METHOD AND DEVICE FOR MANUFACTURING PROPENE AND C4 HYDROCARBON

• US 20190263730A1
• Filed: 10/19/2016
• Published: 08/29/2019
• Est. Priority Date: 10/19/2016
• Status: Active Grant

• Current Assignee: Dalian Institute of Chemical Physics Chinese Academy of Sciences (Chinese Academy of Sciences)
• Original Assignee: Dalian Institute of Chemical Physics Chinese Academy of Sciences (Chinese Academy of Sciences)
• Inventors: ZHANG, Tao, YE, Mao, HE, Changqing, ZHANG, Jinling, WANG, Xiangao, TANG, Hailong, JIA, Jinming, ZHAO, Yinfeng, LIU, Zhongmin
• Granted Patent: US 10,640,433 B2
• Time in Patent Office: Days
• CPC Class Codes: B01D 45/12 by centrifugal forces centrifuges B04B; cyclones B04C
• CPC Class Codes: B01J 29/90 Regeneration or reactivation
• CPC Class Codes: B01J 38/30 in gaseous suspension, e.g. fluidised bed
• CPC Class Codes: B01J 38/32 Indirectly heating or cooling material within regeneration zone or prior to entry into regeneration zone
• CPC Class Codes: B01J 8/00 Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
• CPC Class Codes: B01J 8/1827 the fluidising gas being a reactant
• CPC Class Codes: B01J 8/1863 followed by a downward movement outside the reactor and subsequently re-entering it
• CPC Class Codes: B01J 8/26 with two or more fluidised beds, e.g. reactor and regeneration installations
• CPC Class Codes: B01J 8/388 externally, i.e. the particles leaving the vessel and subsequently re-entering it
• CPC Class Codes: C07C 1/20 starting from organic compounds containing only oxygen atoms as heteroatoms
• CPC Class Codes: C07C 11/04 Ethylene
• CPC Class Codes: C07C 11/06 Propene
• CPC Class Codes: C07C 11/08 with four carbon atoms
• CPC Class Codes: C07C 2/862 the non-hydrocarbon contains only oxygen as hetero-atoms
• CPC Class Codes: C07C 2529/85 Silicoaluminophosphates (SAPO compounds)
• CPC Class Codes: C07C 4/06 Catalytic processes C07C4/025 takes precedence
• CPC Class Codes: C07C 9/10 with four carbon atoms
• CPC Class Codes: Y02P 20/52 using catalysts, e.g. selective catalysts
• CPC Class Codes: Y02P 20/584 Recycling of catalysts
• CPC Class Codes: Y02P 30/20 using bio-feedstock
• CPC Class Codes: Y02P 30/40 : Ethylene production

Abstract

A method and device for preparing propylene and C4 hydrocarbons from oxygen-containing compounds. The method includes returning 70 wt. % or more of the light fractions in the generated product to a dense phase zone of a fast fluidized-bed reactor from a reactor feed distributor at the bottom-most of the fast fluidized-bed reactor to react ethylene and the oxygen-containing compounds to perform an alkylation reaction in presence of a catalyst to produce products of propylene and the like, and circulating 80 wt. % or more of the hydrocarbons with 5 or more carbons into a catalytic cracking lift pipe to perform a cracking reaction to generate a product containing propylene and C4 hydrocarbons, which is subsequently fed into a dilute phase zone of the fast fluidized-bed reactor. The method and device of the present invention improve the reaction rate of ethylene alkylation, and the unit volume production capacity of reactor is high.

Claims

1-14. -14. (canceled)

15. A device for preparing propylene and C4 hydrocarbons from oxygen-containing compounds, comprising:

a fast fluidized-bed reactor, the fast fluidized-bed reactor comprises a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the fast fluidized-bed reactor is a dense phase zone, the upper part of the fast fluidized-bed reactor is a dilute phase zone, the n reactor feed distributors are disposed in the dense phase zone, the reactor heat extractor is disposed inside or outside the reactor shell, the first reactor gas-solid separator and the second reactor gas-solid separator are placed outside the reactor shell, the inlet of the first reactor gas-solid separator is connected to a regenerated catalyst lift pipe, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the dense phase zone, the gas outlet of the first reactor gas-solid separator is located in the dilute phase zone, the inlet of the second reactor gas-solid separator is located in the dilute phase zone, the catalyst outlet of the second reactor gas-solid separator is placed in the dense phase zone, the gas outlet of the second reactor gas-solid separator is connected to the product gas outlet, and the reactor stripper passes through the reactor shell from outside to inside at the bottom of the fast fluidized-bed reactor and is opened in the dense phase zone of the fast fluidized-bed reactor;

a catalytic cracking lift pipe, the bottom of the catalytic cracking lift pipe is connected to the outlet of a catalytic cracking inclined pipe and is provided with an inlet of hydrocarbons with 5 or more carbons, and the outlet of the catalytic cracking lift pipe is connected to the dilute phase zone of the fast fluidized-bed reactor; and

a fluidized-bed regenerator, the fluidized-bed regenerator comprises a regenerator shell, a regenerator feed distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper, wherein the lower part of the fluidized-bed regenerator is a regeneration zone, the upper part of the fluidized-bed regenerator is a settling zone, the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, the regenerator gas-solid separator is placed in the settling zone or outside the regenerator shell, the inlet of the regenerator gas-solid separator is disposed in the settling zone, the catalyst outlet of the regenerator gas-solid separator is disposed in the regeneration zone, the gas outlet of the regenerator gas-solid separator is connected to the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;

