Fluidized-bed apparatus and method to co-produce p-xylene and light olefins by methanol and/or dimethyl ether and benzene

A technology of p-xylene and low-carbon olefins, which is applied in the field of equipment for the production of p-xylene and low-carbon olefins, and can solve the problems of complex process, low benzene conversion rate, high benzene conversion rate and high p-xylene yield

Active Publication Date: 2018-11-13
DALIAN INST OF CHEM PHYSICS CHINESE ACAD OF SCI
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Simultaneously realize two reactions in the same reactor, the process is simple, but the benzene conversion rate is low; realize two reactions in different reactors, the process is more complicated, but the benzene conversion rate and p-xylene yield are higher

Method used

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  • Fluidized-bed apparatus and method to co-produce p-xylene and light olefins by methanol and/or dimethyl ether and benzene

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0123] use figure 1 The device shown, but the turbulent fluidized bed reactor 1 does not include the reactor gas-solid separator 4 and the perforated plate 26, and the regeneration riser 24 is directly connected to the dilute phase zone of the turbulent fluidized bed reactor 1. The turbulent fluidized bed reactor 1 contains a reactor feed distributor 3-1.

[0124] The reaction conditions in the reaction zone of the turbulent fluidized bed reactor 1 are: the superficial linear velocity of the gas is about 1.0m / s, the reaction temperature is about 500°C, the reaction pressure is about 0.15MPa, and the bed density is about 350kg / m3.

[0125] The reaction conditions in the regeneration zone of the fluidized bed regenerator 14 are: the apparent linear velocity of the gas is about 1.0m / s, the regeneration temperature is about 650°C, the regeneration pressure is about 0.15MPa, and the bed density is about 350kg / m3.

[0126] The catalyst contains HZSM-5 molecular sieve, and the carbo...

Embodiment 2

[0131] use figure 1 In the shown device, the turbulent fluidized bed reactor 1 contains 3 reactor feed distributors 3-1 to 3-3, the opening ratio of the porous plate 26 is 10%, and the reactor gas-solid separator 4 is placed Inside the reactor shell 2.

[0132] The reaction conditions in the reaction zone of the turbulent fluidized bed reactor 1 are: the superficial linear velocity of the gas is about 1.0m / s, the reaction temperature is about 500°C, the reaction pressure is about 0.15MPa, and the bed density is about 350kg / m3.

[0133] The reaction conditions in the regeneration zone of the fluidized bed regenerator 14 are: the apparent linear velocity of the gas is about 1.0m / s, the regeneration temperature is about 650°C, the regeneration pressure is about 0.15MPa, and the bed density is about 350kg / m3.

[0134] The catalyst contains HZSM-5 molecular sieve, and the carbon content of the regenerated catalyst is about 0.1 wt.%.

[0135] The regeneration medium is air; the st...

Embodiment 3

[0145] use figure 1 In the shown device, the turbulent fluidized bed reactor 1 contains 6 reactor feed distributors 3-2 to 3-6, the opening ratio of the porous plate is 5%, and the reactor gas-solid separator 4 is placed in the reaction Inside the device housing 2.

[0146] The reaction conditions in the reaction zone 1 of the turbulent fluidized bed reactor are: the apparent linear velocity of the gas is about 0.8m / s, the reaction temperature is about 560°C, the reaction pressure is about 0.6MPa, and the bed density is about 460kg / m 3 .

[0147] The reaction conditions in the regeneration zone of the fluidized bed regenerator 14 are: the apparent linear velocity of the gas is about 1.7m / s, the regeneration temperature is about 600°C, the regeneration pressure is about 0.6MPa, and the bed density is about 220kg / m 3 .

[0148] The catalyst contains HZSM-11 molecular sieve, and the carbon content of the regenerated catalyst is about 0.15wt.%.

[0149] The regeneration medium i...

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Abstract

The application discloses a turbulent fixed-bed reactor, apparatus and method to co-produce p-xylene and light olefins by methanol and / or dimethyl ether and benzene, solves or improves the problem that MTO (methanol to olefins) reaction and alkylation reaction compete each other in the process of co-producing p-xylene and light olefins by methanol and / or dimethyl ether and benzene, and implementssynergy of MTO reaction and alkylation reaction. By controlling mass transfer and reactions and coordinating and optimizing the competition between alkylation reaction and MTO reaction to arrive at their synergy, benzene conversion rate, p-xylene yield and light olefins selectivity are increased. The turbulent fixed-bed reactor comprises a first reactor feeding distributor and a plurality of second reactor feeding distributors; the first reactor feeding distributor and the second reactor feeding distributors are arranged sequentially along a gas flow direction in a reaction zone of the turbulent fixed-bed reactor.

Description

technical field [0001] This application relates to a device and production method for the co-production of p-xylene (PX) and low-carbon olefins, especially suitable for the fluidization of methanol and / or dimethyl ether and benzene to produce p-xylene and co-production of low-carbon olefins A bed device and a production method belong to the field of chemistry and chemical engineering. Background technique [0002] Para-xylene (PX) is one of the basic organic raw materials in the petrochemical industry, and has a wide range of applications in many fields such as chemical fiber, synthetic resin, pesticide, medicine, and polymer materials. Currently p-xylene production mainly uses toluene, C 9 Aromatic hydrocarbons and mixed xylenes are used as raw materials, and are produced through disproportionation, isomerization, adsorption separation or cryogenic separation. Since the p-xylene content in its product is thermodynamically controlled, p-xylene is at C 8 Mixed aromatics on...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01J8/26B01J8/38C07C2/86C07C15/08C07C1/20C07C11/02
CPCB01J8/1836B01J8/1872B01J8/26B01J8/388C07C1/20C07C2/864C07C2/865B01J2208/00327C07C15/08C07C11/02B01J8/18B01J8/38Y02P30/20Y02P30/40C07C2529/40B01J8/0055B01J8/1827B01J2208/0092B01J2208/00938B01J2208/00911B01J8/44Y02P20/52Y02P20/584C07C11/08C07C11/06C07C11/04B01J8/1863B01J2208/00168
Inventor 张涛叶茂刘中民张今令唐海龙贾金明何长青王贤高张骋李华赵银峰李承功
Owner DALIAN INST OF CHEM PHYSICS CHINESE ACAD OF SCI
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