Method and device for manufacturing propene and C4 hydrocarbon

Patent metadata

Field	Value
Publication number	US-10640433-B2
Application number	US-201616342611-A
Country	US
Kind code	B2
Filing date	Oct 19, 2016
Priority date	Oct 19, 2016
Publication date	May 5, 2020
Grant date	May 5, 2020

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.

First claim

The invention claimed is:

1. 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 one or more 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 first 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.

2. The device according to claim 1 , 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.

3. The device according to claim 1 , 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.

4. The device according to claim 1 , wherein the catalytic cracking lift pipe and the fast fluidized-bed reactor share the second gas-solid separator.

5. The device according to claim 1 , wherein the fluidized-bed regenerator is a turbulent fluidized-bed regenerator.

6. The device according to claim 1 , wherein the first reactor gas-solid separator, the second reactor gas-solid separator and the regenerator gas-solid separator are cyclone separators.

7. A method for preparing propylene and C4 hydrocarbons from oxygen-containing compounds, comprising:
feeding a raw material containing an oxygen-containing compound from one or more 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 first reactor gas-solid separator, 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 CO 2 , 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.

8. The method according to claim 7 , 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 r

Assignees

• Dalian Inst Chem & Physics Cas

Inventors

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

Classifications

• B01D45/12

  by centrifugal forces (centrifuges B04B; cyclones B04C) · CPC title

• C07C11/06

  Propene · CPC title

• B01J8/388

  externally, i.e. the particles leaving the vessel and subsequently re-entering it · CPC title

• C07C1/20 Primary

  starting from organic compounds containing only oxygen atoms as heteroatoms · CPC title

• C07C4/06

  Catalytic processes {(C07C4/025 takes precedence)} · CPC title