Crude benzene hydrorefining process

A technology for hydrofining and crude benzene, which is applied in the fields of hydrocarbons, chemical instruments and methods, organic chemistry, etc. It can solve the problems of excessive waste of raw materials, easy coking and blockage of the reaction system, high requirements for reaction temperature, etc., and achieve a stable reaction process , reduce the risk of coking in the system, and reduce equipment requirements

Active Publication Date: 2013-09-04
湖北巨邦石油化工有限公司
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0016] The existing technology shows that there are many deficiencies in the existing crude benzene refining process, not only the waste of raw materials is large, but also the reaction system is easy to coke and block, and at the same time, the requirement for the reaction temperature is relatively high

Method used

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  • Crude benzene hydrorefining process
  • Crude benzene hydrorefining process
  • Crude benzene hydrorefining process

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0047] First, the raw material is coordinating thick benzene, the component and mass score it contains as follows:

[0048] Benzene: 75%, toluene: 13.9%, two toluene: 2.24%, light group points: 0.86%, reorganization points: 8%, total sulfur content 6546.57ppm, total nitrogen content 899.3ppm.

[0049] 2. In this embodiment, the response temperature of the hydrogen hydrogenation reaction of hydrogenation is 140 ° C, the catalyst is CO-MO, and the volume ratio of hydrogen oil is 500: 1. -1 , Pressure 2.8MPa;

[0050] The reaction temperature of the gas catalytic pre-hydrogenation reaction is 190 ° C, the catalyst is NI-MO catalyst, the volume ratio of hydrogen oil is 400: 1. -1 , Pressure 2.0MPa;

[0051] The reaction temperature of the main catalytic hydrogenation reaction is 270 ° C, the catalyst is CR-MO catalyst, the volume ratio of hydrogen oil is 400: 1. -1 , Pressure 2.0MPa.

[0052] After hydrogenation reaction:

[0053] The total sulfur content of the product is 0.2PPM tota...

Embodiment 2

[0055] Examples of this embodiment are operated according to Example 1, the difference is:

[0056] In this embodiment, the reaction temperature of the hydrogen hydrogenation reaction of the hydrogenation is 130 ° C, the catalyst is CO-MO, and the volume ratio of hydrogen oil is 300: 1, the volume airspace 0.1H -1 , Pressure 2.4MPa;

[0057] The reaction temperature of the gas catalytic pre-hydrogenation reaction is 210 ° C, the catalyst is NI-MO catalyst, the volume ratio of hydrogen oil is 500: 1. -1 , Pressure 2.8MPa;

[0058] The reaction temperature of the main catalytic hydrogenation reaction is 290 ° C, the catalyst is CR-MO catalyst, the volume ratio of hydrogen oil is 500: 1. -1 , Pressure 2.8MPa.

[0059] After hydrogenation reaction:

[0060] The total sulfur content of the product is 0.2PPM total nitrogen content is less than 0.3PPM liquid -phase catalytic aromatics reactor 99.662%gas phase catalytic pre -hydrogen hydrocarbon rectification feed rate is 99.668%of the pr...

Embodiment 3

[0062] Examples of this embodiment are operated according to Example 1, the difference is:

[0063] In this embodiment, the reaction temperature of the hydrogen hydrogenation reaction of the liquid phase is 135 ° C, the catalyst is CO-MO, the volume ratio of hydrogen oil is 400: 1. -1 , Pressure 2.6MPa;

[0064] The reaction temperature of the gas catalytic pre-hydrogenation reaction is 200 ° C, the catalyst is NI-MO catalyst, the volume ratio of hydrogen oil is 450: 1. -1 , Pressure 2.6MPa;

[0065] The reaction temperature of the main catalytic hydrogenation reaction is 280 ° C, the catalyst is CR-MO catalyst, the volume ratio of hydrogen oil is 450: 1. -1 , Pressure 2.6MPa.

[0066] After hydrogenation reaction:

[0067] The total sulfur content of the product is 0.2PPM total nitrogen content is less than 0.3PPM liquid -phase catalytic aromatics reaction reaction rate of 99.67%gas phase catalytic pre -hydrogen hydrogen reaction aromatics.99.678%.

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Abstract

The present invention provides a crude benzene hydrorefining process, which comprises: sequentially carrying out a liquid phase catalysis pre-hydrogenation reaction, a gas phase catalysis pre-hydrogenation reaction and a main catalysis hydrogenation reaction on crude benzene, and then carrying out extraction rectification on the material obtained from the main hydrogenation reaction to obtain distillates of various distillation ranges. Compared with the process in the prior art, the process of the present invention has the following characteristics that: the catalysis hydrogenation process is adjusted into the three stage catalysis hydrogenation technology, heavy benzol pre-separation is not required before catalysis hydrogenation, and unsaturated olefin in the crude benzene is subjected to hydrogenation at a low reaction temperature of 130-140 DEG C to prepare saturated olefin in the liquid phase catalysis reforming pre-hydrogenation step so as to avoid occurrence of system clogging due to high temperature polymerization coking of easy high temperature polymerization unsaturated olefin contained in the crude benzene in the subsequent step. In addition, heavy benzol in the crude benzene can be subjected to hydrogenation to prepare mixed aromatic hydrocarbons, wherein the mixed aromatic hydrocarbons can be used as excellent blending components, and material output values and added values are increased.

Description

Technical field [0001] The invention involves a kind of coarse benzene hydrogen refinement. Background technique [0002] After entering the 21st century, with the development of organic synthetic industries, the demand for industrial pure benzene has become increasingly larger, and the increasing scarce oil resources have severely restricted the output of oil oil benzene.The scorching coarse benzene status as the other source of pure benzene is becoming more and more important.However, due to the improvement of environmental quality, countries around the world have increasingly restrictions on the amount of oil -containing oil products.Coking thick benzene is a kind of light fraction from coal coking gas. The main ingredients are benzene, toluene, and dysrene, and also contain a small amount of non -aromatic hydrocarbon composition.In its purification process, the most important thing is the removal of organic sulfur. [0003] At present, the industry mainly uses a pickled metho...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C7/163C07C15/04
Inventor 刘勇武
Owner 湖北巨邦石油化工有限公司
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