wherein, the bottom of the reactor stripper is provided with a reactor stripping gas inlet, the bottom of the reactor stripper is connected to the inlet of a inclined spent catalyst pipe, a spent catalyst sliding valve is arranged in the inclined spent catalyst pipe, the outlet of the inclined spent catalyst pipe is connected to the inlet of a spent catalyst lift pipe, the bottom of the spent catalyst lift pipe is provided with a spent catalyst lifting gas inlet, and the outlet of the spent catalyst lift pipe is connected to the settling zone of the fluidized-bed regenerator;

the bottom of the regenerator stripper is provided with a regenerator stripping gas inlet, the bottom of the regenerator stripper is connected to the inlet of a regenerated inclined pipe, a regenerated sliding valve is arranged in the regenerated inclined pipe, the outlet of the regenerated inclined pipe is connected to the inlet of the regenerated catalyst lift pipe, the bottom of the regenerated catalyst lift pipe is provided with a regenerated lift gas inlet, and the outlet of the regenerated catalyst lift pipe is connected to the inlet of the reactor gas-solid separator; and

the bottom of the regenerator stripper is further connected to the inlet of the catalytic cracking inclined pipe, and a catalytic cracking sliding valve is arranged in the catalytic cracking inclined pipe.

16. The device according to claim 15, wherein the one or more reactor feed distributors are disposed in the dense phase zone from bottom to top, and these are between 1 and 10 distributors.

17. The device according to claim 15, wherein the horizontal height of opening of the reactor stripper in the reactor shell is higher than 1/10 the height of the dense phase zone.

18. The device according to claim 15, wherein the catalytic cracking lift pipe and the fast fluidized-bed reactor share the second gas-solid separator.

19. The device according to claim 15, wherein the fluidized-bed regenerator is a turbulent fluidized-bed regenerator.

20. The device according to claim 15, wherein the first reactor gas-solid separator, the second reactor gas-solid separator and the regenerator gas-solid separator are cyclone separators.

21. A method for preparing propylene and C4 hydrocarbons from oxygen-containing compounds, comprising:

feeding a raw material containing an oxygen-containing compound from n reactor feed distributors to a dense phase zone of a fast fluidized-bed reactor, and contacting the raw material with a catalyst, to generate a stream containing propylene and C4 hydrocarbons product and a spent catalyst containing carbon;

regenerating the spent catalyst by a fluidized-bed regenerator to form a regenerated catalyst, wherein a part of the regenerated catalyst is fed to the bottom of the dense phase zone of the fast fluidized-bed reactor after being gas-solid separated by a reactor gas-solid separator 1, and another part of the regenerated catalyst is fed to a catalytic cracking lift pipe via a catalytic cracking inclined pipe;

sending the stream discharged from the fast fluidized-bed reactor containing propylene and C4 hydrocarbons product into a product separation system, obtaining propylene, C4 hydrocarbons, light fractions, propane and hydrocarbons with 5 or more carbons after separation, wherein the light fractions contain more than 90 wt % of ethylene and a small amount of methane, ethane, hydrogen, CO and CO₂, returning 70 wt. % or more of the light fractions to the dense phase zone of the fast fluidized-bed reactor from the reactor feed distributor at the bottom-most of the fast fluidized-bed reactor to react ethylene and the oxygen-containing compounds to perform an alkylation reaction in presence of the catalyst to produce a product containing propylene, and retrieving less than 30 wt. % of the light fractions as a by-product; and

feeding 80 wt. % or more of the hydrocarbons with 5 or more carbons coming from the product separation system into the catalytic cracking lift pipe via an inlet of hydrocarbons with 5 or more carbons, to contact cocurrent with the regenerated catalyst coming from the catalytic cracking inclined pipe to perform a cracking reaction to generate a stream containing propylene and C4 hydrocarbons and a carbon-containing catalyst, subsequently, feeding the stream containing propylene and C4 hydrocarbons and the carbon-containing catalyst into a dilute phase zone of the fast fluidized-bed reactor via the outlet of the catalytic cracking lift pipe, and retrieving less than 20 wt. % of the hydrocarbons with 5 or more carbons as a by-product.

22. The method according to claim 21, being carried out by using a device comprising:

a fast fluidized-bed reactor, the fast fluidized-bed reactor comprises a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the fast fluidized-bed reactor is a dense phase zone, the upper part of the fast fluidized-bed reactor is a dilute phase zone, the n reactor feed distributors are disposed in the dense phase zone, the reactor heat extractor is disposed inside or outside the reactor shell, the first reactor gas-solid separator and the second reactor gas-solid separator are placed outside the reactor shell, the inlet of the first reactor gas-solid separator is connected to a regenerated catalyst lift pipe, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the dense phase zone, the gas outlet of the first reactor gas-solid separator is located in the dilute phase zone, the inlet of the second reactor gas-solid separator is located in the dilute phase zone, the catalyst outlet of the second reactor gas-solid separator is placed in the dense phase zone, the gas outlet of the second reactor gas-solid separator is connected to the product gas outlet, and the reactor stripper passes through the reactor shell from outside to inside at the bottom of the fast fluidized-bed reactor and is opened in the dense phase zone of the fast fluidized-bed reactor;

