Fluidized bed reactor, device and method for preparing low-carbon olefins from oxygen-containing compound

Patent metadata

Field	Value
Publication number	US-12286594-B2
Application number	US-202017784647-A
Country	US
Kind code	B2
Filing date	Oct 16, 2020
Priority date	Oct 16, 2020
Publication date	Apr 29, 2025
Grant date	Apr 29, 2025

Abstract

A fluidized bed reactor, a device, and a method for producing low-carbon olefins from oxygen-containing compound are provided. The fluidized bed reactor includes a reactor shell, a reaction zone, a coke control zone and a delivery pipe, where there are n baffles arranged in the coke control zone, and the n baffles divide the coke control zone into n sub-coke control zones which include a first sub-coke control zone, a second sub-coke control zone, and an nth sub-coke control zone; at least one catalyst circulation hole is provided on each of the n-1 baffles, so that the catalyst flows in an annular shape in the coke control zone, where n is an integer. The device and method can be adapted to a new generation of DMTO catalyst, and the unit consumption of production ranges from 2.50 to 2.58 tons of methanol/ton of low-carbon olefins.

First claim

What is claimed is:

1. A fluidized bed reactor, comprising a reactor shell, a reaction zone, a coke control zone, and a delivery pipe;
wherein the reactor shell comprises a lower shell and an upper shell, the lower shell encloses the reaction zone, the delivery pipe is disposed above the reaction zone and the delivery pipe is in communication with the reaction zone, an outer periphery of the delivery pipe is provided with the upper shell, the upper shell and the delivery pipe enclose to form a cavity comprising the coke control zone;
an upper part of the delivery pipe is provided with a gas outlet;
the reaction zone comprises a reaction raw material inlet and a coke controlled catalyst inlet;
the coke control zone comprises a catalyst inlet, a coke controlled catalyst outlet, a coke control gas outlet, and a coke control raw material inlet;
the coke control zone is an annular cavity;
n baffles are arranged in the coke control zone, and the n baffles divide the coke control zone into n sub-coke control zones, the n sub-coke control zones comprise a first sub-coke control zone, a second sub-coke control zone, and an nth sub-coke control zone;
at least one catalyst circulation hole is provided on each of n- 1 of the n baffles so that a catalyst flows in an annular shape in the coke control zone, wherein n is an integer; and
the catalyst inlet is arranged in the first sub-coke control zone, the coke controlled catalyst outlet is arranged in the nth sub-coke control zone, and the coke control gas outlet is arranged between two adjacent baffles of the n baffles.

2. The fluidized bed reactor according to claim 1 , wherein 2≤n≤10;
a cross section of the coke control zone is annular in shape, and a cross section of the sub-coke control zone is fan in shape;
the coke control gas outlet is connected to the delivery pipe by a coke control zone gas delivery pipe;
a coke control zone distributor is provided at a bottom of each of the n sub-coke control zones; the coke control raw material inlet is in communication with the coke control zone distributor, or the coke control raw material inlet is located below the coke control zone distributor;
a reaction zone distributor is arranged at the reaction raw material inlet, and the reaction zone distributor is arranged at a bottom of the reaction zone.

3. The fluidized bed reactor according to claim 1 , further comprising a spent catalyst zone, wherein the spent catalyst zone is arranged above the coke control zone and sleeved on the outer periphery of the delivery pipe, wherein a partition plate is provided between the spent catalyst zone and the coke control zone; and
a spent catalyst zone distributor is arranged at a bottom of the spent catalyst zone;
the spent catalyst zone comprises a heat extractor for the fluidized bed reactor;
the fluidized bed reactor further comprises a gas-solid separation zone, the gas-solid separation zone is arranged above the spent catalyst zone and the gas-solid separation zone is sleeved on the outer periphery of the delivery pipe; the gas-solid separation zone is provided with a gas-solid separation device; and the spent catalyst zone is in communication with the gas-solid separation zone;
the gas-solid separation device comprises a first gas-solid separation device and a second gas-solid separation device; an inlet of the first gas-solid separation device is in communication with the delivery pipe, and a catalyst outlet of the first gas-solid separation device is located in the spent catalyst zone; and a catalyst outlet of the second gas-solid separation device is provided in the spent catalyst zone;
the fluidized bed reactor further comprises a product gas delivery pipe and a gas collection chamber, the product gas delivery pipe and the gas collection chamber are arranged on an upper part of the reactor shell, wherein the product gas delivery pipe is arranged at a top of the reactor shell, and the product gas delivery pipe is connected to a top of the gas collection chamber; and a gas outlet of the second gas-solid separation device is connected to the gas collection chamber, and a gas outlet of the first gas-solid separation device is connected to the gas collection chamber;
the fluidized bed reactor further comprises a spent catalyst circulation pipe, the spent catalyst circulation pipe is arranged outside the reactor shell; wherein an inlet of the spent catalyst circulation pipe is connected to the spent catalyst zone, and an outlet of the spent catalyst circulation pipe is connected to a bottom of the reaction zone.

