Fluidized bed reactor and method for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether

Patent metadata

Field	Value
Publication number	US-11072571-B2
Application number	US-201716608444-A
Country	US
Kind code	B2
Filing date	Nov 24, 2017
Priority date	Apr 27, 2017
Publication date	Jul 27, 2021
Grant date	Jul 27, 2021

Abstract

A fluidized bed reactor for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether, including a first distributor and a second distributor. The first distributor is located at the bottom of the fluidized bed, and the second distributor is located at the downstream of the first distributor along a gas flow direction. Also, a method for producing para-xylene and co-producing light olefins, including the following steps: a material stream A enters a reaction zone of the fluidized bed reactor from the first gas distributor; a material stream B enters the reaction zone of the fluidized bed reactor from the second gas distributor; a reactant contacts a catalyst in the reaction zone to generate a gas phase stream comprising para-xylene and light olefins.

First claim

What is claimed is:

1. A fluidized bed reactor for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether, comprising a reaction zone, a first distributor, and a second distributor, wherein the first distributor is located at the bottom of the reaction zone of a fluidized bed, and the second distributor is placed above the first distributor,
wherein the second distributor comprises an intake pipe, a plurality of microporous pipes and a plurality of intake ring pipes,
the intake pipe is connected with a gas path of the microporous pipes, gas is introduced by the intake pipes from the outside of the fluidized bed into the microporous pipes in the fluidized bed;
the intake ring pipes are connected with a gas path of the intake pipe, the intake ring pipes are disposed on a plane perpendicular to the flow direction of the gas from the first distributor;
the microporous pipes are disposed on the intake ring pipes and perpendicular to a plane of the intake ring pipes,

wherein, side and end faces of the microporous pipes have a uniform microporous structure such that the gas is uniformly distributed in the three-dimensional space in which the second distributor is located; and
wherein, the fluidized bed reactor further comprises a regenerated catalyst delivery pipe which is connected with the bottom of the reaction zone.

2. The fluidized bed reactor 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 reaction zone of the fluidized bed.

3. The fluidized bed reactor of claim 1 , wherein the first distributor is a branched pipe distributor or a plate distributor with blast caps.

4. The fluidized bed reactor of claim 1 , wherein the microporous pipes are ceramic microporous pipes or powder metallurgical microporous pipes.

5. The fluidized bed reactor of claim 1 , wherein side and end faces of the microporous pipes have micropores with a pore diameter ranging from 0.5 μm to 50 μm and a porosity ranging from 25% to 50%.

6. The fluidized bed reactor of claim 1 , wherein the microporous pipes are arranged in parallel with each other; the intake ring pipes are arranged in a concentric ring or planar spiral in the same plane.

7. The fluidized bed reactor of claim 1 , wherein the fluidized bed reactor comprises a settling zone, a gas-solid separator, and a stripping zone;
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.

8. A method for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether, wherein a fluidized bed reactors comprising a reaction zone, a first distributor and a second distributor is used, wherein the first distributor is located at the bottom of the reaction zone of a fluidized bed, and the second distributor is placed above the first distributor;
wherein the second distributor comprises an intake pipe, a plurality of microporous pipes and a plurality of intake ring pipes,
the intake pipe is connected with a gas path of the microporous pipes, the gas is introduced by the intake pipe from the outside of the fluidized bed into the microporous pipes in the fluidized bed;
the intake ring pipes are connected with a gas path of the intake pipe, the intake ring pipes are disposed on a plane perpendicular to the flow direction of the gas from the first distributor;
the microporous pipes are disposed on the intake ring pipes and perpendicular to a plane of the intake ring pipes,
wherein, side and end faces of the microporous pipes have a uniform microporous structure such that gas is uniformly distributed in the three-dimensional space in which the second gas distributor is located;
wherein, the fluidized bed reactor further comprises a regenerated catalyst delivery pipe which is connected with the bottom of the reaction zone,

the method comprising:
(1) passing a 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 benzene, or the material stream A containing methanol and/or dimethyl ether and benzene;
(2) passing a material stream B containing methanol and/or dimethyl ether from the second distributor into the reaction zone of the fluidized bed reactor; and
(3) in the reaction zone, contacting methanol and/or dimethyl ether and benzene 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.

9. The method of claim 8 , wherein the method for producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene 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 benzene, 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 benzene to the fluidized bed reactor via the first distributor; and
(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 the regenerated catalyst delivery pipe.

10. The method of claim 8 , wherein 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 20:1.

11. The method of claim 8 , wherein, the material stream A contains benzene, but the material stream A entering from the first distributor does not contain methanol.

12. The method of claim 8 , wherein the material stream A contains methanol and dimethyl ether and benzene, and the sum of the mass percentages of methanol and dimethyl ether in material stream A entering from the first distributor is in a range from 2% to 20%.

13. The method of claim 8 , 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.

14. The method of claim 9 , wherein 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.

Assignees

• Dalian Inst Chem & Physics Cas

Inventors

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

Classifications

• B01J8/1872

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

• C07C2/64

  Addition to a carbon atom of a six-membered aromatic ring · CPC title

• C07C2529/40

  of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 · CPC title

• C07C2/865

  the non-hydrocarbon is an ether · CPC title

• C07C11/08

  with four carbon atoms · CPC title