a catalytic cracking lift pipe, the bottom of the catalytic cracking lift pipe is connected to the outlet of a catalytic cracking inclined pipe and is provided with an inlet of hydrocarbons with 5 or more carbons, and the outlet of the catalytic cracking lift pipe is connected to the dilute phase zone of the fast fluidized-bed reactor; and

a fluidized-bed regenerator, the fluidized-bed regenerator comprises a regenerator shell, a regenerator feed distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper, wherein the lower part of the fluidized-bed regenerator is a regeneration zone, the upper part of the fluidized-bed regenerator is a settling zone, the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, the regenerator gas-solid separator is placed in the settling zone or outside the regenerator shell, the inlet of the regenerator gas-solid separator is disposed in the settling zone, the catalyst outlet of the regenerator gas-solid separator is disposed in the regeneration zone, the gas outlet of the regenerator gas-solid separator is connected to the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;

wherein, the bottom of the reactor stripper is provided with a reactor stripping gas inlet, the bottom of the reactor stripper is connected to the inlet of a inclined spent catalyst pipe, a spent catalyst sliding valve is arranged in the inclined spent catalyst pipe, the outlet of the inclined spent catalyst pipe is connected to the inlet of a spent catalyst lift pipe, the bottom of the spent catalyst lift pipe is provided with a spent catalyst lifting gas inlet, and the outlet of the spent catalyst lift pipe is connected to the settling zone of the fluidized-bed regenerator;

the bottom of the regenerator stripper is provided with a regenerator stripping gas inlet, the bottom of the regenerator stripper is connected to the inlet of a regenerated inclined pipe, a regenerated sliding valve is arranged in the regenerated inclined pipe, the outlet of the regenerated inclined pipe is connected to the inlet of the regenerated catalyst lift pipe, the bottom of the regenerated catalyst lift pipe is provided with a regenerated lift gas inlet, and the outlet of the regenerated catalyst lift pipe is connected to the inlet of the reactor gas-solid separator;

the bottom of the regenerator stripper is further connected to the inlet of the catalytic cracking inclined pipe, and a catalytic cracking sliding valve is arranged in the catalytic cracking inclined pipe; and

the spent catalyst passes through the reactor stripper, the inclined spent catalyst pipe, the spent catalyst sliding valve and the spent catalyst lift pipe into the settling zone of the fluidized-bed regenerator;

a regeneration medium enters the regeneration zone of the fluidized-bed regenerator from the regenerator feed distributor, the regeneration medium reacts with the spent catalyst to perform calcination to produce a flue gas containing CO and CO₂ and the regenerated catalyst, and the flue gas is discharged after dust removal by the regenerator gas-solid separator;

a part of the regenerated catalyst passes through the regenerator stripper, the regenerated inclined pipe, the regenerated sliding valve and the regenerated catalyst lift pipe into the inlet of the first reactor gas-solid separator, and enters the bottom of the dense phase zone of the fast fluidized-bed reactor after gas-solid separation;

another part of the regenerated catalyst passes through the regenerator stripper, the catalytic cracking inclined pipe and the catalytic cracking sliding valve into the catalytic cracking lift pipe;

a reactor stripping gas enters the reactor stripper via the reactor stripping gas inlet and contacts countercurrent with the spent catalyst, and then enters the fast fluidized-bed reactor;

a spent catalyst lifting gas enters the spent catalyst lift pipe via the spent catalyst lifting gas inlet and contacts cocurrent with the spent catalyst, and then enters the settling zone of the fluidized-bed regenerator;

a regenerator stripping gas enters the regenerator stripper via the regenerator stripping gas inlet and contacts countercurrent with the regenerated catalyst, and then enters the fluidized-bed regenerator;

a regenerated lift gas enters the regenerated catalyst lift pipe via the regenerated lift gas inlet and contacts cocurrent with the regenerated catalyst, and then enters the inlet of the first reactor gas-solid separator.

23. The method according to claim 21, wherein the catalyst contains a SAPO molecular sieve.

24. The method according to claim 21, wherein the circulating amount of the light fractions is 5-40 wt. % of the feeding amount of the oxygen-containing compound.

25. The method according to claim 21, wherein the circulating amount of the hydrocarbons with 5 or more carbons is 2-20 wt. % of the feeding amount of the oxygen-containing compound.

26. The method according to claim 21, wherein the carbon content of the spent catalyst is 5-12 wt. %, and the carbon content of the regenerated catalyst is less than 2 wt. %.

27. The method according to claim 21, wherein the oxygen-containing compound is methanol and/or dimethyl ether;

and/or the regeneration medium is any one of air, oxygen-poor air or water vapor or a mixture thereof; and

/or the reactor stripping gas, the regenerator stripping gas, the spent catalyst lifting gas and the regenerated lift gas are water vapor or nitrogen.

