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Method and device for in-situ on-line cyclonic activity recovery of catalyst in fluidized bed hydrogenation reactor

A technology for hydrogenation reactors and activity recovery, applied in catalyst regeneration/reactivation, chemical instruments and methods, physical/chemical process catalysts, etc., can solve problems such as catalyst life that has not been seen, and achieve extended life and slow down the coking process Effect

Active Publication Date: 2019-07-12
SHANGHAI HUACHANG ENVIRONMENT PROTECTION
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Although it has been reported that the disturbance of the catalyst in the ebullating bed reactor can slow down the carbon deposition of the catalyst and prolong the life of the catalyst, it has not been seen in the engineering technology to forcibly regulate the movement state of the catalyst to realize the method of slowing down the carbon deposition of the catalyst and prolonging the life of the catalyst. and installation

Method used

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  • Method and device for in-situ on-line cyclonic activity recovery of catalyst in fluidized bed hydrogenation reactor
  • Method and device for in-situ on-line cyclonic activity recovery of catalyst in fluidized bed hydrogenation reactor
  • Method and device for in-situ on-line cyclonic activity recovery of catalyst in fluidized bed hydrogenation reactor

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Experimental program
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Embodiment 1

[0069] 1. Device name

[0070] 5000L / h fluidized bed hydrogenation reactor cold mold device.

[0071] 2. Process flow

[0072] Such as Figure 5 Shown. Tap water comes from tank b. After the tap water is pressurized by circulating pump c (higher than the pressure in the reactor), it enters the reactor from the mixed phase inlet at the bottom of fluidized bed hydrogenation reactor a; air in the atmosphere is fed by air compressor d After being compressed, it is stored in the gas storage tank e, and the air enters the reactor from the outlet of the gas storage tank e from the mixed phase inlet at the bottom of the fluidized bed hydrogenation reactor a. Under the momentum transfer of tap water and air, the catalyst particles in the fluidized bed hydrogenation reactor a reach a fluidized state. In the ebullating bed reactor, the gas-liquid-solid three-phase mixture is separated by the three-phase separator at the top of the reactor, the obtained gas phase is discharged from the gas ph...

Embodiment 2

[0082] 1. Device name

[0083] 200L / h sludge cracking liquid hydrodeoxygenation device.

[0084] 2. Process flow

[0085] Such as Image 6 Shown. The feed oil and hydrogen supply agent enter the reactor from the bottom of the fluidized bed hydrogenation reactor a. The control range of the feed temperature of the feedstock oil and the hydrogen donor is from room temperature to 45°C, and the mass ratio of the hydrogen donor and feedstock is generally controlled to be 0.25 to 2:1. The hydrogen donor may be diesel oil or wax oil distillate obtained by fractional distillation of the boiling bed hydrodeoxygenation product of the feedstock, or diesel or wax oil distillate with high aromatic content outside the device. The circulating oil comes from the oil phase outlet of the cold high-pressure separator g. After the circulating oil is pressurized to 8-20 MPa (higher than the pressure in the reactor) by the circulating pump c, it is combined with hydrogen (including circulating hydrogen ...

Embodiment 3

[0095] 1. Device name

[0096] 100L / h sawdust cracking liquid hydrodeoxygenation device

[0097] 2. Process flow

[0098] Such as Figure 7 Shown. The feed oil and hydrogen supply agent enter the reactor from the bottom of the fluidized bed hydrogenation reactor a. The control range of the feed temperature of the feedstock oil and the hydrogen donor is from room temperature to 45°C, and the mass ratio of the hydrogen donor and feedstock is generally controlled to be 0.25 to 2:1. The hydrogen donor may be diesel oil or wax oil distillate obtained by fractional distillation of the boiling bed hydrodeoxygenation product of the feedstock, or diesel or wax oil distillate with high aromatic content outside the device. The circulating oil comes from the oil phase outlet of the cold high-pressure separator g. After the circulating oil is pressurized to 8-20 MPa (higher than the pressure in the reactor) by the circulating pump c, it is combined with hydrogen (including circulating hydrogen...

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Abstract

The invention relates to a method and device for in-situ on-line cyclonic activity recovery of a catalyst in a fluidized bed hydrogenation reactor, and provides a method for the in-situ on-line cyclonic activity recovery of the catalyst in the fluidized bed hydrogenation reactor. The method comprises the following steps: a) a three-phase mixture consisting of a gas phase, a liquid phase and catalyst particles in the fluidized bed hydrogenation reactor is degassed in the fluidized bed hydrogenation reactor to obtain a two-phase mixture consisting of the liquid phase and the catalyst particles;b) a forcedly obtained two-phase mixture rotates in the fluidized bed hydrogenation reactor to form a swirling flow field, and regulates a coupled motion state of the catalyst particles revolving around a central axis of the swirling flow field in the swirling flow field and revolving around the central axis of the catalyst particles themselves; and c) centrifugal force generated by the revolutionmotion of the catalyst particles in the swirl flow field is utilized to achieve separation of the catalyst particles from the two-phase mixture. The invention further provides the device for the in-situ on-line cyclonic activity recovery of the catalyst in the fluidized bed hydrogenation reactor.

Description

Technical field [0001] The present disclosure relates to a fluidized bed hydrogenation reactor, in particular to a method and device for restoring in-situ cyclone activity of a catalyst in a fluidized bed hydrogenation reactor. Background technique [0002] The main reasons for catalyst deactivation are: (i) sintering and isolation of the active phase; (ii) the catalyst pores and active sites are blocked by carbon deposits and metal deposits; (iii) the active sites are poisoned. For the deactivation caused by the blockage of the catalyst pores and active sites by carbon deposits, the outer layer of carbon deposits that initially wraps the catalyst is permeable and mainly consists of carbon deposits with a pre-graphitized carbon structure; as the cycle progresses, The carbon deposits accumulate continuously, and the outer layer of the catalyst carbon deposits is less and less permeable to liquid diffusion, resulting in a decrease in the activity and selectivity of the catalyst; th...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01J8/14B01J38/00
CPCB01J8/14B01J38/00
Inventor 李剑平王尧汪华林沈其松杨雪晶崔馨常玉龙黄渊付鹏波
Owner SHANGHAI HUACHANG ENVIRONMENT PROTECTION