CN108368000A - For producing C3To C5The method of alkene - Google Patents
For producing C3To C5The method of alkene Download PDFInfo
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- CN108368000A CN108368000A CN201680072615.2A CN201680072615A CN108368000A CN 108368000 A CN108368000 A CN 108368000A CN 201680072615 A CN201680072615 A CN 201680072615A CN 108368000 A CN108368000 A CN 108368000A
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- Prior art keywords
- catalyst
- regenerator
- gas
- vertical baffle
- alkene
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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
- B01J38/12—Treating with free oxygen-containing gas
- B01J38/30—Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/06—Propene
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/08—Alkenes with four carbon atoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/10—Alkenes with five carbon atoms
-
- 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
-
- 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
-
- 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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Providing makes dehydrogenation of corresponding paraffins produce С in the fluid bed by the chromium oxide aluminium oxide catalyst recycled in systems3To С5The method of alkene, the system comprises the reductive desorption preparation units of the catalyst after reactor, regenerator (13) and regenerator (13), wherein described prepared by being carried out with reducing gas processing catalyst under reverse flow state using horizontal subdivision screen (2).Thus, the reductive desorption preparation of catalyst is an immediately proceeding at after regenerator (13) using vertical baffle (6) in the orientation of the catalyst under recurrent state, then it is carried out under reverse flow state, fluid bed is divided by the vertical baffle (6) promotes section (14) and head pressure section (15), wherein the ratio between the residence time of the catalyst in this condition is 0.3 to 3.0.Technical result is that the yield of target product especially alkene improves.
Description
Technical field
The present invention relates to petrochemistry fields, and the method for being particularly used for production alkene, the alkene are further
Basic monomer for producing synthetic rubber and the production for polypropylene, methyl t-butyl ether etc..
Background technology
In the presence of by make in the reactor-regenerator system with mobile coarse grain catalyst dehydrogenation of corresponding paraffins come
Produce known method (Ya.Ya.Kirnos, O.B.Litvin " the Modern industrial methods of of alkene
butadiene synthesis”.Analytic comparative reviews of TsNIITENeftekhim,series
" Production of synthetic rubbers ", Moscow, page 1967,81).
The shortcomings that known method, is the impossible of the complicated instrument and design high productive capacity device of reactor unit
Property, the difficulty of the cycle due to arranging coarse grain catalyst in reactor-regenerator system.
In the presence of the known method for producing light olefin (in patent RU 2125079, IPC that on January 20th, 1999 announces
C10G11/18, B01J8/18), it the described method comprises the following steps：It is former that hydrocarbon is fed in the reaction zone comprising solid catalyst
Material, makes the hydrocarbon raw material in reaction zone be contacted with catalyst under conditions of being conducive to hydrocarbon and being catalytically converted into light olefin, turns in catalysis
The reaction product of acquisition is separated from reaction zone after change, separating catalyst simultaneously makes the catalyst of inactivation in a regenerator
Regeneration.According to the present invention, hydrocarbon raw material and urging in the reactor with recirculating fluidized bed were made with 0.1 second to 3 seconds residence time
Agent contacts.
The method proposed does not allow for С3To С5The commercial dehydrogenation performance of alkane：Reactor production capacity is just led to
It crosses and the olefins yield for the material quantity that decomposes.
Immediate scheme is by being urged with particulate chrominaalumina on technological essence and the result realized
The dehydrogenation of the corresponding paraffins carried out in the system of the fluid bed of agent is come the method for producing alkene, and the system comprises reactions
The reduction for the regenerated catalyst that device, regenerator and catalyst recycle therebetween-desorption preparation unit (R.K.Mikhailov,
A.N.Bushin,I.Ya.Tyuryaev,S.M.Khripina“Preparation of a catalyst for the
dehydrogenation of paraffinic hydrocarbons”,Scientific and Technical
Collected Volume " Synthetic Rubber Industry ", TsNIITENeftekhim, Moscow, the 1969, the 4th
Phase, page 3 to 6).
According to this method, before catalyst is fed to reactor, reduction-desorption preparation of regenerated catalyst is logical
In gas-catalyst adverse current shape in the case of mistake in preparation unit using through (fall-through) type horizontal subdivision screen
It is carried out with reducing gas processing catalyst under state.
Due to the mass exchange process in the used method for making catalyst be contacted with short time of contact with gas
Low rate and by the low gas linear velocity in the preparation unit of dehydrogenation system design limitation, the method can not achieve catalyst
The reduction (preparation) of enough depth.All these yields for leading to the target product from certain embodiments reduce.