28. The method according to claim 21, wherein the reaction conditions in the dense phase zone of the fast fluidized-bed reactor are:

the apparent linear velocity of gas is in a range from 1.0 m/s to 8.0 m/s, the reaction temperature is in a range from 300°

C. to 550°

C., the reaction pressure is in a range from 100 kPa to 500 kPa, and the bed density is in a range from 50 kg/m³ to 500 kg/m³; and

/or the reaction conditions in the catalytic cracking lift pipe are;

the apparent linear velocity of gas is in a range from 2.0 m/s to 10.0 m/s, the reaction temperature is in a range from 400°

C. to 750°

C., the reaction pressure is in a range from 100 kPa to 500 kPa, and the bed density is in a range from 30 kg/m³ to 300 kg/m³; and

/or the reaction conditions in the regeneration zone of the fluidized-bed regenerator are;

the apparent linear velocity of gas is in a range from 0.1 m/s to 2 m/s, the regeneration temperature is in a range from 500°

C. to 750°

C., the regeneration pressure is in a range from 100 kPa to 500 kPa, and the bed density is in a range from 200 kg/m³ to 1200 kg/m³.

29. The method according to claim 21, being carried out by using a device, comprising:

a fast fluidized-bed reactor, the fast fluidized-bed reactor comprises a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the fast fluidized-bed reactor is a dense phase zone, the upper part of the fast fluidized-bed reactor is a dilute phase zone, the n reactor feed distributors are disposed in the dense phase zone, the reactor heat extractor is disposed inside or outside the reactor shell, the first reactor gas-solid separator and the second reactor gas-solid separator are placed outside the reactor shell, the inlet of the first reactor gas-solid separator is connected to a regenerated catalyst lift pipe, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the dense phase zone, the gas outlet of the first reactor gas-solid separator is located in the dilute phase zone, the inlet of the second reactor gas-solid separator is located in the dilute phase zone, the catalyst outlet of the second reactor gas-solid separator is placed in the dense phase zone, the gas outlet of the second reactor gas-solid separator is connected to the product gas outlet, and the reactor stripper passes through the reactor shell from outside to inside at the bottom of the fast fluidized-bed reactor and is opened in the dense phase zone of the fast fluidized-bed reactor;

a catalytic cracking lift pipe, the bottom of the catalytic cracking lift pipe is connected to the outlet of a catalytic cracking inclined pipe and is provided with an inlet of hydrocarbons with 5 or more carbons, and the outlet of the catalytic cracking lift pipe is connected to the dilute phase zone of the fast fluidized-bed reactor; and

a fluidized-bed regenerator, the fluidized-bed regenerator comprises a regenerator shell, a regenerator feed distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper, wherein the lower part of the fluidized-bed regenerator is a regeneration zone, the upper part of the fluidized-bed regenerator is a settling zone, the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, the regenerator gas-solid separator is placed in the settling zone or outside the regenerator shell, the inlet of the regenerator gas-solid separator is disposed in the settling zone, the catalyst outlet of the regenerator gas-solid separator is disposed in the regeneration zone, the gas outlet of the regenerator gas-solid separator is connected to the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;

wherein, the bottom of the reactor stripper is provided with a reactor stripping gas inlet, the bottom of the reactor stripper is connected to the inlet of a inclined spent catalyst pipe, a spent catalyst sliding valve is arranged in the inclined spent catalyst pipe, the outlet of the inclined spent catalyst pipe is connected to the inlet of a spent catalyst lift pipe, the bottom of the spent catalyst lift pipe is provided with a spent catalyst lifting gas inlet, and the outlet of the spent catalyst lift pipe is connected to the settling zone of the fluidized-bed regenerator;

the bottom of the regenerator stripper is provided with a regenerator stripping gas inlet, the bottom of the regenerator stripper is connected to the inlet of a regenerated inclined pipe, a regenerated sliding valve is arranged in the regenerated inclined pipe, the outlet of the regenerated inclined pipe is connected to the inlet of the regenerated catalyst lift pipe, the bottom of the regenerated catalyst lift pipe is provided with a regenerated lift gas inlet, and the outlet of the regenerated catalyst lift pipe is connected to the inlet of the reactor gas-solid separator;

the bottom of the regenerator stripper is further connected to the inlet of the catalytic cracking inclined pipe, and a catalytic cracking sliding valve is arranged in the catalytic cracking inclined pipe;

the one or more reactor feed distributors are disposed in the dense phase zone from bottom to top, and these are between 1 and 10 distributors; and

the spent catalyst passes through the reactor stripper, the inclined spent catalyst pipe, the spent catalyst sliding valve and the spent catalyst lift pipe into the settling zone of the fluidized-bed regenerator;

a regeneration medium enters the regeneration zone of the fluidized-bed regenerator from the regenerator feed distributor, the regeneration medium reacts with the spent catalyst to perform calcination to produce a flue gas containing CO and CO₂ and the regenerated catalyst, and the flue gas is discharged after dust removal by the regenerator gas-solid separator;

a part of the regenerated catalyst passes through the regenerator stripper, the regenerated inclined pipe, the regenerated sliding valve and the regenerated catalyst lift pipe into the inlet of the first reactor gas-solid separator, and enters the bottom of the dense phase zone of the fast fluidized-bed reactor after gas-solid separation;

another part of the regenerated catalyst passes through the regenerator stripper, the catalytic cracking inclined pipe and the catalytic cracking sliding valve into the catalytic cracking lift pipe;

a reactor stripping gas enters the reactor stripper via the reactor stripping gas inlet and contacts countercurrent with the spent catalyst, and then enters the fast fluidized-bed reactor;

a spent catalyst lifting gas enters the spent catalyst lift pipe via the catalyst lifting gas inlet and contacts cocurrent with the spent catalyst, and then enters the settling zone of the fluidized-bed regenerator;

a regenerator stripping gas enters the regenerator stripper via the regenerator stripping gas inlet and contacts countercurrent with the regenerated catalyst, and then enters the fluidized-bed regenerator;

a regenerated lift gas enters the regenerated catalyst lift pipe via the regenerated lift gas inlet and contacts cocurrent with the regenerated catalyst, and then enters the inlet of the first reactor gas-solid separator.

