CN110117214A - A kind of device and method of methanol Efficient Conversion producing light olefins - Google Patents
A kind of device and method of methanol Efficient Conversion producing light olefins Download PDFInfo
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- CN110117214A CN110117214A CN201910457418.8A CN201910457418A CN110117214A CN 110117214 A CN110117214 A CN 110117214A CN 201910457418 A CN201910457418 A CN 201910457418A CN 110117214 A CN110117214 A CN 110117214A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/82—Phosphates
- C07C2529/84—Aluminophosphates containing other elements, e.g. metals, boron
- C07C2529/85—Silicoaluminophosphates (SAPO compounds)
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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
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- 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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- 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
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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Abstract
The invention discloses a kind of devices of methanol Efficient Conversion producing light olefins, including the first riser reactor, dense-phase fluidized bed reactor, the second riser reactor and regenerator；First riser reactor is connected with the first gas-solid quick separating equipment being arranged in the first settler；Dense bed reactor is connected by pre- carbon deposition catalyst feed-line with the first settler, the second gas-solid quick separating equipment is equipped in second settler, dense bed reactor outlet connects the second riser reactor, and the second riser reactor is connected with the second gas-solid quick separating equipment；Regenerator is connected by reclaimable catalyst feed-line with the second settler, and regenerator is connected by regenerative agent feed-line with the first riser reactor.Invention additionally discloses a kind of methods of methanol Efficient Conversion producing light olefins.The present invention converts C4 or more hydrocarbon component using complete regenerated catalyst, and carries out pre- carbon distribution to catalyst, significantly improves selectivity of light olefin and yield.
Description
Technical field
The present invention relates to a kind of device and methods of methanol Efficient Conversion producing light olefins, belong to chemical technology field.
Background technique
The low-carbon alkenes such as ethylene, propylene are important basic chemical industry raw material, are widely used in various polymeric material fields, relate to
And the every profession and trades such as agricultural, automobile, daily necessities, with the development of national economy, demand growth is quick.Traditional production technology master
To come from naphtha catalytic cracking.In recent years, due to the maturation of shale gas exploitation technology, the propane of by-product, ethane resource increase,
Using ethane, propane as raw material producing ethylene by cracking, propylene technology maturation, process units gradually increases, it has also become alkene production capacity
Important supplement.However, ethane propane flammable gas is mainly from import, China's Domestic Resources are less, and foreign countries always can to the control of raw material
Influence the stable operation of device.Rich coal resources in China is as raw material, via the MTO technique of preparing light olefins from methanol using coal
Meet the important channel of the substitution petroleum and alkane cracking process route of China's Energy Situation, good economy performance, raw material sources can
Control, can be effectively relieved the dependence to import raw material, meet domestic demand.
SAPO-34 molecular sieve is the discovery that MTO technology realizes industrialized key.Because it is with unique 3 D pore canal eight
Ring structure and suitable acid centre and good hydrothermal stability, show excellent in reaction for preparing light olefins from methanol
Catalytic performance.Currently, industrial mature MTO technique mainly has middle petrochemical industry S-MTO technique, Dalian Chemistry and Physics Institute DMTO technique, beauty
Uop Inc., state MTO technique.The catalyst of use is all SAPO-34 active component.The methanol to olefins reaction of SAPO-34 catalysis
There are apparent induction period, i.e. reaction initial stage, conversion ratio and olefine selective increases with the increase of catalyst carbon deposition,
Due to inactivating after catalyst carbon deposition rapidly, MTO reaction uses Circulating Fluidized Bed Process, and the catalyst after inactivation is made charcoal again
It is raw, the methanol conversion activity of Lai Huifu catalyst.
While methanol produces ethylene, propylene through MTO reaction process, meeting by-product largely mixes C4, C5+ component, carbon-based
Yield is total to account for about 13-15%, this portioned product added value is lower, and common Land use systems have directly as by-product sale, or
Separating-purifying utilizes, or carries out cracking increasing output of ethylene and propylene product through olefin cracking technique, wherein increasing production second through cracking technology
Alkene and propylene product have stronger economy.