Invention content
The fluidisation of chromia-alumina catalyst is improved the purpose of the present invention is the raising due to catalyst reduction degree
The yield of the target product during paraffin dehydrogenation in bed.
Providing in the fluid bed by the chromia-alumina catalyst recycled in systems makes dehydrogenation of corresponding paraffins
To produce С3To С5The method of alkene, the system comprises the catalyst after reactor, regenerator 13 and the regenerator 13
Reduction-desorption preparation unit.
The preparation is urged by being handled with reducing gas under reverse flow state using horizontal subdivision screen 2
Agent carries out.In addition, after the regenerator 13, the processing is using vertical baffle 6
It in the orientation of catalyst under recurrent state, is then carried out under reverse flow state, fluid bed is divided by the vertical baffle 6
Section 14 and head pressure section 15 are promoted, wherein the ratio between the residence time of catalyst in this condition is 0.3 to 3.0.
As reducing gas, hydrogen-containing gas С О, C can be used1-С5Hydrocarbon and its mixture.
Vertical baffle 6 can be designed as circulation pipe.
Vertical baffle 6 can be placed on the top for the reducing zone 1 being incorporated in 13 bottom of regenerator.
Vertical baffle 6 can indicate the extension of the vertical component for the reducing zone 8 being included in 13 container bottom of regenerator.
Preferably, linear velocity of the linear velocity higher than the gas in head pressure section 15 of the gas in section 14 is promoted.
The reducing gas of reduction from catalyst-desorption preparation unit can be discharged into the gaseous fuel of regenerator 13
Combustion zone.
The catalyst of carbonization and reduction is fed to regenerator 13 for coke burning-up, oxidation from paraffin dehydrogenation reactor
And heating.Coke burns out the burning using gaseous fuel at 640 DEG C to 680 DEG C, is preferably carried out at 650 DEG C.
Reducing gas include a large amount of residual reducing gas, the residual reducing gas with catalyst it is complete restore needed for
1.2 to 2.0 times of amount of amount be fed to reduction-desorption preparation unit bottom.Residual gas is in regenerator bottoms in order to prevent
Undesirable burning in (catalyst zoneofoxidation), the gas from catalyst preparation unit should advantageously be guided to again
The gas fuel combustion area of raw device 13.
Technical result is that the yield of target product especially alkene improves.
Description of the drawings
A variety of design schemes can be used to implement the scheme provided in the present invention.
Fig. 1, Fig. 2 and Fig. 3 show the schematic diagrames of the reduction of catalyst-desorption preparation unit.
According to Fig. 1, preparation carries out in the reducing zone 1 in being incorporated to 13 bottom of regenerator.The quilt in entire height of reducing zone 1
Separate through screen 2 is separated.Reducing gas is fed to the bottom of reducing zone 1 by injector 3.Nitrogen is by being located under injector 3
The injector 4 of side is fed.Vertical baffle 6 can be flat, cylindrical, tubulose or can be other shape.
In order to implement process according to the present invention, vertical baffle 6 is arranged in the spray for supplying the air to regenerator 13
The top of the reducing zone 1 of 5 lower section of emitter, wherein baffle are designed to feed nitrogen thereto to provide catalyst on reducing zone 1
The circulation pipe of recycling in portion.It can be seen from figure 1, for regenerator 13 provide air injector 5 be located at
The space between separation screen 7 below 6 bottom end of circulation pipe is the of the catalyst preparation operated under recurrent state in orientation
One stage 17.Separate screen 7 and for reduction sleeve 1 bottom supply nitrogen injector 4 between space be in catalyst
With the second stage 16 of the catalyst preparation operated under gas reverse flow state.The catalyst that reactor is recycled to from regenerator 13 exists
It is subjected to while prepared by reduction-desorption continually by the first stage contacted with supply to the reducing gas and nitrogen of reducing zone 1
And second stage.
According to fig. 2, the preparation of catalyst carries out in the reducing zone 8 in being incorporated to regenerator 13 so that the top of reducing zone 8
It is inserted into the bottom of regenerator vessel and represents vertical baffle 6, wherein the upper end 9 of reducing zone 8 is located at for regenerator 13
The lower section of the injector 10 of air is provided.
In order to implement process according to the present invention, in the shell on the reducing zone top in the region in regenerator vessel
In the presence of the opening 11 overflowed for catalyst.In the slot of regenerator conical lower portion below the opening overflowed for catalyst,
In the presence of the injector 12 for feeding catalyst fluidization gas.This causes in the opening overflowed for catalyst and for again
Raw device provides cycle in the strong orientation for occur in the region between the injector 10 of air catalyst.The region is to be located at also
The first stage 17 of the catalyst preparation unit of 16 top of the second preparatory phase in 8 bottom of former area.
