Three-phase fluidized bed reactor

Abstract

The invention discloses an improved three-phase fluidized layer reactor, which consists of a reactor casing body and a three-phase separator positioned at the inner upper part of the casing body, wherein, the three-phase separator is composed of the inner cylinders and outer cylinders of two concentric cylinders with different inner diameters, a float tube arranged on the outer cylinder, and the inner wall of the reactor casing body. An upper limiting apparatus and a lower limiting apparatus are arranged on the reactor casing body, and the three-phase separator is positioned between the upper limiting apparatus and the lower limiting apparatus. The reactor is mainly suitable for the chemical reaction of different kinds of liquid and gas substances under the circumstance of contacting with solid particles, and has the advantages of large catalyst inventory, high utilization rate of the reactor, and high stability of operation.

Description

technical field [0001] The invention relates to a gas-liquid-solid three-phase ebullating bed reactor, in particular to a three-phase ebullating bed reactor used for chemical reactions of different kinds of liquid and gas substances in contact with solid particles. Background technique [0002] The ebullating bed reactor is a three-phase fluidized bed of gas, liquid and solid, which can process heavy and low-quality feed oil with high metal and high asphaltene content. It has the characteristics of small pressure drop, uniform temperature distribution, constant catalyst activity throughout the operation cycle, and the ability to add fresh catalyst and take out spent catalyst during operation. [0003] A typical fluidized bed process is described in US Re 25,770, but this process method has the following disadvantages in practical application: the amount of catalyst storage in the reactor is small, and the space utilization rate of the reactor is low; the maintenance cost of ...

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Problems solved by technology

[0003] A typical fluidized bed process is described in US Re 25,770, but this process method has the following disadvantages in practical application: the amount of catalyst storage in the reactor is small, and the space utilization rate of the reactor is low; the maintenance cost of the circulating oil pump is high, and once Malfunction and damage of the circulating oil pump will cause the catalyst to sink and accumulate, resulting in the forced shutdown of the device; the liquid product in the reactor stays for too long under non-catalytic hydrogenation conditions, and it is easy to undergo secondary thermal cracking reaction at high temperature Coking reduces product quality

However, in actual use, it is found that if the oil intake or circulating hydrogen is unstable, or the oil discharge from the reactor or the exhaust pi

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