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Yield increase method of BTX aromatic hydrocarbons

A technology of BTX aromatics and aromatics, applied in the field of increasing production of BTX aromatics, can solve the problem of low utilization value of non-aromatics, and achieve self-sufficiency in reaction heat, good technical effects, and optimal adjustment effects

Active Publication Date: 2014-10-22
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] The technical problem to be solved by the present invention is that in the prior art, for low-aromatic mixtures, the traditional solvent extraction separation process only simply separates BTX aromatics, and a large amount of toluene, heavy aromatics and non-aromatics in the light aromatics products have low utilization value. The problem is to provide a new method for increasing the production of BTX. This method has the advantages of simple separation of hydrocarbon raw materials, high added value of products, avoiding solvent extraction process, and high value of non-aromatic hydrocarbons.

Method used

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  • Yield increase method of BTX aromatic hydrocarbons

Examples

Experimental program
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Effect test

Embodiment 1

[0023] with C 6 + As the raw material (the content of benzene is 24.4 tons / hour, the content of toluene is 9.3 tons / hour, the content of xylene is 2.1 tons / hour, and the content of ethylbenzene is 3.6 tons / hour), using figure 1 The process technology increases the production of BTX, and the circulation amount of the reaction liquid phase product is 30% by weight. Reaction unit, the reactor is a single-stage fixed-bed adiabatic reactor, the reaction pressure is 2.75 MPa, the reaction temperature is 360°C, the hydrogen partial pressure is 1.4 MPa, and the liquid phase weight space velocity is 2.1h -1 ; The stripper is a 44-layer float valve tray, the operating pressure at the top of the tower is 0.7MPa, the temperature of the partial condenser at the top of the tower is 40°C, and the non-condensable gas is discharged, wherein the molar concentration of ethane is 44.1%, and the molar concentration of propane is 36.9% %, other light hydrocarbons 19.0mol%. The benzene tower adop...

Embodiment 2

[0027] to reform C 9 +as raw material (benzene content is 0.03 tons / hour, toluene content is 39.5 tons / hour, xylene content is 33.9 tons / hour, C 9 + Aromatics content is 524.5 tons / hour), using figure 1 The process technology increases the production of BTX, and the circulation amount of the reaction liquid phase product is 30% by weight. Reaction unit, reaction pressure 2.8 MPa, reaction temperature 320°C, hydrogen partial pressure 1.14 MPa; stripping column is a 44-layer float valve tray, the operating pressure at the top of the tower is 0.7MPa, the control temperature of the top separator is 40°C, discharge Non-condensable gas, in which the molar concentration of ethane is 20.3%, the molar concentration of propane is 66.3%, and other light hydrocarbons are 13.4mol%. The benzene tower adopts 55 layers of valve trays, the operating pressure at the top of the tower is 0.05MPa, and 59.7 tons / hour of benzene product with a purity of 99.95wt% is obtained at the top of the tow...

Embodiment 3

[0031] to reform C 9 + as raw material (benzene content is 0.1 tons / hour, toluene content is 40 tons / hour, xylene content is 33.9 tons / hour, C 9 + Aromatics content is 524.5 tons / hour), using figure 1 The process technology increases the production of BTX, and the circulation amount of the reaction liquid phase product is 50% by weight. Reaction unit, reaction pressure 2.8 MPa, reaction temperature 320°C, hydrogen partial pressure 1.14 MPa; stripping column is a 44-layer float valve tray, the operating pressure at the top of the tower is 0.7MPa, the control temperature of the top separator is 40°C, discharge Non-condensable gas, in which the molar concentration of ethane is 20.3%, the molar concentration of propane is 66.3%, and other light hydrocarbons are 13.4mol%. The benzene tower adopts 55 layers of valve trays, the operating pressure at the top of the tower is 0.05MPa, and 59.7 tons / hour of benzene product with a purity of 99.95wt% is obtained at the top of the tower...

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Abstract

The invention relates to a yield increase method of BTX aromatic hydrocarbons, and mainly solves a problem of low utilization values of heavy aromatic hydrocarbons and non-aromatic hydrocarbons in the prior art. The method comprises the following steps: sending a mixture containing many aromatic rings or polycyclic C6 and above heavy components from a reforming, catalytic cracking and gasoline hydrogenation apparatus and hydrogen to a fixed bed reactor containing a molecular sieve catalyst in order to obtain a reaction product rich in BTX, and adjusting the circulating load of the reaction liquid phase product and C9 and above fractions to adjust the BTX composition of a product. The added values of raw materials are improved, the technical problem is solved, and the method can be used in industrial production of aromatic hydrocarbons.

Description

technical field [0001] The invention relates to a method for increasing the production of BTX aromatics. Background technique [0002] In industry, the reformed products produced by the reforming process and the pyrolysis gasoline obtained by cracking naphtha are generally separated by solvent extraction to separate BTX aromatics and non-aromatics. This process is based on the aromatics and non-aromatics in the solvent used. The polarity is different to achieve the purpose of separating the target aromatics. Although solvent extraction of BTX can obtain higher-purity BTX aromatics, it requires a complex solvent extraction device, and the extraction solvent needs to be continuously replenished during the extraction operation. The solvent extraction method obtains high-purity It is beneficial in terms of the mixing of aromatic hydrocarbons, but it is unfavorable in terms of the need for additional solvent extraction equipment and the need for continuous input of solvents duri...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C15/04C07C15/06C07C15/08C07C4/12C07C4/18C07C7/04
CPCY02P20/52
Inventor 李木金施德杨卫胜贺来宾
Owner CHINA PETROLEUM & CHEM CORP
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