The prior art is related to the technology of more C4 or more component cracking increasing output of ethylene and propene yield, and auxiliary can be set
Reactor and regenerative system, to after separation C4 and the above component carry out cracking reaction, or by after separation by C4 and above group
Divide and returns to main reactor progress cracking reaction.C4 and the above component are returned to main reactor, and there are C4 treating capacities to be restricted, conversion
Individual cracker is arranged in the not high problem of rate, C4 and the above component, and the catalyst inactivated after C4 conversion still has conversion first
The activity of alcohol alkene, is not efficiently used.
Summary of the invention
The technical problem to be solved by the present invention is to overcome the deficiencies of existing technologies, it is low to provide a kind of methanol Efficient Conversion system
The device and method of carbon olefin handles C4 and the above hydrocarbon component by setting riser reactor, and carbon distribution rear catalyst passes through
Settler separate rear part point is recycled back to riser reactor, continues to convert C4 and the above component, can be handled with effective solution C4
Low problem is measured, and uses same catalyst, the catalyst after carbon distribution enters main reaction system, and it is anti-to continue to participate in methanol-to-olefins
It answers, the selectivity of reaction for preparing light olefins from methanol greatly improved.
In order to solve the above technical problems, the present invention provides a kind of device of methanol Efficient Conversion producing light olefins, feature
It is, including the first riser reactor, dense-phase fluidized bed reactor, the second riser reactor and regenerator；First riser
Reactor is connected with the first gas-solid quick separating equipment being arranged in the first settler；Dense bed reactor passes through pre- carbon distribution
Catalyst transport pipeline is connected with the first settler, and the second gas-solid quick separating equipment, dense bed are equipped in the second settler
Reactor outlet connects the second riser reactor, and the second riser reactor is connected with the second gas-solid quick separating equipment；
Regenerator is connected by reclaimable catalyst feed-line with the second settler, and regenerator passes through regenerative agent feed-line and the
One riser reactor is connected.
Further, the bottom of first riser reactor is equipped with C4 and the above hydrocarbon charging mouth, methanol and C4 and with
Upper hydrocarbon mixed feeding, methanol charge proportion account for the 0-40% of C4 and the above hydrocarbon；Dense bed reactor bottom is equipped with the first material benzenemethanol
Feed inlet, dense bed reactor top are equipped with the second material benzenemethanol feed inlet.
Further, cyclone separator is respectively equipped in first settler, the second settler and regenerator；Described
One settler, the second settler and regenerator bottoms are respectively equipped with reclaimable catalyst air stripper, the second settler air stripper and again
Raw catalyst stripper.
Further, spent agent circulation pipe is equipped between the reclaimable catalyst air stripper and the first riser reactor
Line；Dense bed catalyst recycle line is equipped between the second settler air stripper and dense bed reactor.
Further, interior heat collector is arranged in second settler, and outside heat removing tank is arranged in regenerator.
Further, reactor product gas general pipeline, the regenerator are equipped at the top of first settler and the second settler
Top is equipped with regenerated flue gas pipeline.
The present invention also provides a kind of methods of methanol Efficient Conversion producing light olefins, characterized in that the following steps are included:
(1) C4 and the above hydrocarbon raw material enter the first riser reactor and catalyst haptoreaction, the gas-phase product of generation and
Catalyst carries out gas-solid in the first settler and mutually separates, and gas-phase product is directly entered separation system after separation；
(2) solid-phase catalyst a part after carbon distribution enters dense bed reactor by pre- carbon deposition catalyst feed-line, with raw material
Methanol reaction, the first riser reactor is returned in another part self-loopa, and the reaction was continued；
(3) dense bed reactor is connected with the second riser reactor, and catalyst enters second after dense bed reacts and promoted
The reaction was continued with methanol for pipe reactor, and carbon deposition catalyst is separated in the second settler with gas-phase product, solid-phase catalyst
A part carries out self-loopa and returns dense bed reactor；Another part carbon deposition catalyst enters regeneration through reclaimable catalyst feed-line
Device is regenerated completely；
(4) regenerated catalyst enters the first riser reactor through regenerative agent feed-line completely and raw material C4 and the above hydrocarbon are anti-
It answers.
Further, the catalyst is molecular sieve catalyst containing SAPO-34.
