Method for removing sulphur from coking benzol

A technology for coking benzene and oxidant, applied in chemical instruments and methods, molecular sieve catalysts, production of bulk chemicals, etc., can solve the problems of high cost, large amount of three wastes, high corrosion of equipment, etc., achieving less three wastes and simple process flow , The effect of high desulphurization efficiency

Active Publication Date: 2012-07-25
JIANGSU YANGNONG CHEM GROUP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] The purpose of the present invention is to provide a method for removing sulfur from coking benzene, so as to overcome the shortcomings of the existing process, such as large amount of "three wastes", high equipment corrosion, and high cost

Method used

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  • Method for removing sulphur from coking benzol
  • Method for removing sulphur from coking benzol
  • Method for removing sulphur from coking benzol

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0027] Three kettles connected in series, each kettle volume: 20L, 20L, 20L, the total effective reaction volume is 30L. The reaction temperature is 55°C to 65°C, and the exothermic heat of the reaction is exchanged through the jacket. Catalyst Titanium silicon molecular sieve catalyst fine particles (particle size 1-3um) account for 5% of the weight of coked benzene. Methanol is 50% of the weight of coked benzene, hydrogen peroxide is 5% of the weight of coked benzene, and the content is 27.5% (volume percentage).

[0028] Firstly, after the clinker is layered according to the proportion gap reaction, the slurry is put into the high-level tank, and the coking benzene, catalyst slurry and H 2 o 2 Use a peristaltic pump to drive into the first-stage reaction kettle at the same time, and the flow rates are V BZ =7.1L / hr, V H2O2 =56mL / hr, slurry V=2.9L / hr, add oxidant hydrogen peroxide dropwise in the first-stage reactor or each reactor. The stirring speed is 350rpm, the thr...

Embodiment 2

[0032] Three kettles connected in series, the volume of each kettle: 20L, 20L, 20L, the effective reaction volume is 30L, the reaction temperature is 30°C-40°C, and the catalyst is 5% of the weight of coked benzene. Methanol is 50% of the weight of coked benzene, and the content of hydrogen peroxide is 35% (percentage by volume). The consumption is 5% of the weight of coked benzene.

[0033] Firstly, after the clinker is layered according to the proportion gap reaction, the slurry is put into the high-level tank, and the coking benzene, catalyst slurry and H 2 o 2 Use a peristaltic pump to drive into the first-stage reaction kettle at the same time, and the flow rates are V BZ =7.1L / hr, V H2O2 =56mL / hr, slurry V=2.9L / hr, add oxidant hydrogen peroxide dropwise in the first-stage reactor or each reactor. The stirring speed is 350rpm, the three reactors stay for about 3 hours, the feed flow rate per hour = 10L / h, and the reaction materials overflow from the upper end of the re...

Embodiment 3

[0036] Three kettles connected in series, each kettle volume: 20L, 20L, 20L, the total effective reaction volume is 30L. The reaction temperature is 55°C-65°C, the reaction is exothermic, and the heat is exchanged through the jacket. The catalyst is 5% by weight of coked benzene. Methanol is 20% of the weight of coked benzene, and the content of hydrogen peroxide is 27.5% (volume percentage). The consumption is 5% of the weight of coked benzene.

[0037] Firstly, after the clinker is layered according to the proportion gap reaction, the slurry is put into the high-level tank, and the coking benzene, catalyst slurry and H 2 o 2 Use a peristaltic pump to drive into the first-stage reaction kettle at the same time, and the flow rates are V BZ =7.1L / hr, V H2O2 =56mL / hr, slurry V=2.9L / hr, add oxidant hydrogen peroxide dropwise in the first-stage reactor or each reactor. The stirring speed is 350rpm, the three reactors stay for about 3 hours, the feed flow rate per hour = 10L / h...

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Abstract

The invention relates to a method for removing sulphur from coking benzol, belonging to the technical field of organic chemical engineering; and the invention in particular relates to continuous sulphur removal technology of coking benzol; the coking benzol, solvent, oxidant and titanium-silicon molecular sieve catalyst particles are added in a slurry bed reaction kettle and are reacted under thetemperature of 10-90 DEG C, and the reacted products are divided into oil-phase slurry and water-phase slurry, alkaline washing and water-washing layering are carried out to the oil-phase slurry for obtaining sulphur-removal benzene, and the water-phase slurry is returned to the reaction kettle. After being treated, the coking benzol contained about 200ppm of sulphur contains 0-5ppm of sulphur; the method has simple flow, less three wastes and high yield coefficient and is easy to realize industrialization.

Description

technical field [0001] The invention belongs to the technical field of organic chemical industry, and particularly relates to the continuous desulfurization technology of coking benzene desulfurization. Background technique [0002] Benzene is an important chemical raw material with a wide range of uses. One of its main sources is coking benzene obtained from high-temperature pyrolysis of coal. In recent years, the price of international oil market has been rising continuously, and the gap between petroleum benzene, which uses petroleum as raw material, and coking benzene produced by benzene hydrogenation method and pickling method has widened in terms of raw material cost. In 2005, the production cost of coking benzene was at least lower than that of petroleum benzene 1500 yuan / t. Compared with petroleum benzene, the coking benzene obtained after high-temperature pyrolysis still contains sulfur substances such as thiophene. Compared with petroleum benzene, the content of i...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C15/04C07C7/148B01J29/89
CPCY02P20/52
Inventor 王秋萍袁源顾志强许金来丁克鸿吴翔汪洋
Owner JIANGSU YANGNONG CHEM GROUP
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