Fig. 3 shows that reducing gas is expelled to the gas fuel combustion area of regenerator 13 from reduction-desorption preparation unit.
It restores exhaust gas to supply to gas fuel combustion area by insertion piece 21, by pipeline 18 to the gas fuel combustion
Area provides gaseous fuel to keep Target regeneration temperatures.The catalyst for carrying out autoreduction-desorption preparation unit is fed to by pipe 19
Paraffin dehydrogenation reactor.Reducing gas is emitted into waste heat boiler (not shown in FIG.) by pipeline 20 from regenerator 13.
Therefore, recurrent state in the orientation in order to realize the catalyst in fluid bed can arrange vertical in a fluidized bed
Baffle 6, which, which is divided into fluid bed, promotes section 14 and head pressure section 15.Baffle 6 can have in its bottom for urging
The opening 11 that catalyst overflows during interior (in the baffle position) cycle of agent.In order to provide the cycle of catalyst, supply is extremely
The linear velocity for promoting the gas of section 14 should be above the linear velocity of the gas in a pressure section 15.Therefore, it is promoted in section 14
Catalyst concn and the head pressure of corresponding catalyst layer will be less than catalyst concn in a pressure section 15 and corresponding catalysis
The head pressure of oxidant layer, which ensure that catalyst rise in promoting section 14 and in head pressure section 15 decline during catalyst it is strong
Cycle in strong orientation.
In order to realize catalyst and reducing gas reverse flow state, it can use and provide catalyst and gas in screen opening
Countercurrent movement with free cross-sectional area run through horizontal subdivision screen.Screen can have such as slit-shaped openings and can
With by being manufactured with the angled inclined angle bar such as gas flow direction, pipe, tablet.
Due to the fact that the starting stage prepared in chromia-alumina catalyst is provided in the orientation of catalyst
The additional preparatory phase operated under recurrent state allows to improve reduction (preparation) degree of catalyst and reduce to catalyst
Prepare the consumption of the reducing gas of supply：
With the strong interior cycle of catalyst and with the increased quality in the increased stage of gas linear velocity
It exchanges；
The repeatable recycling that catalyst passes through the space in the stage；
Due to strong directed circulation and the space in stage caused by increasing because of the section in stage (diameter)
It may increase, with the increase of the increased catalyst residence times of the catalyst concn in the space in the stage；
In the case where the two benches of catalyst prepare the reallocation with the conversion of reducing gas in each stage, reduction process
" milder " implement.
During the preparation of regeneration (oxidation) catalyst before catalyst is fed to reactor, including chromium oxidation of appraising at the current rate
The increased reducing degree of the catalyst of object reduces the sexavalence metal oxide supplied together with recycling catalyst to reactor
(CrO3Type) amount.In view of in the reducing environment of reactor, sexavalence metal oxide (CrO3) it is being produced as catalyst poison
Vapor in the case of be changed into trivalent metal oxide (Cr2O3Type), catalyst reduction journey in reduction-desorption preparation unit
The increase of degree leads to the raising of dehydrogenation
In the case that the ratio between catalyst residence times within the stage of reduction-desorption preparation unit are less than 0.3, have and urge
Improvement and corresponding dehydrogenation of the additional stage recycled in the orientation of agent to the operating characteristics of generally preparation unit
Improved influence is no longer detectable, and than more than 3, the operating characteristics of preparation unit and corresponding dehydrogenation drop
It is low.
Specific implementation mode
It is illustrated by the following examples the present invention.
Embodiment 1
Dehydrogenation from normal butane to butylene with including 14 weight %Cr2O3, 3 weight %K2O, 9 weight %SiO2With 74 weights
Measure % А 12O3Chromia-alumina catalyst fluidized bed plant in carry out.The device include reactor and have catalyst
The regenerator continuously recycled.Fig. 1 gives the figure of reduction-desorption preparation unit of catalyst.It will be used as reduction by injector 3
The natural gas (methane content is about 97 weight %) of gas is with 15Nm3(equivalent to about 120 hours/hour-1Air speed) amount into
To the bottom to reducing zone 1.By the injector 4 positioned at 3 lower section of injector with about 10Nm3(equivalent to about 70 hours/hour-1
Air speed) amount feed nitrogen.It is carried out at a temperature of 650 DEG C at a temperature of 585 DEG C and in a regenerator in the reactor
The process.Normal butane was fed to reactor with 480kg/ hours amounts.Catalyst is by reducing zone 1 in reactor-regeneration
Internal circulating load in device system is 7.2t/ hours.Residence time of the catalyst in reducing zone 1 is 1.7 minutes to 1.9 minutes.It will
Nitrogen is with about 5Nm3The amount of/hour is fed into circulation pipe 6 for making the catalyst in 1 top of reducing zone recycle.
