Fluidized bed gas distributor, reactor using fluidized bed gas distributor, and method for producing para-xylene and co-producing light olefins

Patent metadata

Field	Value
Publication number	US-10967350-B2
Application number	US-201716608816-A
Country	US
Kind code	B2
Filing date	Nov 24, 2017
Priority date	Apr 27, 2017
Publication date	Apr 6, 2021
Grant date	Apr 6, 2021

Abstract

Disclosed are a fluidized bed gas distributor and a fluidized bed reactor, the fluidized bed reactor comprising a first distributor (1) and a second distributor (2), wherein the first distributor (1) is located at the bottom of a fluidized bed, and second distributor (2) is located downstream of a gas from the first distributor (1). Also disclosed is a method for producing a para-xylene and co-producing light olefins, the method comprising the following steps: material stream A enters a reaction zone (3) of a fluidized bed reactor from a first gas distributor (1); material stream B enters the reaction zone (3) of the fluidized bed reactor from a second gas distributor (2); and the reactants are brought into contact with a catalyst in the reaction zone (3) to generate a gas phase stream comprising para-xylene and light olefins.

First claim

What is claimed is:

1. A fluidized bed gas distributor, comprising a first distributor and a second distributor, wherein the first distributor is located at the bottom of the fluidized bed, and the second distributor is located in at least one region of the gas flow downstream from the first distributor;
wherein, the second distributor comprises an intake pipe, a microporous pipe and an intake ring pipe;
wherein one end of the microporous pipe is connected with the intake ring pipe, and the other end is closed; and
wherein the side and end faces of the microporous pipe have a uniform microporous structure.

2. The fluidized bed gas distributor of claim 1 , wherein,
the intake pipe is connected with the microporous pipe, the gas is introduced by the intake pipe from the outside of the fluidized bed into the microporous pipe in the fluidized bed;
the intake ring pipe is connected with the intake pipe, the intake ring pipe is disposed on a plane perpendicular to the flow direction of the gas from the first distributor;
the microporous pipe is disposed on the intake ring pipe and perpendicular to a plane of the intake ring pipe.

3. The fluidized bed gas distributor of claim 1 , wherein material stream A enters the fluidized bed through the first distributor, material stream B enters the fluidized bed through the second distributor and contacts with at least a portion of the gas of the material stream A.

4. The fluidized bed gas distributor of claim 1 , wherein the first distributor is a two-dimensional gas distributor and the first distributor distributes the gas on the plane in which the first distributor is located at the bottom of the fluidized bed.

5. The fluidized bed gas distributor of claim 1 , wherein the second distributor is a three-dimensional gas distributor and the second distributor distributes the gas in at least a portion of the reaction space in which the second distributor is located in the fluidized bed.

6. The fluidized bed gas distributor of claim 1 , wherein the first distributor is a branched pipe distributor and/or a plate distributor with blast caps.

7. The fluidized bed gas distributor of claim 1 , wherein the microporous pipe is a ceramic microporous pipe and/or a metal microporous sintered pipe.

8. The fluidized bed gas distributor of claim 1 , wherein the side and end faces of the microporous pipe have micropores with a pore diameter ranging from 0.5 μm to 50 μm and a porosity ranging from 25% to 50%, the gas velocity in the pipe of the microporous pipe is in a range from 0.1 m/s to 10 m/s.

9. The fluidized bed gas distributor of claim 1 , wherein the fluidized bed gas distributor comprises a plurality of microporous pipes comprising the microporous pipe and a plurality of intake ring pipes comprising the intake ring pipe, and wherein the plurality of microporous pipes are arranged in parallel with each other, and the plurality of intake ring pipes are arranged in a concentric ring or planar spiral in the same plane.

10. A fluidized bed reactor, comprising the fluidized bed gas distributor according to claim 1 .

11. The fluidized bed reactor of claim 10 , wherein the fluidized bed reactor comprises a reaction zone, a settling zone, a gas-solid separator, a stripping zone and a regenerated catalyst delivery pipe;
the first distributor is placed at the bottom of the reaction zone, the second distributor is placed above the first distributor, the settling zone is above the reaction zone, the settling zone is provided with the gas-solid separator, the stripping zone is below the reaction zone, and the regenerated catalyst delivery pipe is connected with the reaction zone.

