CN102463073A - Reaction device for fluidized bed catalyst performance evaluation - Google Patents
Reaction device for fluidized bed catalyst performance evaluation Download PDFInfo
- Publication number
- CN102463073A CN102463073A CN2010105528608A CN201010552860A CN102463073A CN 102463073 A CN102463073 A CN 102463073A CN 2010105528608 A CN2010105528608 A CN 2010105528608A CN 201010552860 A CN201010552860 A CN 201010552860A CN 102463073 A CN102463073 A CN 102463073A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- reactor
- control valve
- regenerator
- stream control
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a reaction device for fluidized bed catalyst performance evaluation, which mainly solves the problems that during the fluidized bed catalyst performance evaluation, the device form is single, and the purpose can not be flexibly regulated. The reaction device for the fluidized bed catalyst performance evaluation adopts the technical scheme that the reaction device mainly comprises a regenerator 4, a first reactor 10, a second reactor 15 and a lifting pipe 12, wherein the lower part of the regenerator 4 is connected with an inlet of a catalyst flow rate control valve 6, an outlet of the catalyst flow rate control valve 6 is connected with the first reactor 10, the lower part of the first reactor 10 is connected with an inlet of a catalyst flow rate control valve 13, an outlet of the catalyst flow rate control valve 13 is connected with the second reactor 15, the lower part of the second reactor 15 is connected with an inlet of a catalyst flow rate control valve 17, an outlet of the catalyst flow rate control valve 17 is connected with an inlet of the lifting pipe 12, and an outlet of the lifting pipe 12 is connected with the regenerator 4. The problems are perfectly solved, and the reaction device can be used in the fluidized bed catalyst evaluation.
Description
Technical field
The present invention relates to a kind of reaction unit that is used for the examination of fluid catalyst performance, especially be applied in the performance examination of minute fluid catalyst of level deactivation rate.
Technical background
At present; Fluidized-bed reaction technology has been widely used in fields such as petrochemical industry, Coal Chemical Industry, fine chemistry industry; Control easily owing to it has temperature, the rapid deactivation catalyst be prone to realize advantages such as cyclic regeneration, easy realization large-scale production, fluid bed obtains increasing attention in the application of chemical field.
Fluidized-bed reaction-regeneration technology is used in catalytic cracking (FCC) field in a large number; Because FCC catalysqt deactivation speed is very fast; Belong to a second level inactivation, so the basic at present riser reactor that all adopts of FCC loops back riser and continues to use after the FCC catalyst of inactivation is regenerated in regenerator.The exploitation of FCC technology and catalyst, a large amount of experimental works are exactly to accomplish on the in vitro small-sized reaction unit.FCC catalyst performance examination device the earliest is ARCO device (the Wachted S of U.S. Atlanti Richfild company exploitation; J.Am.Chem.Soc, Div Petrol Chem Mtg, 1977); It can realize continuous reaction regeneration operation; Riser reactor is connected in series by several close phase back-mixing fluid beds, non-plug-flow reaction device, so reaction effect falls far short than commercial plant.And aspect catalyst control, do not adopt guiding valve or plug valve and adopt probe, the control effect is very bad, causes the instability of catalyst circulation amount.The experimental provision that FCC technological development is afterwards adopted has adopted riser reactor; Examination catalyst performance and regenerating stability under nearly plug flow regime; The data that obtain have directiveness to the design of commercial plant; And on catalyst flows control, also adopted equipment such as guiding valve, guaranteed the stability that catalyst flows.CN 200820003767 has announced a kind of multi-functional riser catalytic cracking experimental rig; Adopt small-sized plug valve control catalyst to flow; Riser adopts multiple feed; And convenient disassembly, regenerator and settler adopt height to be arranged in juxtaposition, and this device may be used in FCC process exploitation and the evaluating catalyst.And in the examination of initial FCC catalyst reaction performance, the more employing of a lot of units is fixed fluidized bed, this be a kind of will react and regenerate check and rate the mode of separately carrying out.
