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Multi-optimized slurry bed hydrogenation reactor, application and design method thereof

A hydrogenation reactor and slurry bed technology, applied in chemical instruments and methods, chemical/physical processes, hydrocarbon oil cracking, etc., can solve problems such as blockage and coking, reduce costs, speed up reaction rates, and deepen reaction levels Effect

Inactive Publication Date: 2015-08-05
CATECH TECH
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0006] The invention provides a multi-optimized slurry bed hydrogenation reactor, adding a forced internal circulation structure, enhancing the degree of back-mixing of reactants, improving the conversion rate of raw materials and the yield of light oil, and at the same time solving the problem of coking, clogging and Fly temperature problem

Method used

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  • Multi-optimized slurry bed hydrogenation reactor, application and design method thereof

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0037] This example is an example of residual oil hydrogenation. The structural parameters of the reactor are as follows: the inner diameter of the reactor shell is 200mm, the height of the reactor shell is 3500mm, the diameter of the reactor circulation pipe is 80mm, and the height is 3200mm. Using FeOOH iron-based catalyst and the above-mentioned slurry bed hydrogenation reactor, heavy oil hydrogenation test was carried out under the slurry bed process conditions with the following basic parameters. The properties of the residual oil used in the test are shown in Table 1.

[0038] The basic process parameters of the pilot slurry bed:

[0039] Temperature: 440-460°C;

[0040] Experimental pressure: 17-19Mpa;

[0041] Hydrogen oil ratio: 900:1-1000:1;

[0042] Airspeed: 0.5h -1 ;

[0043] Circulation volume / feed volume: 4.0;

[0044] Catalyst / feed residue: 1 / 100(wt);

[0045] Vulcanizing agent / feed residue: 2.5 / 100 (wt).

[0046] The results of the test are as follows:

...

Embodiment 2

[0051] This embodiment is an example of direct coal liquefaction. The reactor used is the same as in Example 1, and the catalyst is the same as in Example 1. Under the pilot test slurry bed process conditions with the following basic parameters, the direct coal liquefaction test is carried out. The pulverized coal used in the test See Table 2 for the properties, and the basic process parameters of the pilot slurry bed are as follows:

[0052] Temperature: 440-465°C;

[0053] Experimental pressure: 17-20Mpa;

[0054] Hydrogen oil ratio: 1200:1~1600:1;

[0055] Airspeed: 0.35~0.50h -1 ;

[0056] Circulation volume / feed volume: 6.0;

[0057] Mass ratio of oil / coal feed / circulating solvent: 10:10:1;

[0058] Catalyst / feed coal: 1.2 / 100(wt);

[0059] Vulcanizing agent / feed coal: 2.5 / 100(wt);

[0060] Slurry bed chemical hydrogen consumption (hydrogen / feed): 5 / 100 (wt).

[0061] The results of the test are as follows:

[0062] Coal conversion rate: 88.2%, liquid yield 58.3%...

Embodiment 3

[0067] This embodiment is an example of oil-coal mixing, the reactor structure is the same as Example 1, the catalyst is the same as Example 1, the properties of the residual oil used in the test are the same as Example 1, and the properties of coal powder are the same as Example 2. The basic process parameters of the pilot test slurry bed in the present embodiment are as follows:

[0068] Temperature: 440-460°C;

[0069] Experimental pressure: 17-20Mpa;

[0070] Hydrogen oil ratio: 1000:1-1400:1;

[0071] Airspeed: 0.40-0.50h -1 ;

[0072] Circulation volume / feed volume: 5.0;

[0073] Oil / coal feed / refined wax oil mass ratio: 9:10:2;

[0074] Catalyst / feed oil coal slurry: 1 / 100(wt);

[0075] Vulcanizing agent / feed oil coal slurry: 2.5 / 100(wt);

[0076] Slurry bed chemical hydrogen consumption (hydrogen / feed): 4.5 / 100 (wt).

[0077] The results of the test are as follows:

[0078] Total conversion rate of oil and coal: 91.2%, liquid yield 71.3%, coke production rate ...

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Abstract

The invention discloses a multi-optimized slurry bed hydrogenation reactor, an application and a design method thereof, wherein the multi-optimized slurry bed hydrogenation reactor includes an internal circulating structure and a feed distributor. A material inlet is arranged on a lower part of a column body of the reactor while a material outlet is arranged on the top of the column body. The internal circulating structure includes a circulating bubble cap, a circulating tube and a circulating pump. The circulating bubble cap is arranged in the upper part in the column body and is in the structure of an inverted circular truncated-conical hollow cup. The lower end of the circulating bubble cap is connected to the circulating tube, is communicated with the bottom of the column body and is communicated with the circulating pump outside the column body. The feed distributor includes an inlet feed distributor and a circulating feed distributor and is arranged between the inner wall in the lower part of the column body and the circulating tube. The material inlet includes an entrance inlet and a circulating inlet. Reaction materials are fed into the column body through the entrance inlet and then through the inlet feed distributor, wherein circulated material recycled by the internal circulating structure is fed into the circulating inlet through the circulating pump and then is fed into the column body through the circulating feed distributor. The multi-optimized slurry bed hydrogenation reactor is improved in backmixing degree of reactants and is improved in conversion rate of raw materials and yield of light oil.

Description

technical field [0001] The invention relates to a slurry bed hydrogenation reactor and related technologies matched with it, belonging to the fields of petrochemical and coal chemical industries. Background technique [0002] In recent years, with the continuous increase of crude oil extraction and the continuous decrease of conventional crude oil reserves, the trend of crude oil inferiority has become more and more serious. Among the middle distillate oil obtained by direct distillation of crude oil and the middle distillate oil obtained by secondary processing such as coking and catalytic cracking, etc. The S and N content of the carbon dioxide also increased accordingly. However, the market demand for light oil continues to increase, people's awareness of environmental protection continues to increase, environmental protection laws and regulations have stricter requirements on engine exhaust emissions, and various fuel standards require more stringent S and N content. Th...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G47/26C10G45/16
CPCB01J8/22C10G45/00
Inventor 李苏安邓清宇王坤朋
Owner CATECH TECH
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