30. The method according to claim 21, being carried out by using a device, comprising:

a fast fluidized-bed reactor, the fast fluidized-bed reactor comprises a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the fast fluidized-bed reactor is a dense phase zone, the upper part of the fast fluidized-bed reactor is a dilute phase zone, the n reactor feed distributors are disposed in the dense phase zone, the reactor heat extractor is disposed inside or outside the reactor shell, the first reactor gas-solid separator and the second reactor gas-solid separator are placed outside the reactor shell, the inlet of the first reactor gas-solid separator is connected to a regenerated catalyst lift pipe, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the dense phase zone, the gas outlet of the first reactor gas-solid separator is located in the dilute phase zone, the inlet of the second reactor gas-solid separator is located in the dilute phase zone, the catalyst outlet of the second reactor gas-solid separator is placed in the dense phase zone, the gas outlet of the second reactor gas-solid separator is connected to the product gas outlet, and the reactor stripper passes through the reactor shell from outside to inside at the bottom of the fast fluidized-bed reactor and is opened in the dense phase zone of the fast fluidized-bed reactor;

a catalytic cracking lift pipe, the bottom of the catalytic cracking lift pipe is connected to the outlet of a catalytic cracking inclined pipe and is provided with an inlet of hydrocarbons with 5 or more carbons, and the outlet of the catalytic cracking lift pipe is connected to the dilute phase zone of the fast fluidized-bed reactor; and

a fluidized-bed regenerator, the fluidized-bed regenerator comprises a regenerator shell, a regenerator feed distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper, wherein the lower part of the fluidized-bed regenerator is a regeneration zone, the upper part of the fluidized-bed regenerator is a settling zone, the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, the regenerator gas-solid separator is placed in the settling zone or outside the regenerator shell, the inlet of the regenerator gas-solid separator is disposed in the settling zone, the catalyst outlet of the regenerator gas-solid separator is disposed in the regeneration zone, the gas outlet of the regenerator gas-solid separator is connected to the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;

wherein, the bottom of the reactor stripper is provided with a reactor stripping gas inlet, the bottom of the reactor stripper is connected to the inlet of a inclined spent catalyst pipe, a spent catalyst sliding valve is arranged in the inclined spent catalyst pipe, the outlet of the inclined spent catalyst pipe is connected to the inlet of a spent catalyst lift pipe, the bottom of the spent catalyst lift pipe is provided with a spent catalyst lifting gas inlet, and the outlet of the spent catalyst lift pipe is connected to the settling zone of the fluidized-bed regenerator;

the bottom of the regenerator stripper is provided with a regenerator stripping gas inlet, the bottom of the regenerator stripper is connected to the inlet of a regenerated inclined pipe, a regenerated sliding valve is arranged in the regenerated inclined pipe, the outlet of the regenerated inclined pipe is connected to the inlet of the regenerated catalyst lift pipe, the bottom of the regenerated catalyst lift pipe is provided with a regenerated lift gas inlet, and the outlet of the regenerated catalyst lift pipe is connected to the inlet of the reactor gas-solid separator;

the bottom of the regenerator stripper is further connected to the inlet of the catalytic cracking inclined pipe, and a catalytic cracking sliding valve is arranged in the catalytic cracking inclined pipe;

the one or more reactor feed distributors are disposed in the dense phase zone from bottom to top, and these are between 1 and 10 distributors; and

the spent catalyst passes through the reactor stripper, the inclined spent catalyst pipe, the spent catalyst sliding valve and the spent catalyst lift pipe into the settling zone of the fluidized-bed regenerator;

a regeneration medium enters the regeneration zone of the fluidized-bed regenerator from the regenerator feed distributor, the regeneration medium reacts with the spent catalyst to perform calcination to produce a flue gas containing CO and CO₂ and the regenerated catalyst, and the flue gas is discharged after dust removal by the regenerator gas-solid separator;

a part of the regenerated catalyst passes through the regenerator stripper, the regenerated inclined pipe, the regenerated sliding valve and the regenerated catalyst lift pipe into the inlet of the first reactor gas-solid separator, and enters the bottom of the dense phase zone of the fast fluidized-bed reactor after gas-solid separation;

another part of the regenerated catalyst passes through the regenerator stripper, the catalytic cracking inclined pipe and the catalytic cracking sliding valve into the catalytic cracking lift pipe;

a reactor stripping gas enters the reactor stripper via the reactor stripping gas inlet and contacts countercurrent with the spent catalyst, and then enters the fast fluidized-bed reactor;

a spent catalyst lifting gas enters the spent catalyst lift pipe via the spent catalyst lifting gas inlet and contacts cocurrent with the spent catalyst, and then enters the settling zone of the fluidized-bed regenerator;

a regenerator stripping gas enters the regenerator stripper via the regenerator stripping gas inlet and contacts countercurrent with the regenerated catalyst, and then enters the fluidized-bed regenerator;

a regenerated lift gas enters the regenerated catalyst lift pipe via the regenerated lift gas inlet and contacts cocurrent with the regenerated catalyst, and then enters the inlet of the first reactor gas-solid separator.