At present, because the finiteness of petroleum resources, various countries unit or mechanism begin to greatly develop Coal Chemical Industry or gas chemical industry, and the technology that wherein prepares low-carbon alkene by synthesis gas through methanol causes increasing attention.In US 4499327 patents silicoaluminophosphamolecular molecular sieves catalyst applications is studied in great detail in methanol conversion system olefin process, think that SAPO-34 is the first-selected catalyst of MTO technology.The SAPO-34 catalyst has very high light olefin selectivity, and activity is also higher, and can make methanol conversion is the degree that was less than in reaction time of light olefin 10 seconds, more even reach in the reaction time range of riser.But there are deactivation rate characteristics faster in this catalyst.Because the SAPO-34 deactivation rate is very fast; The deactivation rate that probably belongs to minute level; Deactivation rate than FCC catalyst is less; This just makes and also exists very big difference based on the used experimental provision of the process exploitation of SAPO-34 catalyst that the riser reaction unit that in the past adopted, the fixed fluidized bed examination device of FCC catalyst etc. all are difficult to be applied on the catalyst of this minute level inactivation of picture SAPO-34 type.Announced a kind of reactivity worth evaluation method of preparing low carbon olefin hydrocarbon by methanol fluid catalyst among the CN200710111149; Adopt fixed fluidized bedly, in charging, add carrier gas, to reduce the deactivation rate of catalyst; The method of two root chromatogram column Conjoint Analysis is adopted in product analysis; Analyze oxygenatedchemicals and hydro carbons for one, analyze hydrogen and oxygenatedchemicals for one, adopt methane to carry out quantitatively as internal standard compound.But analysis time was long about 20 minutes the chromatography time of each sample in this method, and the deactivation rate substantial deviation of catalyst is actual, and the directive significance of the data of acquisition is had a greatly reduced quality.
Except the methanol to olefins reaction field of using the SAPO-34 catalyst; The fluidized-bed process of successive reaction-regeneration is all adopted in a plurality of fields such as preparing gasoline by methanol, naphtha catalytic cracking, olefins by catalytic cracking, alkylation of toluene, and the deactivation rate of catalyst all belongs to a minute level inactivation mostly.For minute catalyst of level inactivation, owing to adopt the technology of reaction-regeneration continued operation, and this technology and traditional FCC reaction-regeneration technology are essentially different, and make many-sides such as reactor pattern, catalyst flow that very big difference all arranged.
Though investigating, the reaction of the catalyst of minute level inactivation or regenerability also can adopt fixed fluidized bed the completion; But the catalyst stability under successive reaction-regeneration mode can instruct the large-scale plant design that crucial effects is arranged after all, so the examination under catalyst successive reaction-regeneration is very necessary.Existing reaction unit does not all have the examination problem of fine solution minute level decaying catalyst successive reaction-regeneration, has the problem that device type is single, purposes can not be adjusted flexibly.The present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the problem that device type is single, purposes is difficult to flexible adjustment when carrying out the examination of fluid catalyst performance, and a kind of new reaction unit that is used for the examination of fluid catalyst performance is provided.This reaction unit is used for the performance examination of fluid catalyst, has device type novelty, the purposes advantage of adjustment flexibly.
For addressing the above problem; The technical scheme that the present invention adopts is following: a kind of reaction unit that is used for the examination of fluid catalyst performance; Mainly comprise regenerator 4, first reactor 10, second reactor 15, riser 12; Regenerator 4 bottoms link to each other with catalyst stream control valve 6 inlets, and 6 outlets of catalyst stream control valve link to each other with first reactor 10, and first reactor, 10 bottoms link to each other with catalyst stream control valve 13 inlets; 13 outlets of catalyst stream control valve link to each other with second reactor 15; Second reactor, 15 bottoms link to each other with catalyst stream control valve 17 inlets, and 17 outlets of catalyst stream control valve link to each other with riser 12 inlets, and riser 12 outlets link to each other with regenerator 4.
In the technique scheme, said regenerator 4, first reactor 10, second reactor, 15 tops all have gas vent, and catalyst filter all is set before the gas vent; Said catalyst stream control valve is plug valve or guiding valve; Said second reactor 15 uses as stripper when no raw material charging; Said catalyst stream control valve 6 outlets link to each other with the close section mutually of first reactor 10; Said riser 12 outlets link to each other with the dilute phase section of regenerator 4; Said regenerator 4 tops are provided with catalyst addition tube line 2.
