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Crude benzene hydrorefining process

A technology for hydrorefining and crude benzene, applied in the fields of hydrocarbons, chemical instruments and methods, organic chemistry, etc., can solve the problems of easy coking and clogging of the reaction system, high reaction temperature requirements, and many waste of raw materials, etc. Coking risk, stable reaction process, lower energy consumption and cost savings

Active Publication Date: 2015-12-23
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
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  • Crude benzene hydrorefining process

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0047] 1. The raw material is coking crude benzene, and its components and mass fractions are as follows:

[0048] Benzene: 75%, toluene: 13.9%, xylene: 2.24%, light component: 0.86%, heavy component: 8%, total sulfur content 6546.57ppm, total nitrogen content 899.3ppm.

[0049] 2. In this example, the reaction temperature of the liquid-phase catalytic prehydrogenation reaction is 140°C, the catalyst is Co-Mo, the volume ratio of hydrogen to oil is 500:1, and the volume space velocity is 3h -1 , pressure 2.8MPa;

[0050] The reaction temperature of the gas-phase catalytic prehydrogenation reaction is 190°C, the catalyst is Ni-Mo catalyst, the volume ratio of hydrogen to oil is 400:1, and the volume space velocity is 0.5h -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 to oil is 400:1, and the volume space velocity is 0.5h -1 , Pressure 2.0MPa.

[0052...

Embodiment 2

[0055] The present embodiment is operated by embodiment 1, difference is:

[0056] In this example, the reaction temperature of the liquid-phase catalytic prehydrogenation reaction is 130°C, the catalyst is Co-Mo, the volume ratio of hydrogen to oil is 300:1, and the volume space velocity is 0.1h -1 , pressure 2.4MPa;

[0057] The reaction temperature of the gas-phase catalytic prehydrogenation reaction is 210°C, the catalyst is Ni-Mo catalyst, the volume ratio of hydrogen to oil is 500:1, and the volume space velocity is 5h -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 to oil is 500:1, and the volume space velocity is 5h -1 , Pressure 2.8MPa.

[0059] After hydrogenation reaction:

[0060] The total sulfur content of the product is 0.2ppm and the total nitrogen content is less than 0.3ppm. The retention rate of aromatics in the liquid-phase catalyt...

Embodiment 3

[0062] The present embodiment is operated by embodiment 1, difference is:

[0063] In this example, the reaction temperature of the liquid-phase catalytic prehydrogenation reaction is 135°C, the catalyst is Co-Mo, the volume ratio of hydrogen to oil is 400:1, and the volume space velocity is 2h -1 , pressure 2.6MPa;

[0064] The reaction temperature of the gas-phase catalytic prehydrogenation reaction is 200°C, the catalyst is Ni-Mo catalyst, the volume ratio of hydrogen to oil is 450:1, and the volume space velocity is 3h -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 to oil is 450:1, and the volume space velocity is 3h -1 , Pressure 2.6MPa.

[0066] After hydrogenation reaction:

[0067] The total sulfur content of the product is 0.2ppm and the total nitrogen content is less than 0.3ppm. The retention rate of aromatics in the liquid-phase catalytic...

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Abstract

The invention provides a crude benzene hydrogenation refining process, which is obtained by sequentially performing liquid-phase catalytic pre-hydrogenation reaction, gas-phase catalytic pre-hydrogenation reaction and main catalytic hydrogenation reaction on crude benzene, and then extracting, rectifying and main hydrogenation reaction material, obtained distillates of each distillation range; compared with the prior art, the present invention adjusts the catalytic hydrogenation process to a three-stage hydrogenation technology, and does not need to pre-separate heavy benzene before catalytic hydrogenation; In the hydrogenation process, the unsaturated olefins in the crude benzene are hydrogenated into saturated hydrocarbons at a relatively low reaction temperature of 130~140°C, so as to avoid the unsaturated hydrocarbons contained in the crude benzene that are easy to polymerize at high temperatures in the subsequent process. In the case of high-temperature polymerization coking and blockage of the system; the method can hydrogenate heavy benzene in crude benzene to obtain mixed aromatics, which can be used as high-quality blending components of gasoline and diesel, and the output value and added value of materials can be improved.

Description

technical field [0001] The invention relates to a crude benzene hydrogenation refining process. Background technique [0002] After entering the 21st century, with the development of the organic synthesis industry, the demand for industrial pure benzene is increasing, and the increasing shortage of petroleum resources has seriously restricted the output of petroleum crude benzene. As another source of pure benzene, the status of coking crude benzene is becoming more and more important. However, due to the improvement of environmental quality requirements, countries around the world have increasingly strict restrictions on the sulfur content of oil products. Coking crude benzene is a light distillate oil recovered from coal coking crude gas. Its main components are benzene, toluene, and xylene, and it also contains a small amount of non-aromatic components. In its purification process, the most critical thing is the removal of organic sulfur. [0003] At present, the indus...

Claims

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Application Information

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Patent Type & Authority Patents(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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