Table 1 provides the data of other conditions and dehydrogenation about process.The same table is provided according to closest
Prior art normal butane dehydrogenation under similar conditions result.
Embodiment 2
Including 20 weight %Cr in a manner of similar to embodiment 12O3, 2 weight %K2O, 2 weight %SiO2With 76 weights
Measure % А 12O3Catalyst on carry out dehydrogenation of the iso-butane to isobutene, however desorption temperature be 580 DEG C, regeneration temperature 650
℃.Internal circulating load of the catalyst between reactor and regenerator is 6.9t/ hours, and isobutane feed amount is 450kg/ hours.Fig. 2
The figure that reduction-desorption preparation unit of the regenerated catalyst before regenerated catalyst is fed to reactor is given with Fig. 3 exists.
In order to implement process according to the present invention, gas is supplied so that catalyst fluidization to injector 12.With 5Nm3/ hour
Amount feed natural gas as reducing gas.Reducing gas is discharged into gas fuel combustion area.
Table 1 provides the data of other conditions and dehydrogenation about process.The same table is provided according to closest
Prior art dehydrogenation of isobutane under similar conditions result.
Embodiment 3
Dehydrogenation of the propane to propylene carries out on the catalyst similar with the catalyst used in embodiment 2, wherein using
According to the reduction of the catalyst of the same embodiment-desorption preparation unit.Therefore, dehydrogenating propane temperature is 590 DEG C, and regeneration temperature is
650 DEG C, internal circulating load of the catalyst between reactor and regenerator is 5.8t/ hours, and propane feed amount is 400kg/ hours.
Table 1 provides the data of other conditions and dehydrogenation about process.The same table is provided according to closest
Prior art dehydrogenating propane under similar conditions result.
Embodiment 4
Isopentane dehydrogenation carries out on the catalyst similar with catalyst used in embodiment 1, wherein using according to same
The reduction of the catalyst of one embodiment-desorption preparation unit.It is 575 DEG C to this isopentane desorption temperature, regeneration temperature 650
DEG C, internal circulating load of the catalyst between reactor and regenerator is 7.2t/ hours, and isopentane inlet amount is 480kg/ hours.
Table 1 provides the data of other conditions and dehydrogenation about process.The same table is provided according to closest
Prior art isopentane dehydrogenation under similar conditions result.
From the alkene production that can be seen that in the embodiment of offer during proposed method allows raising paraffin dehydrogenation
Rate.
Industrial applicability
What is proposed is used to produce С3To С5The method of alkene can be used for producing polypropylene, methyl tertiary butyl ether(MTBE) etc..
1. dehydrogenation of table
*t1Residence time of the catalyst in the first stage of preparation unit under recurrent state in the orientation of catalyst.
t2Residence time of the catalyst in the second stage of preparation unit under the reverse flow state of catalyst and gas.
Claims (6)
1. making dehydrogenation of corresponding paraffins next life in a kind of fluid bed by the chromia-alumina catalyst recycled in systems
Produce С3To С5The method of alkene, the system comprises the catalysis after reactor, regenerator (13) and the regenerator (13)
The reduction of agent-desorption preparation unit, wherein it is described preparation be by using horizontal subdivision screen (2) in the case of in adverse current shape
With reducing gas the catalyst is handled under state to carry out, which is characterized in that described after the regenerator (13)
Processing is using vertical baffle (6) in the orientation of the catalyst under recurrent state, then in reverse flow state
Lower progress, the fluid bed is divided by the vertical baffle (6) promotes section (14) and head pressure section (15), wherein described urge
The ratio between the residence time of agent in this condition is 0.3 to 3.0.
2. according to the method described in claim 1, it is characterized in that, the vertical baffle (6) is designed to circulation pipe.
3. according to the method described in claim 2, it is characterized in that, the vertical baffle (6) is placed on and is incorporated to the regeneration
The top of reducing zone (1) in device (13) bottom.
4. according to the method described in claim 2, it is characterized in that, the vertical baffle (6) is the vertical component of reducing zone (8)
Extension, the reducing zone (8) is included in the regenerator (13) container bottom.
5. according to the method described in claim 1, it is characterized in that, the linear velocity for promoting the gas in section (14) is higher than
The linear velocity of gas in the head pressure section (15).
6. the method according to any one of claims 1 to 5, it is characterized in that, the reduction-from the catalyst
The reducing gas of desorption preparation unit is discharged into the gas fuel combustion area of the regenerator (13).