Adopt reaction unit of the present invention, can be used for minute examination of the fluid catalyst of level inactivation, can be applicable to fields such as methanol-to-olefins, alkylation of toluene, olefin cracking, light oil cracking.Especially can use this device will react some accessory substance that produces and be back to continuation generation purpose product in second reactor; As when being applied to the methanol-to-olefins evaluating catalyst; Can the carbon four above hydrocarbon that methanol conversion in second reactor generates be back to and continue to generate low-carbon alkene in first reactor; Be about to methanol-to-olefins and olefin cracking and combine investigation, expanded the purposes of this device greatly, have and adjust advantage flexibly.
Adopt technical scheme of the present invention: said regenerator 4, first reactor 10, second reactor, 15 tops all have gas vent, and catalyst filter all is set before the gas vent; Said catalyst stream control valve is plug valve or guiding valve; Said second reactor 15 uses as stripper when no raw material charging; Said catalyst stream control valve 6 outlets link to each other with the close section mutually of first reactor 10; Said riser 12 outlets link to each other with the dilute phase section of regenerator 4; Said regenerator 4 tops are provided with catalyst addition tube line 2, and device type is novel, purposes can be adjusted flexibly, has obtained better technical effect.
Description of drawings
Fig. 1 is the schematic flow sheet of device according to the invention;
Among Fig. 1,1 is the exhanst gas outlet pipeline; 2 is the catalyst addition tube line; 3 is the regenerator catalyst filter; 4 is regenerator; 5 is the regenerating medium feeding line; 6 is the catalyst stream control valve; 7 is the first material feeding tube line; 8 is the first reactor product outlet line; 9 is product mix gas outlet line; 10 is first reactor; 11 is the second reactor product outlet line; 12 is riser; 13 is the catalyst stream control valve; 14 is the second reactor catalyst filter; 15 is second reactor; 16 is the second material feeding tube line; 17 for promoting the medium feeding line; 18 is the catalyst stream control valve; 19 is the first reactor catalyst filter; 20 is that the second reactor product gas connects the first reactor product tracheae line.
First raw material gets in first reactor 10 from pipeline 7, contacts with catalyst, and the gaseous products of generation is discharged through pipeline 8; The catalyst that has carbon distribution gets in second reactor 15 behind catalyst stream control valve 13; Contact with second raw material from pipeline 16, the product of generation is discharged from pipeline 11, and decaying catalyst gets into riser 12 behind catalyst stream control valve 18; Decaying catalyst is promoted in the regenerator 4; Contact with regenerating medium, the regenerated flue gas of generation is discharged from pipeline 1, and the catalyst after the regeneration gets in first reactor 10 behind catalyst stream control valve 6.
Through embodiment the present invention is done further elaboration below, but be not limited only to present embodiment.
The specific embodiment
[embodiment 1]
On reaction unit as shown in Figure 1; Regenerator, first reactor, second reactor head all have gas vent; Catalyst filter all is set before the gas vent, and the catalyst stream control valve is a plug valve, and the outlet of catalyst stream control valve links to each other with the close section mutually of first reactor; The riser outlet links to each other with the dilute phase section of regenerator, and the regenerator top is provided with the catalyst addition tube line.The device operating pressure is normal pressure (gauge pressure), and catalyst adopts SAPO-34, and first raw material adopts carbon four above hydrocarbon mixtures; Wherein C 4 olefin content is 88% (weight); Second raw material employing purity is 99.5% methyl alcohol, and regenerating medium is an air, and regeneration temperature is 650 ℃; The first reactor reaction temperature is 550 ℃, and carbon four mass space velocities are 1.8 hours
-1, the carbon deposition quantity of catalyst mass fraction that comes out from first reactor bottom is that 1.2%, the second reactor reaction temperature is 470 ℃, the methanol quality air speed is 4.2 hours
-1, the carbon deposition quantity of catalyst mass fraction that comes out from second reactor bottom is 4.8%, it is nitrogen that riser promotes medium.The second reactor outlet product and the first reactor outlet product merge the back and get into separation process, and isolated gaseous products adopts online gas chromatographic analysis, and ethene and propylene carbon back yield are 86.74% (weight) in the gaseous products.