31. The method according to claim 21, being carried out by using a device, comprising:

a fast fluidized-bed reactor, the fast fluidized-bed reactor comprises a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the fast fluidized-bed reactor is a dense phase zone, the upper part of the fast fluidized-bed reactor is a dilute phase zone, the n reactor feed distributors are disposed in the dense phase zone, the reactor heat extractor is disposed inside or outside the reactor shell, the first reactor gas-solid separator and the second reactor gas-solid separator are placed outside the reactor shell, the inlet of the first reactor gas-solid separator is connected to a regenerated catalyst lift pipe, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the dense phase zone, the gas outlet of the first reactor gas-solid separator is located in the dilute phase zone, the inlet of the second reactor gas-solid separator is located in the dilute phase zone, the catalyst outlet of the second reactor gas-solid separator is placed in the dense phase zone, the gas outlet of the second reactor gas-solid separator is connected to the product gas outlet, and the reactor stripper passes through the reactor shell from outside to inside at the bottom of the fast fluidized-bed reactor and is opened in the dense phase zone of the fast fluidized-bed reactor;

a catalytic cracking lift pipe, the bottom of the catalytic cracking lift pipe is connected to the outlet of a catalytic cracking inclined pipe and is provided with an inlet of hydrocarbons with 5 or more carbons, and the outlet of the catalytic cracking lift pipe is connected to the dilute phase zone of the fast fluidized-bed reactor; and

a fluidized-bed regenerator, the fluidized-bed regenerator comprises a regenerator shell, a regenerator feed distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper, wherein the lower part of the fluidized-bed regenerator is a regeneration zone, the upper part of the fluidized-bed regenerator is a settling zone, the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, the regenerator gas-solid separator is placed in the settling zone or outside the regenerator shell, the inlet of the regenerator gas-solid separator is disposed in the settling zone, the catalyst outlet of the regenerator gas-solid separator is disposed in the regeneration zone, the gas outlet of the regenerator gas-solid separator is connected to the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;

wherein, the bottom of the reactor stripper is provided with a reactor stripping gas inlet, the bottom of the reactor stripper is connected to the inlet of a inclined spent catalyst pipe, a spent catalyst sliding valve is arranged in the inclined spent catalyst pipe, the outlet of the inclined spent catalyst pipe is connected to the inlet of a spent catalyst lift pipe, the bottom of the spent catalyst lift pipe is provided with a spent catalyst lifting gas inlet, and the outlet of the spent catalyst lift pipe is connected to the settling zone of the fluidized-bed regenerator;

the bottom of the regenerator stripper is provided with a regenerator stripping gas inlet, the bottom of the regenerator stripper is connected to the inlet of a regenerated inclined pipe, a regenerated sliding valve is arranged in the regenerated inclined pipe, the outlet of the regenerated inclined pipe is connected to the inlet of the regenerated catalyst lift pipe, the bottom of the regenerated catalyst lift pipe is provided with a regenerated lift gas inlet, and the outlet of the regenerated catalyst lift pipe is connected to the inlet of the reactor gas-solid separator;

the bottom of the regenerator stripper is further connected to the inlet of the catalytic cracking inclined pipe, and a catalytic cracking sliding valve is arranged in the catalytic cracking inclined pipe;

the catalytic cracking lift pipe and the fast fluidized-bed reactor share the second gas-solid separator; and

the spent catalyst passes through the reactor stripper, the inclined spent catalyst pipe, the spent catalyst sliding valve and the spent catalyst lift pipe into the settling zone of the fluidized-bed regenerator;

a regeneration medium enters the regeneration zone of the fluidized-bed regenerator from the regenerator feed distributor, the regeneration medium reacts with the spent catalyst to perform calcination to produce a flue gas containing CO and CO₂ and the regenerated catalyst, and the flue gas is discharged after dust removal by the regenerator gas-solid separator;

a part of the regenerated catalyst passes through the regenerator stripper, the regenerated inclined pipe, the regenerated sliding valve and the regenerated catalyst lift pipe into the inlet of the first reactor gas-solid separator, and enters the bottom of the dense phase zone of the fast fluidized-bed reactor after gas-solid separation;

another part of the regenerated catalyst passes through the regenerator stripper, the catalytic cracking inclined pipe and the catalytic cracking sliding valve into the catalytic cracking lift pipe;

a reactor stripping gas enters the reactor stripper via the reactor stripping gas inlet and contacts countercurrent with the spent catalyst, and then enters the fast fluidized-bed reactor;

a spent catalyst lifting gas enters the spent catalyst lift pipe via the spent catalyst lifting gas inlet and contacts cocurrent with the spent catalyst, and then enters the settling zone of the fluidized-bed regenerator;

a regenerator stripping gas enters the regenerator stripper via the regenerator stripping gas inlet and contacts countercurrent with the regenerated catalyst, and then enters the fluidized-bed regenerator;

a regenerated lift gas enters the regenerated catalyst lift pipe via the regenerated lift gas inlet and contacts cocurrent with the regenerated catalyst, and then enters the inlet of the first reactor gas-solid separator.