4. A method for producing low-carbon olefins from an oxygen-containing compound using the fluidized bed reactor according to claim 1 .

5. The method according to claim 4 , comprising the following steps:
feeding a coke control raw material and the catalyst from a regenerator into the coke control zone to react to generate a coke controlled catalyst and a coke control product gas;
wherein the catalyst forms an annular flow through the at least one catalyst circulation hole on each of n−1 of the n baffles;
the method comprises the following steps:
(1) feeding the coke control raw material from a coke control zone distributor into the coke control zone, and feeding the catalyst from the catalyst inlet to the coke control zone, wherein the coke control raw material and the catalyst contact to react in the coke control zone to generate the coke controlled catalyst and the coke control product gas; wherein the coke controlled catalyst enters the reaction zone via the coke controlled catalyst outlet, and the coke control product gas enters the delivery pipe via the coke control gas outlet; and
(2) feeding a raw material containing the oxygen-containing compound into the reaction zone via the reaction raw material inlet, to contact with the coke controlled catalyst, to obtain a first stream comprising the low-carbon olefins.

6. The method according to claim 5 , wherein, the coke control raw material comprises a C 1 -C 6 hydrocarbon compound;
the C 1 -C 6 hydrocarbon compound is at least one of C 1 -C 6 alkanes and C 1 -C 6 olefins.

7. The method according to claim 6 , wherein the coke control raw material further comprises at least one of hydrogen, an alcohol compound, and water; and
a total content of the alcohol compound and the water in the coke control raw material is greater than or equal to 10 wt % and less than or equal to 50 wt %;
the alcohol compound is at least one of methanol and ethanol.

8. The method according to claim 7 , wherein, the coke control raw material comprises: 0 wt % to 20 wt % of the hydrogen, 0 wt % to 50 wt % of methane, 0 wt % to 50 wt % of ethane, 0 wt % to 20 wt % of ethylene, 0 wt % to 50 wt % of propane, 0 wt % to 20 wt % of propylene, 0 wt % to 90 wt % of butane, 0 wt % to 90 wt % of butene, 0 wt % to 90 wt % of pentane, 0 wt % to 90 wt % of pentene, 0 wt % to 90 wt % of hexane, 0 wt % to 90 wt % of hexene, 0 wt % to 50 wt % of the methanol, 0 wt % to 50 wt % of the ethanol, and 0 wt % to 50 wt % of the water; and
a weight content of the C 1 -C 6 hydrocarbon compound is not zero.

9. The method according to claim 5 , wherein the oxygen-containing compound is at least one of methanol and dimethyl ether;
the catalyst comprises an SAPO molecular sieve; a coke content in the coke controlled catalyst ranges from 4 wt % to 9 wt %; and a quartile deviation of a coke content distribution in the coke controlled catalyst is less than 1 wt %.

10. The method according to claim 9 , wherein coke species in the coke controlled catalyst comprise polymethylbenzene and polymethylnaphthalene;
a total weight content of the polymethylbenzene and the polymethylnaphthalene in a total coke weight

Assignees

• Dalian Inst Chem & Physics Cas

Inventors

• Ye Mao
• Zhang Tao
• Zhang Jinling
• Xu Shuliang
• Tang Hailong
• Wang Xiangao
• Zhang Cheng
• Jia Jinming
• Wang Jing
• Li Hua
• Li Chenggong
• Liu Zhongmin

Classifications

• C10G2400/20

  C2-C4 olefins · CPC title

• C10G2300/4093

  Catalyst stripping · CPC title

• C07C2531/06

  containing polymers · CPC title

• C07C2529/85

  Silicoaluminophosphates (SAPO compounds) · CPC title

• C07C1/24

  by elimination of water · CPC title