[embodiment 2]
According to condition and the step of embodiment 1, just first raw material employing purity is 99.5% methyl alcohol, and second raw material adopts steam, and second reactor uses as stripper, and the first reactor reaction temperature is 470 ℃, and the methanol quality air speed is 4.2 hours
-1, the carbon deposition quantity of catalyst mass fraction that comes out from first reactor bottom is 4.3%, behind stripping, gets into riser, ethene and propylene carbon back yield are 81.28% (weight) in the gaseous products.
Obviously, adopt device of the present invention, can carry out the successive reaction-regenerability examination of fluid catalyst, device type is novel, purposes is adjusted flexibly, has bigger technical advantage, can be used for the performance examination of fluid catalyst.
Claims (7)
1. one kind is used for the reaction unit that the fluid catalyst performance is checked and rated; Mainly comprise regenerator (4), first reactor (10), second reactor (15), riser (12); Regenerator (4) bottom links to each other with catalyst stream control valve (6) inlet; Catalyst stream control valve (6) outlet links to each other with first reactor (10); First reactor (10) bottom links to each other with catalyst stream control valve (13) inlet, and catalyst stream control valve (13) outlet links to each other with second reactor (15), and second reactor (15) bottom links to each other with catalyst stream control valve (17) inlet; Catalyst stream control valve (17) outlet links to each other with riser (12) inlet, and riser (12) outlet links to each other with regenerator (4).
2. according to the said reaction unit that is used for the examination of fluid catalyst performance of claim 1, it is characterized in that said regenerator (4), first reactor (10), second reactor (15) top all have gas vent, all are provided with catalyst filter before the gas vent.
3. according to the said reaction unit that is used for the examination of fluid catalyst performance of claim 1, it is characterized in that said catalyst stream control valve is plug valve or guiding valve.
4. according to the said reaction unit that is used for fluid catalyst performance examination of claim 1, it is characterized in that said second reactor (15) uses as stripper when no raw material charging.
5. according to the said reaction unit that is used for the examination of fluid catalyst performance of claim 1, it is characterized in that said catalyst stream control valve (6) outlet links to each other with the close section mutually of first reactor (10).
6. according to the said reaction unit that is used for the examination of fluid catalyst performance of claim 1, it is characterized in that said riser (12) outlet links to each other with the dilute phase section of regenerator (4).
7. according to the said reaction unit that is used for the examination of fluid catalyst performance of claim 1, it is characterized in that said regenerator (4) top is provided with catalyst addition tube line (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010552860.8A CN102463073B (en) | 2010-11-17 | 2010-11-17 | Reaction device for fluidized bed catalyst performance evaluation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010552860.8A CN102463073B (en) | 2010-11-17 | 2010-11-17 | Reaction device for fluidized bed catalyst performance evaluation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102463073A true CN102463073A (en) | 2012-05-23 |
| CN102463073B CN102463073B (en) | 2014-10-15 |
Family
ID=46067369
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010552860.8A Expired - Fee Related CN102463073B (en) | 2010-11-17 | 2010-11-17 | Reaction device for fluidized bed catalyst performance evaluation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102463073B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103539717A (en) * | 2012-07-12 | 2014-01-29 | 中国石油化工股份有限公司 | Reaction device for producing benzpyrole |
| CN104437274A (en) * | 2013-09-16 | 2015-03-25 | 中国石油大学(华东) | Fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO) |
| CN110361499A (en) * | 2018-04-09 | 2019-10-22 | 国家能源投资集团有限责任公司 | The method of iron-base fischer-tropsch synthesis catalyst activity rating |
| CN112569873A (en) * | 2019-09-27 | 2021-03-30 | 中国石油化工股份有限公司 | Solid acid alkylation reaction and regeneration device and solid acid alkylation method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1356299A (en) * | 2001-12-14 | 2002-07-03 | 清华大学 | Process and system for preparing low-carbon olefin from methanol or dimethylether |