32. The method according to claim 21, being carried out by using a device, comprising:

a fast fluidized-bed reactor, the fast fluidized-bed reactor comprises a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the fast fluidized-bed reactor is a dense phase zone, the upper part of the fast fluidized-bed reactor is a dilute phase zone, the n reactor feed distributors are disposed in the dense phase zone, the reactor heat extractor is disposed inside or outside the reactor shell, the first reactor gas-solid separator and the second reactor gas-solid separator are placed outside the reactor shell, the inlet of the first reactor gas-solid separator is connected to a regenerated catalyst lift pipe, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the dense phase zone, the gas outlet of the first reactor gas-solid separator is located in the dilute phase zone, the inlet of the second reactor gas-solid separator is located in the dilute phase zone, the catalyst outlet of the second reactor gas-solid separator is placed in the dense phase zone, the gas outlet of the second reactor gas-solid separator is connected to the product gas outlet, and the reactor stripper passes through the reactor shell from outside to inside at the bottom of the fast fluidized-bed reactor and is opened in the dense phase zone of the fast fluidized-bed reactor;

a catalytic cracking lift pipe, the bottom of the catalytic cracking lift pipe is connected to the outlet of a catalytic cracking inclined pipe and is provided with an inlet of hydrocarbons with 5 or more carbons, and the outlet of the catalytic cracking lift pipe is connected to the dilute phase zone of the fast fluidized-bed reactor; and

a fluidized-bed regenerator, the fluidized-bed regenerator comprises a regenerator shell, a regenerator feed distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper, wherein the lower part of the fluidized-bed regenerator is a regeneration zone, the upper part of the fluidized-bed regenerator is a settling zone, the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, the regenerator gas-solid separator is placed in the settling zone or outside the regenerator shell, the inlet of the regenerator gas-solid separator is disposed in the settling zone, the catalyst outlet of the regenerator gas-solid separator is disposed in the regeneration zone, the gas outlet of the regenerator gas-solid separator is connected to the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;

wherein, the bottom of the reactor stripper is provided with a reactor stripping gas inlet, the bottom of the reactor stripper is connected to the inlet of a inclined spent catalyst pipe, a spent catalyst sliding valve is arranged in the inclined spent catalyst pipe, the outlet of the inclined spent catalyst pipe is connected to the inlet of a spent catalyst lift pipe, the bottom of the spent catalyst lift pipe is provided with a spent catalyst lifting gas inlet, and the outlet of the spent catalyst lift pipe is connected to the settling zone of the fluidized-bed regenerator;

the bottom of the regenerator stripper is provided with a regenerator stripping gas inlet, the bottom of the regenerator stripper is connected to the inlet of a regenerated inclined pipe, a regenerated sliding valve is arranged in the regenerated inclined pipe, the outlet of the regenerated inclined pipe is connected to the inlet of the regenerated catalyst lift pipe, the bottom of the regenerated catalyst lift pipe is provided with a regenerated lift gas inlet, and the outlet of the regenerated catalyst lift pipe is connected to the inlet of the reactor gas-solid separator;

the bottom of the regenerator stripper is further connected to the inlet of the catalytic cracking inclined pipe, and a catalytic cracking sliding valve is arranged in the catalytic cracking inclined pipe;

the fluidized-bed regenerator is a turbulent fluidized-bed regenerator; and

the spent catalyst passes through the reactor stripper, the inclined spent catalyst pipe, the spent catalyst sliding valve and the spent catalyst lift pipe into the settling zone of the fluidized-bed regenerator;

a regeneration medium enters the regeneration zone of the fluidized-bed regenerator from the regenerator feed distributor, the regeneration medium reacts with the spent catalyst to perform calcination to produce a flue gas containing CO and CO₂ and the regenerated catalyst, and the flue gas is discharged after dust removal by the regenerator gas-solid separator;

a part of the regenerated catalyst passes through the regenerator stripper, the regenerated inclined pipe, the regenerated sliding valve and the regenerated catalyst lift pipe into the inlet of the first reactor gas-solid separator, and enters the bottom of the dense phase zone of the fast fluidized-bed reactor after gas-solid separation;

another part of the regenerated catalyst passes through the regenerator stripper, the catalytic cracking inclined pipe and the catalytic cracking sliding valve into the catalytic cracking lift pipe;

a reactor stripping gas enters the reactor stripper via the reactor stripping gas inlet and contacts countercurrent with the spent catalyst, and then enters the fast fluidized-bed reactor;

a spent catalyst lifting gas enters the spent catalyst lift pipe via the spent catalyst lifting gas inlet and contacts cocurrent with the spent catalyst, and then enters the settling zone of the fluidized-bed regenerator;

a regenerator stripping gas enters the regenerator stripper via the regenerator stripping gas inlet and contacts countercurrent with the regenerated catalyst, and then enters the fluidized-bed regenerator;

a regenerated lift gas enters the regenerated catalyst lift pipe via the regenerated lift gas inlet and contacts cocurrent with the regenerated catalyst, and then enters the inlet of the first reactor gas-solid separator.