Further, the first riser reactor reaction condition are as follows: reaction temperature 500-600oC, reaction pressure
0.01-0.3MPa, gas phase 3 ~ 10m/s of linear velocity, carbon deposition quantity of catalyst 1-3%；Dense bed reactor reaction temperature 400-500oC,
Reaction pressure 0.01-0.3MPa, gas phase 2 ~ 4m/s of linear velocity, carbon deposition quantity of catalyst 3-10%；Second riser reactor reaction temperature
Spend 400-500oC, reaction pressure 0.01-0.3MPa, gas phase linear velocity 4-12m/s, carbon deposition quantity of catalyst 6-12%.
Further, the regenerator is the complete regeneration reactor of dense bed, and regenerated catalyst is averaged carbon distribution as 0-
0.5%, regeneration used medium is air.
Advantageous effects of the invention:
(1) C4 and the above component are handled by setting riser reactor, carbon distribution rear catalyst is by settler separate rear part point
It is recycled back to riser reactor, continues to convert C4 and the above component, can effectively be solved at C4 by adjusting catalyst circulation amount
Reason measures low problem；
(2) same catalyst is used, the catalyst after carbon distribution enters main reaction system, continues to participate in methanol to olefins reaction, greatly
Width improves the selectivity of reaction for preparing light olefins from methanol and the utilization rate of catalyst.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram of the device of methanol Efficient Conversion producing light olefins of the present invention.
Fig. 2 is the structural schematic diagram of comparative example 1.
The meaning of each main appended drawing reference in figure are as follows:
1.C4 and the above hydrocarbon charging mouth, 2. spent agent pipeloops, 3. first riser reactors, 4. reclaimable catalyst air lifts
Device, 5. first settlers, 6. first cyclone separators, 7.C4 reaction oil gas, 8. pre- carbon deposition catalyst feed-lines, 9. first gas
Gu quick separating equipment, 10. reactor product gas general pipeline, 11. regenerated flue gas pipelines, 12. first material benzenemethanol feed inlets, 13. is close
Phase bed reactor, 14. dense bed catalyst recycle lines, 15. second settler air stripper, 16. second material benzenemethanol feed inlets,
17. the second riser reactor, 18. second settlers, 19. second cyclone separators, 20. second gas-solid quick separating equipment,
21. reclaimable catalyst feed-line, 22. regenerated catalyst air stripper, 23. regeneration airs, 24. outside heat removing tanks, 25. regenerators,
26. third cyclone separator, 27. regenerative agent feed-lines.
Specific embodiment
The invention will be further described below in conjunction with the accompanying drawings.Following embodiment is only used for clearly illustrating the present invention
Technical solution, and not intended to limit the protection scope of the present invention.
As shown in Figure 1, a kind of device of methanol Efficient Conversion producing light olefins, including the first riser reactor 3, close phase
Fluidized-bed reactor 13, the second riser reactor 17 and regenerator 25；First riser reactor 3 is with setting in the first sedimentation
The first gas-solid quick separating equipment 9 in device 5 is connected；Dense bed reactor 13 by pre- carbon deposition catalyst feed-line 8 with
First settler 5 is connected, and the second gas-solid quick separating equipment 20 is equipped in the second settler 18, and dense bed reactor 13 exports
The second riser reactor 17 is connected, the second riser reactor 17 is connected with the second gas-solid quick separating equipment 20；Regeneration
Device 25 is connected by reclaimable catalyst feed-line 21 with the second settler 18, and regenerator 25 passes through regenerative agent feed-line
27 are connected with the first riser reactor 3.
The first cyclone separator 6, second is respectively equipped in first settler 5, the second settler 18 and regenerator 25
Cyclone separator 19 and third cyclone separator 26；First settler 5, the second settler 18 and 25 bottom of regenerator difference
Equipped with reclaimable catalyst air stripper 4, the second settler air stripper 15 and regenerated catalyst air stripper 22.
Spent agent pipeloop 2 is equipped between the reclaimable catalyst air stripper 4 and the first riser reactor 3；It is described
Dense bed catalyst recycle line 14 is equipped between second settler air stripper 15 and dense bed reactor 13.First sedimentation
It is equipped with reactor product gas general pipeline 10 at the top of device 5 and the second settler 18, is equipped with regenerated flue gas pipeline 11 at the top of the regenerator 25.