| CN101164686A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Multi-bed combination type reactor |
| CN101165026A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene from methanol and dimethyl ether |
| CN201223790Y (en) * | 2008-02-20 | 2009-04-22 | 北京世纪瑞格科技有限公司 | Multifunctional riser catalytic cracking test device |
-
2010
- 2010-11-17 CN CN201010552860.8A patent/CN102463073B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1356299A (en) * | 2001-12-14 | 2002-07-03 | 清华大学 | Process and system for preparing low-carbon olefin from methanol or dimethylether |
| CN101164686A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Multi-bed combination type reactor |
| CN101165026A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene from methanol and dimethyl ether |
| CN201223790Y (en) * | 2008-02-20 | 2009-04-22 | 北京世纪瑞格科技有限公司 | Multifunctional riser catalytic cracking test device |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103539717A (en) * | 2012-07-12 | 2014-01-29 | 中国石油化工股份有限公司 | Reaction device for producing benzpyrole |
| CN103539717B (en) * | 2012-07-12 | 2016-05-18 | 中国石油化工股份有限公司 | Produce the reaction unit of indoles |
| CN104437274A (en) * | 2013-09-16 | 2015-03-25 | 中国石油大学(华东) | Fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO) |
| CN104437274B (en) * | 2013-09-16 | 2017-01-11 | 中国石油大学(华东) | Fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO) |
| CN110361499A (en) * | 2018-04-09 | 2019-10-22 | 国家能源投资集团有限责任公司 | The method of iron-base fischer-tropsch synthesis catalyst activity rating |
| CN112569873A (en) * | 2019-09-27 | 2021-03-30 | 中国石油化工股份有限公司 | Solid acid alkylation reaction and regeneration device and solid acid alkylation method |
| CN112569873B (en) * | 2019-09-27 | 2022-07-15 | 中国石油化工股份有限公司 | Solid acid alkylation reaction and regeneration device and solid acid alkylation reaction and regeneration method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102463073B (en) | 2014-10-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108017496B (en) | Apparatus for producing olefins and aromatic hydrocarbons and method thereof | |
| CN108017487B (en) | Two-stage reaction method for preparing aromatic hydrocarbon from oxygen-containing compound-containing raw material | |
| CN102464532B (en) | Method for preparing low-carbon olefins | |
| CN111484387A (en) | A method for converting a naphtha-containing feedstock into light olefins and/or aromatics | |
| CN102875296A (en) | Reaction unit for preparing low-carbon olefins | |
| CN102463073B (en) | Reaction device for fluidized bed catalyst performance evaluation | |
| CN102463082B (en) | Reactor for fluidized bed catalyst evaluation | |
| CN111233609B (en) | Naphtha-containing raw material conversion device | |
| CN101164686B (en) | Multi-bed combination type reactor | |
| CN111233608A (en) | A kind of raw material conversion method containing naphtha | |
| CN102466661A (en) | Evaluation device of fluidized bed catalyst for preparing olefin from methanol | |
| CN102872773B (en) | Reaction unit for evaluating performance of fluid catalyst | |
| CN102464522A (en) | Production method of low-carbon olefin | |
| CN101333143A (en) | Method for producing arene from petroleum cracking dry gas | |
| CN111056901B (en) | Reaction system and reaction method for preparing aromatic hydrocarbon through catalytic conversion of methanol | |
| CN102875283B (en) | The method of low-carbon alkene is prepared by methyl alcohol and petroleum naphtha | |
| WO2020157540A1 (en) | Method for the conversion of feedstock containing naphtha to low carbon olefins and aromatics | |
| CN111100664B (en) | Method for preparing aromatic hydrocarbon by catalytic conversion of methanol | |
| CN102875295B (en) | Production method of low-carbon olefins | |
| US12122961B2 (en) | System for catalytic cracking of naphtha with mixed spent and regenerated catalyst | |
| CN102875288B (en) | Method for producing low-carbon olefins | |
| CN102463079A (en) | Reaction device for producing low-carbon olefin from methanol | |
| CN102875291B (en) | Method for producing low-carbon olefins from methanol | |
| CN102875284B (en) | The reaction unit of low-carbon alkene is prepared with methyl alcohol and petroleum naphtha | |
| CN102872761B (en) | Production device of low-carbon olefins |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20141015 Termination date: 20171117 |