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| RU2015153678 | 2015-12-14 | ||
| RU2015153678A RU2619128C1 (en) | 2015-12-14 | 2015-12-14 | Method for obtaining olefin c3-c5 carbohydrates |
| PCT/RU2016/000870 WO2017105283A1 (en) | 2015-12-14 | 2016-12-13 | Method for producing с3 -с5 olefinic hydrocarbons |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108368000A true CN108368000A (en) | 2018-08-03 |
Family
ID=58715849
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201680072615.2A Pending CN108368000A (en) | 2015-12-14 | 2016-12-13 | For producing C3To C5The method of alkene |
Country Status (3)
| Country | Link |
|---|---|
| CN (1) | CN108368000A (en) |
| RU (1) | RU2619128C1 (en) |
| WO (1) | WO2017105283A1 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2666541C1 (en) * | 2017-12-04 | 2018-09-11 | Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" | Method for obtaining olefin hydrocarbons |
| RU2710017C1 (en) * | 2019-10-28 | 2019-12-24 | Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" | Device for preparation of catalyst in processes of dehydrogenation of paraffin hydrocarbons c3-c5 |
| RU2710016C1 (en) * | 2019-10-28 | 2019-12-24 | Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" | Method of preparing a catalyst in dehydrogenation of paraffin hydrocarbons c3-c5 and device for its implementation |
| RU2719490C1 (en) * | 2019-10-28 | 2020-04-17 | Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" | Device for preparation of catalyst in processes of dehydrogenation of paraffin hydrocarbons c3-c5 |
| WO2023009031A1 (en) * | 2021-07-26 | 2023-02-02 | Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" | Regenerator for a с3-с5 paraffin dehydrogenation system (variants) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5198397A (en) * | 1991-11-25 | 1993-03-30 | Mobil Oil Corporation | Two-stage fluid bed regeneration of catalyst with shared dilute phase |
| RU2224735C1 (en) * | 2002-10-28 | 2004-02-27 | Щербань Георгий Трофимович | Olefin hydrocarbon production process |
| CN101331211A (en) * | 2005-12-20 | 2008-12-24 | 国际壳牌研究有限公司 | A process and apparatus for the regeneration of spent FCC catalyst |
| RU2402514C1 (en) * | 2009-04-01 | 2010-10-27 | Министерство Промышленности И Торговли Российской Федерации | С3-с5 olefin synthesis method and catalyst to this end |
| CN101903087A (en) * | 2007-12-20 | 2010-12-01 | 切弗朗菲利浦化学公司 | Continuous catalyst activator |
| CN103449948A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气集团公司 | Method for preparing olefin through dehydrogenating alkane |
| CN103706378A (en) * | 2013-12-25 | 2014-04-09 | 上海华畅环保设备发展有限公司 | Treatment method and device for concentrating, drying and detoxifying dead catalyst entrained in isobutylene during preparation of isobutylene by isobutane dehydrogenation |
-
2015
- 2015-12-14 RU RU2015153678A patent/RU2619128C1/en active
-
2016
- 2016-12-13 CN CN201680072615.2A patent/CN108368000A/en active Pending
- 2016-12-13 WO PCT/RU2016/000870 patent/WO2017105283A1/en active Application Filing
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5198397A (en) * | 1991-11-25 | 1993-03-30 | Mobil Oil Corporation | Two-stage fluid bed regeneration of catalyst with shared dilute phase |
| RU2224735C1 (en) * | 2002-10-28 | 2004-02-27 | Щербань Георгий Трофимович | Olefin hydrocarbon production process |
| CN101331211A (en) * | 2005-12-20 | 2008-12-24 | 国际壳牌研究有限公司 | A process and apparatus for the regeneration of spent FCC catalyst |
| CN101903087A (en) * | 2007-12-20 | 2010-12-01 | 切弗朗菲利浦化学公司 | Continuous catalyst activator |
| RU2402514C1 (en) * | 2009-04-01 | 2010-10-27 | Министерство Промышленности И Торговли Российской Федерации | С3-с5 olefin synthesis method and catalyst to this end |
| CN103449948A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气集团公司 | Method for preparing olefin through dehydrogenating alkane |
| CN103706378A (en) * | 2013-12-25 | 2014-04-09 | 上海华畅环保设备发展有限公司 | Treatment method and device for concentrating, drying and detoxifying dead catalyst entrained in isobutylene during preparation of isobutylene by isobutane dehydrogenation |
Also Published As
| Publication number | Publication date |
|---|---|
| RU2619128C1 (en) | 2017-05-12 |
| WO2017105283A1 (en) | 2017-06-22 |
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Application publication date: 20180803 |