The bottom of first riser reactor 3 is equipped with C4 and the above hydrocarbon charging mouth 1, methanol are mixed with C4 and the above hydrocarbon
Charging, methanol charge proportion account for the 0-40% of C4 and the above hydrocarbon；13 bottom of dense bed reactor is equipped with the first material benzenemethanol feed inlet
12,13 top of dense bed reactor is equipped with the second material benzenemethanol feed inlet 16.Interior heat collector is arranged in second settler 18, takes
Thermal medium can be to preheating material or water.Outside heat removing tank 24 is arranged in regenerator 25, removes the heat that generation is burnt in regeneration.Regeneration
Device 25 is the complete regeneration reactor of dense bed, and regenerated catalyst is averaged carbon distribution as 0-0.5%, and regeneration used medium is air.
The present invention also provides a kind of methods of methanol Efficient Conversion producing light olefins, comprising the following steps:
(1) C4 and the above hydrocarbon raw material enter the first riser reactor 3 with from regenerator 25 regenerated catalyst and from
Recycling catalyst haptoreaction, the catalyst are molecular sieve catalyst containing SAPO-34, and the gas-phase product and catalyst of generation exist
It carries out gas-solid through the first gas-solid phase quick separating equipment 9 in first settler 5 mutually to separate, gas-phase product is through the first whirlwind after separation
A small amount of catalyst of the separation entrainment of separator 6 enters reactor product gas main pipe line 10 to back segment separation system；
(2) solid-phase catalyst a part after carbon distribution enters dense bed reactor 13 by pre- carbon deposition catalyst feed-line 8, with original
Expect methanol reaction, the reaction was continued through first riser reactor 3 of the return of catalyst recycle line 2 for another part self-loopa；
(3) dense bed reactor 13 is connected with the second riser reactor 17, and catalyst enters the after the reaction of dense bed 13
The reaction was continued with methanol for two riser reactors 17, and carbon deposition catalyst and gas-phase product pass through the second gas in the second settler 18
Gu quick disconnector 20 is separated, then a small amount of catalyst through the separation product gas entrainment of the second cyclone separator 19, gas phase produce
Object enters reactor product gas main pipe line 10, and solid-phase catalyst a part carries out self-loopa time dense bed reactor 13, and the reaction was continued；
Another part carbon deposition catalyst is regenerated through reclaimable catalyst feed-line 21 into regenerator 25 completely；
(4) regenerated catalyst completely is through first riser reactor of the return of regenerative agent feed-line 27 3 and raw material C4 and the above hydrocarbon
Reaction.
First riser reactor, 3 reaction condition are as follows: reaction temperature 500-600oC, reaction pressure 0.01-
0.3MPa, gas phase 3 ~ 10m/s of linear velocity, carbon deposition quantity of catalyst 1-3%；13 reaction temperature 400-500 of dense bed reactoroC, instead
Answer pressure 0.01-0.3MPa, gas phase 2 ~ 4m/s of linear velocity, carbon deposition quantity of catalyst 3-10%；Second riser reactor 17 reacts temperature
Spend 400-500oC, reaction pressure 0.01-0.3MPa, gas phase linear velocity 4-12m/s, carbon deposition quantity of catalyst 6-12%.