12. A method for producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, wherein at least one of the fluidized bed gas distributors according to claim 1 is used; the method for producing para-xylene and co-producing light olefins comprises at least the following steps:
(1) passing the material stream A from the first distributor into the reaction zone of the fluidized bed reactor, the reaction zone containing a catalyst; the material stream A containing toluene, or the material stream A containing methanol and/or dimethyl ether and toluene;
(2) passing the material stream B containing methanol and/or dimethyl ether from the second distributor into the reaction zone of the fluidized bed reactor;
(3) in the reaction zone, contacting methanol and/or dimethyl ether and toluene from the material stream A and/or the material stream B, with the catalyst to form material stream C comprising para-xylene and light olefins.

13. The method of claim 12 , wherein the method for producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene further comprises the following steps:
(4) passing the material stream C into a settling zone and a gas-solid separator to separate the material stream C to obtain light olefins, para-xylene, chain hydrocarbon by-products, aromatic by-products and unconverted toluene, unconverted methanol and/or dimethyl ether;
(5) returning unconverted methanol and/or dimethyl ether to the fluidized bed reactor via the second distributor; returning the aromatic by-products and unconverted toluene to the fluidized bed reactor via the first distributor;
(6) forming a spent catalyst from the catalyst after carbon deposition in the reaction zone, the spent catalyst is then stripped in a stripper and regenerated, in a regenerator to obtain a regenerated catalyst; passing the regenerated catalyst into the fluidized bed reactor via a regenerated catalyst delivery pipe;
preferably, the mass ratio of methanol and/or dimethyl ether in material stream B to methanol and/or dimethyl ether in material stream A is in a range from 1:1 to 10:1.

14. The method of claim 12 , wherein the sum of the mass percentages of methanol and dimethyl ether in material stream A is in a range from 0% to 30%.

15. The method of claim 13 , wherein the fluidized bed reactor has a gas phase linear velocity ranging from 0.2 m/s to 2 m/s and a reaction temperature ranging from 300° C. to 600° C.;
preferably, the regenerator has a gas phase linear velocity ranging from 0.2 m/s to 2 m/s and a regeneration temperature ranging from 500° C. to 800° C.

16. A method for producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, wherein at least one of the fluidized bed reactors according to claim 10 is used; the method for producing para-xylene and co-producing light olefins comprises at least the following steps:
(1) passing the material stream A from the first distributor into the reaction zone of the fluidized bed reactor, the reaction zone containing a catalyst; the material stream A containing toluene, or the material stream A containing methanol and/or dimethyl ether and toluene;
(2) passing the material stream B containing methanol and/or dimethyl ether from the second distributor into the reaction zone of the fluidized bed reactor;
(3) in the reaction zone, contacting methanol and/or dimethyl ether and toluene from the material stream A and/or the material stream B, with the catalyst to form material stream C comprising para-xylene and light olefins.

17. The method of claim 16 , wherein the method for producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene further comprises the following steps:
(4) passing the material stream C into a settling zone and a gas-solid separator to separate the material stream C to obtain light olefins, para

Assignees

• Dalian Inst Chem & Physics Cas

Inventors

• Zhang Tao
• Ye Mao
• Jia Jinming
• Liu Zhongmin
• Zhang Jinling
• Tang Hailong
• He Changqing
• Wang Xiangao
• Zhang Cheng
• Li Hua
• Zhao Yinfeng
• Li Chenggong

Classifications

• B01J2208/00938

  Flow distribution elements · CPC title

• B01J2208/00902

  Nozzle-type feeding elements · CPC title

• B01J2208/00893

  Feeding means for the reactants · CPC title

• B01J2208/00752

  Feeding · CPC title

• B01J8/1872 Primary

  Details of the fluidised bed reactor (B01J8/1836 takes precedence) · CPC title