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Methanol-to-olefin (MTO) reaction-regeneration process and product separation method

A methanol-to-olefin and process technology, which is applied in the separation field of separating polymer-grade ethylene and propylene, can solve the problems of high energy consumption of equipment, low working temperature of cold separation unit, insufficient matching of working pressure and temperature of separation process, etc. The effect of saving energy consumption and effective recycling

Active Publication Date: 2020-04-28
JIUTAI ENERGY ZHUNGEER CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] The method disclosed in the above-mentioned patent documents needs to use a lower temperature refrigerant in the cold separation unit, and the working temperature of the cold separation unit is lower; in addition, the working pressure and temperature matching of the existing separation process is not sufficient, which leads to the higher energy consumption

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0085] Methanol reacts with the catalyst ZSM-5 through the fluidized bed reactor, and the reactant gas enters the cyclone separator for further separation; the temperature in the reactor is 410°C, the reaction pressure is 0.12 MPa, and the ratio of catalyst circulation to methanol feed is 4: 1. The empty tower velocity in the reactor is 0.3m / s; the spent catalyst in the reactor enters the regenerator for regeneration. The temperature of the regenerator is 557℃, the regenerator pressure is 0.07MPa, and the empty tower velocity in the regenerator 0.17m / s;

[0086] The product gas from the top of the cyclone separator is separated from the catalyst and cooled and then enters the quench tower; the product gas from the quench tower is further cooled in the product gas separation tower, and the water and oxidation in the product gas are removed by the product gas separation tower After the material enters the product gas compressor for three-stage compression and boost: the pressure af...

Embodiment 2

[0089] Methanol reacts with the catalyst ZSM-5 through the fluidized bed reactor, and the reactant gas enters the cyclone separator for further separation; the temperature in the reactor is 460℃; the reaction pressure is 0.25MPa; the catalyst circulation rate to methanol feed rate ratio is 15: 1; The empty tower velocity in the reactor is 0.7m / s; the spent catalyst in the reactor enters the regenerator for regeneration, and the temperature of the regenerator is 620℃; the regenerator pressure is 0.13MPa; the empty tower velocity in the regenerator 0.5m / s;

[0090] The product gas from the top of the cyclone separator is separated from the catalyst and cooled and then enters the quench tower; the product gas from the quench tower is further cooled in the product gas separation tower, and the water and oxidation in the product gas are removed by the product gas separation tower After the material enters the product gas compressor for three-stage compression and boost: the pressure a...

Embodiment 3

[0093] Methanol reacts with the catalyst ZSM-5 through the fluidized bed reactor, and the reactant gas enters the cyclone separator for further separation; the temperature in the reactor is 490℃; the reaction pressure is 0.35MPa; the ratio of catalyst circulation to methanol feed is 26: 1; The empty tower velocity in the reactor is 1.8m / s; the spent catalyst in the reactor enters the regenerator for regeneration, the regenerator temperature is 690℃; the regenerator pressure is 0.21MPa; the empty tower velocity in the regenerator 0.7m / s;

[0094] The product gas from the top of the cyclone separator is separated from the catalyst and cooled and then enters the quench tower; the product gas from the quench tower is further cooled in the product gas separation tower, and the water and oxidation in the product gas are removed by the product gas separation tower After the material enters the product gas compressor for three-stage compression and boost: the pressure after the first sta...

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Abstract

The invention relates to a methanol-to-olefin (MTO) reaction-regeneration process and a product separation method. The pressure value is reduced in the three-stage compression and pressurization in the methanol-to-olefin reaction process, and part of unreacted methanol, dimethyl ether and other impurities are also removed by matching with the temperature. In product separation, the temperature ofa demethanizer is higher than that in the prior art, methane, hydrogen and other components are also effectively separated by properly increasing the pressure, and effective recovery of ethylene and propylene is realized. The temperature of the separation process is relatively high, so that the temperature of the used refrigerant is higher than that of other ethylene refrigerants and propane refrigerants, and the energy consumption is reduced.

Description

Technical field [0001] The invention relates to a methanol-to-olefin (MTO) reverse process and a product separation method, in particular to a separation method for separating polymerization grade ethylene and propylene from the product of the methanol-to-olefin reverse process. Background technique [0002] Methanol to olefins (MTO) is the use of SAPO-n series catalysts (such as silicoaluminophosphate molecular sieve) to produce olefins from methanol. The reaction products mainly consist of ethylene, ethane, acetylene, propylene, propane, propyne, methanol, and dimethyl Ether, hydrogen, nitrogen, methane, carbon monoxide, carbon dioxide, etc. How to separate the reaction products to obtain ethylene and propylene is the core technology of the separation process. [0003] The existing separation process is generally divided into four units: compression unit, impurity removal unit, cold separation unit and thermal separation unit. The compression unit raises the product gas to the ...

Claims

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Application Information

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IPC IPC(8): C07C1/20C07C7/00C07C7/04C07C7/11C07C7/167C07C11/04C07C11/06
CPCC07C1/20C07C7/005C07C7/04C07C7/11C07C7/167C07C2529/40C07C11/04C07C11/06Y02P20/584Y02P30/20Y02P30/40
Inventor 张庆海刘鑫邵永飞卢振林耿立生徐岩文李先亮李凤
Owner JIUTAI ENERGY ZHUNGEER CO LTD
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