Embodiment 1
Reaction unit as shown in Figure 1, dense bed reactor reaction temperature 475oC, reaction pressure (with pressure gauge) are
0.25MPa, gas linear velocity 3m/s, carbon deposition quantity of catalyst 7%；First riser reactor reaction temperature 550oC, reaction pressure
(with pressure gauge) is 0.25MPa, gas linear velocity 5m/s, carbon deposition quantity of catalyst 3%；Second riser reactor reaction temperature
475oC, reaction pressure (with pressure gauge) are 0.25MPa, gas linear velocity 6m/s, carbon deposition quantity of catalyst 8%.First riser
Reactor feed is mixing C4 component, and olefin(e) centent 93wt% is free of methanol；Dense bed reactor feed is methanol, inlet amount
5kg/h；Regenerated catalyst carbon distribution is 0.3wt%；Pre- carbon deposition catalyst and the second riser from the first riser reactor are anti-
Agent mouth is returned by dense bed reactor lower part after answering the self-loopa catalyst of device to mix and enters dense bed reactor.Reaction product uses
Online gas chromatographic analysis, ethylene add propene yield 82.4wt%, and low-carbon alkene (ethylene, propylene and C4) yield reaches
92.7wt%。
Comparative example 1
Reaction unit as shown in Figure 2 is not provided with the first riser reactor, and freshening is not handled for C4 and the above component, and dense bed is anti-
Answer temperature 475oC, reaction pressure (with pressure gauge) are 0.25MPa, gas linear velocity 3m/s, carbon deposition quantity of catalyst 7%；Second
Riser reactor reaction temperature 475oC, reaction pressure (with pressure gauge) are 0.25MPa, gas linear velocity 6m/s, catalyst
Carbon deposition quantity 8%.Dense bed reactor feed is methanol, inlet amount 5kg/h；Regenerated catalyst carbon distribution is 0.3wt%；Second riser
The self-loopa catalyst of reactor returns agent mouth by dense bed reactor lower part and enters dense bed reactor.Reaction product is using online
Gas chromatographic analysis, ethylene add propene yield 80.3wt%, and low-carbon alkene (ethylene, propylene and C4) yield reaches 90.5wt%.
The present invention handles C4 and the above component by setting riser reactor, and carbon distribution rear catalyst is separated by settler
It is partially recycled back to riser reactor afterwards, continues to convert C4 and the above component, can effectively be solved by adjusting catalyst circulation amount
The certainly low problem of C4 treating capacity；Using same catalyst, the catalyst after carbon distribution enters main reaction system, continues to participate in methanol system
The selectivity of reaction for preparing light olefins from methanol and the utilization rate of catalyst greatly improved in olefine reaction.
The above is only a preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, without departing from the technical principles of the invention, several improvement and deformations can also be made, these improvement and deformations
Also it should be regarded as protection scope of the present invention.
Claims (10)
1. a kind of device of methanol Efficient Conversion producing light olefins, characterized in that including the first riser reactor (3), close phase
Fluidized-bed reactor (13), the second riser reactor (17) and regenerator (25)；First riser reactor (3) and setting exist
The first gas-solid quick separating equipment (9) in first settler (5) is connected；Dense bed reactor (13) is catalyzed by pre- carbon distribution
Agent feed-line (8) is connected with the first settler (5), and the second gas-solid quick separating equipment is equipped in the second settler (18)
(20), dense bed reactor (13) outlet connection the second riser reactor (17), the second riser reactor (17) and second
Gas-solid quick separating equipment (20) is connected；Regenerator (25) passes through reclaimable catalyst feed-line (21) and the second settler
(18) it is connected, and regenerator (25) is connected by regenerative agent feed-line (27) with the first riser reactor (3).
2. a kind of device of methanol Efficient Conversion producing light olefins according to claim 1, characterized in that described first mentions
The bottom of riser reactors (3) is equipped with C4 and the above hydrocarbon charging mouth (1), methanol and C4 and the above hydrocarbon mixed feeding, methanol charging
Ratio accounts for the 0-40% of C4 and the above hydrocarbon；Dense bed reactor (13) bottom is equipped with the first material benzenemethanol feed inlet (12), dense bed
Reactor (13) top is equipped with the second material benzenemethanol feed inlet (16).
3. a kind of device of methanol Efficient Conversion producing light olefins according to claim 1, characterized in that described first is heavy
Cyclone separator is respectively equipped in drop device (5), the second settler (18) and regenerator (25)；First settler (5), second
Settler (18) and regenerator (25) bottom be respectively equipped with reclaimable catalyst air stripper (4), the second settler air stripper (15) and
Regenerated catalyst air stripper (22).
4. a kind of device of methanol Efficient Conversion producing light olefins according to claim 3, characterized in that described to be generated to urge
Spent agent pipeloop (2) are equipped between agent air stripper (4) and the first riser reactor (3)；The second settler gas
It mentions and is equipped with dense bed catalyst recycle line (14) between device (15) and dense bed reactor (13).
5. a kind of device of methanol Efficient Conversion producing light olefins according to claim 1, characterized in that described second is heavy
It drops device (18) and interior heat collector is set, outside heat removing tank (24) are arranged in regenerator (25).