33. The method according to claim 21, being carried out by using a device, comprising:

a fast fluidized-bed reactor, the fast fluidized-bed reactor comprises a reactor shell, one or more reactor feed distributors, a first reactor gas-solid separator, a second reactor gas-solid separator, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the fast fluidized-bed reactor is a dense phase zone, the upper part of the fast fluidized-bed reactor is a dilute phase zone, the n reactor feed distributors are disposed in the dense phase zone, the reactor heat extractor is disposed inside or outside the reactor shell, the first reactor gas-solid separator and the second reactor gas-solid separator are placed outside the reactor shell, the inlet of the first reactor gas-solid separator is connected to a regenerated catalyst lift pipe, the catalyst outlet of the first reactor gas-solid separator is located at the bottom of the dense phase zone, the gas outlet of the first reactor gas-solid separator is located in the dilute phase zone, the inlet of the second reactor gas-solid separator is located in the dilute phase zone, the catalyst outlet of the second reactor gas-solid separator is placed in the dense phase zone, the gas outlet of the second reactor gas-solid separator is connected to the product gas outlet, and the reactor stripper passes through the reactor shell from outside to inside at the bottom of the fast fluidized-bed reactor and is opened in the dense phase zone of the fast fluidized-bed reactor;

a catalytic cracking lift pipe, the bottom of the catalytic cracking lift pipe is connected to the outlet of a catalytic cracking inclined pipe and is provided with an inlet of hydrocarbons with 5 or more carbons, and the outlet of the catalytic cracking lift pipe is connected to the dilute phase zone of the fast fluidized-bed reactor; and

a fluidized-bed regenerator, the fluidized-bed regenerator comprises a regenerator shell, a regenerator feed distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper, wherein the lower part of the fluidized-bed regenerator is a regeneration zone, the upper part of the fluidized-bed regenerator is a settling zone, the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, the regenerator gas-solid separator is placed in the settling zone or outside the regenerator shell, the inlet of the regenerator gas-solid separator is disposed in the settling zone, the catalyst outlet of the regenerator gas-solid separator is disposed in the regeneration zone, the gas outlet of the regenerator gas-solid separator is connected to the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;

wherein, the bottom of the reactor stripper is provided with a reactor stripping gas inlet, the bottom of the reactor stripper is connected to the inlet of a inclined spent catalyst pipe, a spent catalyst sliding valve is arranged in the inclined spent catalyst pipe, the outlet of the inclined spent catalyst pipe is connected to the inlet of a spent catalyst lift pipe, the bottom of the spent catalyst lift pipe is provided with a spent catalyst lifting gas inlet, and the outlet of the spent catalyst lift pipe is connected to the settling zone of the fluidized-bed regenerator;

the bottom of the regenerator stripper is provided with a regenerator stripping gas inlet, the bottom of the regenerator stripper is connected to the inlet of a regenerated inclined pipe, a regenerated sliding valve is arranged in the regenerated inclined pipe, the outlet of the regenerated inclined pipe is connected to the inlet of the regenerated catalyst lift pipe, the bottom of the regenerated catalyst lift pipe is provided with a regenerated lift gas inlet, and the outlet of the regenerated catalyst lift pipe is connected to the inlet of the reactor gas-solid separator;

the bottom of the regenerator stripper is further connected to the inlet of the catalytic cracking inclined pipe, and a catalytic cracking sliding valve is arranged in the catalytic cracking inclined pipe;

the first reactor gas-solid separator, the second reactor gas-solid separator and the regenerator gas-solid separator are cyclone separators; and

the spent catalyst passes through the reactor stripper, the inclined spent catalyst pipe, the spent catalyst sliding valve and the spent catalyst lift pipe into the settling zone of the fluidized-bed regenerator;

a regeneration medium enters the regeneration zone of the fluidized-bed regenerator from the regenerator feed distributor, the regeneration medium reacts with the spent catalyst to perform calcination to produce a flue gas containing CO and CO₂ and the regenerated catalyst, and the flue gas is discharged after dust removal by the regenerator gas-solid separator;

a part of the regenerated catalyst passes through the regenerator stripper, the regenerated inclined pipe, the regenerated sliding valve and the regenerated catalyst lift pipe into the inlet of the first reactor gas-solid separator, and enters the bottom of the dense phase zone of the fast fluidized-bed reactor after gas-solid separation;

another part of the regenerated catalyst passes through the regenerator stripper, the catalytic cracking inclined pipe and the catalytic cracking sliding valve into the catalytic cracking lift pipe;

a reactor stripping gas enters the reactor stripper via the reactor stripping gas inlet and contacts countercurrent with the spent catalyst, and then enters the fast fluidized-bed reactor;

a spent catalyst lifting gas enters the spent catalyst lift pipe via the spent catalyst lifting gas inlet and contacts cocurrent with the spent catalyst, and then enters the settling zone of the fluidized-bed regenerator;

a regenerator stripping gas enters the regenerator stripper via the regenerator stripping gas inlet and contacts countercurrent with the regenerated catalyst, and then enters the fluidized-bed regenerator;

a regenerated lift gas enters the regenerated catalyst lift pipe via the regenerated lift gas inlet and contacts cocurrent with the regenerated catalyst, and then enters the inlet of the first reactor gas-solid separator.