is applicable to the regeneration of platinum family loaded catalyst used by the dehydrogenating low-carbon alkane of propane, butane or iso-butane.
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106694017A (en) * | 2016-11-30 | 2017-05-24 | 大连理工大学 | Catalyst for oxidative dehydrogenation of light alkane to prepare olefin, optimization method and application thereof |
| CN106732575A (en) * | 2016-12-07 | 2017-05-31 | 中国科学院大连化学物理研究所 | A kind of catalyst for preparing α naphthols and its preparation method and application |
| CN107126976A (en) * | 2017-04-25 | 2017-09-05 | 广东新华粤树脂科技有限公司 | Crack the hydrogenation catalyst steam blowing hydrogen heat air lift combining and regenerating method of carbon nine |
| CN107774239A (en) * | 2016-08-30 | 2018-03-09 | 中国石油化工股份有限公司 | For removing the renovation process of oxygenatedchemicals adsorbent in low-carbon alkene |
| CN107790112A (en) * | 2016-08-30 | 2018-03-13 | 中国石油化工股份有限公司 | For removing the activation method of oxygenatedchemicals adsorbent in low-carbon alkene |
| CN108473389A (en) * | 2016-01-21 | 2018-08-31 | 沙特基础全球技术有限公司 | Method for producing propene by dehydrogenation of propane |
| CN109736762A (en) * | 2019-03-22 | 2019-05-10 | 吉林大学 | A kind of method that oil shale in-situ catalytic oxidation extracts shale oil gas |
| CN110743593A (en) * | 2019-10-31 | 2020-02-04 | 中国石油大学(华东) | Application of boron-carbon-nitrogen material in catalyzing oxidative dehydrogenation of low-carbon alkane to prepare olefin |
| CN111085194A (en) * | 2020-01-15 | 2020-05-01 | 三门核电有限公司 | Regeneration process of nuclear power plant passive spherical dehydrogenation catalyst |
| CN112218842A (en) * | 2018-07-05 | 2021-01-12 | 陶氏环球技术有限责任公司 | Chemical treatment of catalyst treatment with hydrogen-containing supplemental fuel |
| CN113522314A (en) * | 2020-04-15 | 2021-10-22 | 中国石油化工股份有限公司 | Regeneration method of carbon deposit inactivation hydrogenation catalyst |
| CN114341122A (en) * | 2019-09-25 | 2022-04-12 | 住友化学株式会社 | Method for producing propylene oxide |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6632765B1 (en) * | 2000-06-23 | 2003-10-14 | Chervon U.S.A. Inc. | Catalyst regeneration via reduction with hydrogen |
| CN103044180A (en) * | 2012-12-28 | 2013-04-17 | 北京石油化工学院 | Method for preparing isobutylene by dehydrogenizing iso-butane |
| CN105032503A (en) * | 2015-05-13 | 2015-11-11 | 辽宁石油化工大学 | Regeneration method of noble metal catalyst |
-
2016
- 2016-04-11 CN CN201610221865.XA patent/CN105817271A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6632765B1 (en) * | 2000-06-23 | 2003-10-14 | Chervon U.S.A. Inc. | Catalyst regeneration via reduction with hydrogen |
| CN103044180A (en) * | 2012-12-28 | 2013-04-17 | 北京石油化工学院 | Method for preparing isobutylene by dehydrogenizing iso-butane |
| CN105032503A (en) * | 2015-05-13 | 2015-11-11 | 辽宁石油化工大学 | Regeneration method of noble metal catalyst |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108473389A (en) * | 2016-01-21 | 2018-08-31 | 沙特基础全球技术有限公司 | Method for producing propene by dehydrogenation of propane |
| CN107774239B (en) * | 2016-08-30 | 2020-08-07 | 中国石油化工股份有限公司 | Regeneration method of adsorbent for removing oxygen-containing compounds in low-carbon olefin |
| CN107774239A (en) * | 2016-08-30 | 2018-03-09 | 中国石油化工股份有限公司 | For removing the renovation process of oxygenatedchemicals adsorbent in low-carbon alkene |
| CN107790112A (en) * | 2016-08-30 | 2018-03-13 | 中国石油化工股份有限公司 | For removing the activation method of oxygenatedchemicals adsorbent in low-carbon alkene |
| CN107790112B (en) * | 2016-08-30 | 2020-08-07 | 中国石油化工股份有限公司 | Activation method of adsorbent for removing oxygen-containing compounds in low-carbon olefin |
| CN106694017B (en) * | 2016-11-30 | 2019-10-29 | 大连理工大学 | A kind of catalyst, its optimization method and application for low-carbon alkanes oxidative dehydrogenation alkene |
| CN106694017A (en) * | 2016-11-30 | 2017-05-24 | 大连理工大学 | Catalyst for oxidative dehydrogenation of light alkane to prepare olefin, optimization method and application thereof |
| CN106732575A (en) * | 2016-12-07 | 2017-05-31 | 中国科学院大连化学物理研究所 | A kind of catalyst for preparing α naphthols and its preparation method and application |
| CN107126976A (en) * | 2017-04-25 | 2017-09-05 | 广东新华粤树脂科技有限公司 | Crack the hydrogenation catalyst steam blowing hydrogen heat air lift combining and regenerating method of carbon nine |
| CN107126976B (en) * | 2017-04-25 | 2021-11-16 | 广东新华粤树脂科技有限公司 | Steam purging-hydrogen hot gas stripping combined regeneration method for cracking carbon nine hydrogenation catalyst |
| CN112218842A (en) * | 2018-07-05 | 2021-01-12 | 陶氏环球技术有限责任公司 | Chemical treatment of catalyst treatment with hydrogen-containing supplemental fuel |
| CN112218842B (en) * | 2018-07-05 | 2023-11-28 | 陶氏环球技术有限责任公司 | Chemical treatment of catalyst treatment with hydrogen-containing supplemental fuel |
| CN109736762A (en) * | 2019-03-22 | 2019-05-10 | 吉林大学 | A kind of method that oil shale in-situ catalytic oxidation extracts shale oil gas |
| CN114341122A (en) * | 2019-09-25 | 2022-04-12 | 住友化学株式会社 | Method for producing propylene oxide |
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