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A Multistage Jet Loop Reactor for Oxidative Coupling of Methane to Ethylene

A loop reactor and oxidative coupling technology, which is applied in chemical instruments and methods, organic chemistry, bulk chemical production, etc., can solve problems such as uneven temperature distribution, back-mixing, and low ethylene yield, and reduce deep reactions , reduce back-mixing and increase ethylene yield

Active Publication Date: 2022-04-12
山西潞安化工有限公司 +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] In order to overcome the deficiencies of the above-mentioned prior art, the present invention provides a multi-stage jet loop reactor for the oxidative coupling of methane to ethylene, to solve the problems of uneven temperature distribution in the reactor, serious back-mixing, and low ethylene yield. question

Method used

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  • A Multistage Jet Loop Reactor for Oxidative Coupling of Methane to Ethylene
  • A Multistage Jet Loop Reactor for Oxidative Coupling of Methane to Ethylene
  • A Multistage Jet Loop Reactor for Oxidative Coupling of Methane to Ethylene

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Embodiment 1

[0031] A multi-stage jet loop reactor for oxidative coupling of methane to ethylene is divided into a conical bottom zone, a circulation zone, a gas-solid separation zone, a cyclone separation zone and a feed-back zone. The conical bottom area includes the nozzle 1 and the conical bottom 2; the circulation area includes the lower space of the shell 3, the gas distributor 5, the first-stage guide tube 4 and the second-stage guide tube 6; the gas-solid separation area includes the shell The upper space of the body 3; the cyclone separation area includes a cyclone separator 9; the return area includes a material leg 10, a heat exchanger 11, a return valve 12, a secondary air inlet 13, a discharge valve 14 and a return pipe 15.

[0032] Such as figure 1 As shown, the nozzle 1 is located at the bottom of the conical bottom 2, the conical bottom 2 is connected to the bottom end of the shell 3, the first-stage guide tube 4 and the second-stage guide tube 6 are located in the middle a...

Embodiment 2

[0036] Adopt the reactor configuration identical with embodiment 1, difference is: adopt such as image 3 The placement method of the annular gas distributor shown in (b) is specifically manifested in that the annular gas distribution adopted is a single annular gas distributor, in which a single annular gas distributor with upward openings is placed between the stages of the draft tube (such as Figure 4 (B-B)), place a single-ring gas distributor with openings downward at the middle height of each guide tube (such as Figure 4 (A-A)). The average particle size of the catalyst is 100 μm, the reaction temperature is 800 °C, and the operation is under normal pressure. The gas composition passing through the nozzle is methane, the gas composition passing through the gas distributor and the secondary air inlet is oxygen and nitrogen, and the volumetric space velocity is 6000 h -1 , Methane: Oxygen: Nitrogen molar ratio of 3:1:1, methane conversion rate of 46%, ethylene yield of ...

Embodiment 3

[0038] Adopt the reactor configuration identical with embodiment 1, difference is: adopt such as image 3 The placement method of the annular gas distributor shown in (c) is specifically shown that the double-annular gas distribution is placed at the middle height of each draft tube. The average particle size of the catalyst is 150 μm, the reaction temperature is 800 ° C, the operating pressure is 5 bar, the gas components passing through the nozzle are methane and oxygen, the gas components passing through the gas distributor and the secondary air inlet are oxygen and nitrogen, and the volume space velocity for 8000 h -1 , methane: oxygen: nitrogen molar ratio under the condition of 3:1:1, methane conversion rate was 47%, ethylene yield was 28%.

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Abstract

The invention relates to the technical field of methane conversion, a multi-stage jet loop reactor for oxidative coupling of methane to ethylene, including a nozzle, a conical bottom, a multi-stage guide tube, a gas distributor, a shell, a cyclone separator, Heat exchanger and material return device, the nozzle is located at the bottom of the conical bottom, the conical bottom is at the bottom of the shell, the number of multi-stage guide tubes is located in the lower part of the shell, and the number of multi-stage guide tubes is greater than or equal to 2 The equal-diameter vertical cylinder, the gas distributor is located in the lower part of the shell and the number is one or more. The invention uses nozzles, conical bottoms, multi-stage guide tubes and gas distributors to form a forced internal circulation of materials, which can promote regular movement of materials, reduce back mixing, enhance mass transfer and heat transfer, and contribute to the internal circulation of reactors. Uniform temperature distribution improves catalyst utilization and product yield.

Description

technical field [0001] The invention relates to the technical field of methane conversion, in particular to a multi-stage jet loop reactor for oxidative coupling of methane to produce ethylene. Background technique [0002] Ethylene is an important basic organic chemical product and raw material, and its production level is an important indicator to measure a country's chemical strength. At present, ethylene production is mainly based on naphtha cracking, which has problems such as high cost, high energy consumption and greenhouse gas emissions. With the development of the international economy, the raw materials for ethylene production tend to be lighter and more diversified. Oxidative coupling of methane (OCM) one-step direct ethylene production technology has the advantages of simple route and good economy. It is an ethylene production technology with broad development prospects and is of great significance to the optimization of my country's energy structure. [0003] ...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): B01J8/22C07C2/84C07C11/04
CPCB01J8/226C07C2/84C07C11/04Y02P20/52
Inventor 李德宝高用祥刘俊义林明桂马军祥张力贾丽涛崔艳斌余海兵夏铭牛鹏宇荆明杰
Owner 山西潞安化工有限公司
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