6. a kind of device of methanol Efficient Conversion producing light olefins according to claim 1, characterized in that described first is heavy
It drops and is equipped with reactor product gas general pipeline (10) at the top of device (5) and the second settler (18), regeneration is equipped at the top of the regenerator (25)
Flue gas pipeline (11).
7. a kind of method of methanol Efficient Conversion producing light olefins, characterized in that the following steps are included:
(1) C4 and the above hydrocarbon raw material enter the first riser reactor (3) and catalyst haptoreaction, the gas-phase product of generation
Gas-solid is carried out in the first settler (5) with catalyst mutually to separate, gas-phase product is directly entered separation system after separation；
(2) solid-phase catalyst a part after carbon distribution enters dense bed reactor (13) by pre- carbon deposition catalyst feed-line (8),
It is reacted with material benzenemethanol, the first riser reactor (3) are gone back in another part self-loopa, and the reaction was continued；
(3) dense bed reactor (13) is connected with the second riser reactor (17), and catalyst is after dense bed (13) are reacted
Into the second riser reactor (17), the reaction was continued with methanol, and carbon deposition catalyst and gas-phase product are in the second settler (18)
It is separated, solid-phase catalyst a part carries out self-loopa and goes back to dense bed reactor (13)；Another part carbon deposition catalyst pass through to
Raw catalyst transport pipeline (21) enter regenerator (25) and are regenerated completely；
(4) completely regenerated catalyst through regenerative agent feed-line (27) enter the first riser reactor (3) and raw material C4 and with
Upper hydrocarbon reaction.
8. a kind of method of methanol Efficient Conversion producing light olefins according to claim 7, characterized in that the catalyst
For molecular sieve catalyst containing SAPO-34.
9. a kind of method of methanol Efficient Conversion producing light olefins according to claim 7, characterized in that described first mentions
Riser reactors (3) reaction condition are as follows: reaction temperature 500-600oC, reaction pressure 0.01-0.3MPa, gas phase linear velocity 3 ~
10m/s, carbon deposition quantity of catalyst 1-3%；Dense bed reactor (13) reaction temperature 400-500oC, reaction pressure 0.01-0.3MPa,
Gas phase 2 ~ 4m/s of linear velocity, carbon deposition quantity of catalyst 3-10%；Second riser reactor (17) reaction temperature 400-500oC, reaction
Pressure 0.01-0.3MPa, gas phase linear velocity 4-12m/s, carbon deposition quantity of catalyst 6-12%.
10. a kind of method of methanol Efficient Conversion producing light olefins according to claim 7, characterized in that the regeneration
Device (25) is the complete regeneration reactor of dense bed, and regenerated catalyst is averaged carbon distribution as 0-0.5%, and regeneration used medium is air.
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| CN111944558A (en) * | 2020-08-23 | 2020-11-17 | 浙江工业大学 | Reaction regeneration circulating device system in catalytic cracking |
| CN113087584A (en) * | 2021-03-15 | 2021-07-09 | 中石化洛阳工程有限公司 | Method for producing low-carbon olefin by using oxygen-containing compound |
| CN113354496A (en) * | 2021-03-15 | 2021-09-07 | 中石化洛阳工程有限公司 | Device for producing low-carbon olefin by using oxygen-containing compound |
| CN113509957A (en) * | 2021-07-12 | 2021-10-19 | 南开大学 | Method for improving cycle stability and service life of catalyst for methanol-to-olefin reaction |
| CN113509893A (en) * | 2021-03-15 | 2021-10-19 | 中石化洛阳工程有限公司 | Method for producing low-carbon olefin by using efficient oxygen-containing compound |
| CN113509897A (en) * | 2021-03-15 | 2021-10-19 | 中石化洛阳工程有限公司 | Device of low carbon olefin of high efficiency oxygen compound production |
| CN114177840A (en) * | 2020-09-15 | 2022-03-15 | 中国石油化工股份有限公司 | Reaction system and method for preparing ethylene propylene |
| WO2024187677A1 (en) * | 2023-03-10 | 2024-09-19 | 润和催化剂股份有限公司 | Methanol-to-olefin method using fluidized bed, reactor, and process system |
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| CN113509957A (en) * | 2021-07-12 | 2021-10-19 | 南开大学 | Method for improving cycle stability and service life of catalyst for methanol-to-olefin reaction |
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