A method for hydrogenation and upgrading of high-aromatic diesel oil

A technology for hydrogenation and upgrading of diesel oil, which is applied in the fields of hydrotreating process, petroleum industry, processing of hydrocarbon oil, etc., can solve the problems of low dearomatization rate and unsatisfactory cetane number directly, and achieves simple and good process flow. Hydrogenation effect, the effect of accelerating the reaction rate

Active Publication Date: 2016-04-13
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The process of this method is different from this method, and the dearomatization rate is low, and the cetane number cannot directly meet the requirements of the national standard

Method used

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  • A method for hydrogenation and upgrading of high-aromatic diesel oil
  • A method for hydrogenation and upgrading of high-aromatic diesel oil
  • A method for hydrogenation and upgrading of high-aromatic diesel oil

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0032] Diesel feedstock 1 enters the first hydrogenation reactor, the reaction conditions are: hydrogen partial pressure 6.5MPa, volume space velocity 1.5h -1 , The reaction temperature is 361°C, the volume ratio of hydrogen to oil is 500:1; the effluent enters the second hydrogenation reactor after passing through the gas stripping hydrogen mixer, and the reaction conditions are: hydrogen partial pressure 6.2MPa, volume space velocity 1.1h -1 , The reaction temperature is 248°C, and the volume ratio of hydrogen to oil is 320:1. The raw material oil properties and product properties are listed in Table 2.

[0033] It can be seen from Table 2 that the sulfur content of diesel products can be reduced to less than 10 μg / g, the aromatics content is greatly reduced, and the cetane number is increased by more than 20 units, directly meeting the requirements of the national standard clean diesel oil.

Embodiment 2

[0035] Diesel feedstock 2 enters the first hydrogenation reactor, the reaction conditions are: hydrogen partial pressure 6.8MPa, volume space velocity 1.6h -1 , The reaction temperature is 364°C, the volume ratio of hydrogen to oil is 450:1; the effluent enters the second hydrogenation reactor after passing through the gas stripping hydrogen mixer, and the reaction conditions are: hydrogen partial pressure 6.5MPa, volume space velocity 1.2h -1 , The reaction temperature is 234° C., and the volume ratio of hydrogen to oil is 300:1. The raw material oil properties and product properties are listed in Table 3.

[0036] It can be seen from Table 3 that the sulfur content of diesel products can be reduced to less than 10 μg / g, the aromatics content is greatly reduced, and the cetane number is increased by more than 20 units, which directly meets the requirements of the national standard clean diesel oil.

Embodiment 3

[0038] Diesel raw material 3 enters the first hydrogenation reactor, and the reaction conditions are: hydrogen partial pressure 6.6MPa, volume space velocity 1.3h -1 , The reaction temperature is 368°C, the volume ratio of hydrogen to oil is 550:1; the effluent enters the second hydrogenation reactor after passing through the gas stripping hydrogen mixer, and the reaction conditions are: hydrogen partial pressure 6.4MPa, volume space velocity 1.0h -1 , The reaction temperature is 257°C, and the volume ratio of hydrogen to oil is 340:1. The raw material oil properties and product properties are listed in Table 4.

[0039] It can be seen from Table 4 that the sulfur content of diesel products can be reduced to less than 10 μg / g by using this technology, the aromatics content is greatly reduced, and the cetane number is increased by more than 20 units, directly meeting the requirements of the national standard for clean diesel.

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Abstract

The invention relates to a method for hydro-upgrading high aromatic diesel oil, comprising the following steps: adding raw material oil and hydrogen in a first reactor through a heating furnace, then contacting with a hydrogenation catalyst under the condition of hydrofining to carry out a routine hydrofining reaction, letting a reaction effluent enter a gas stripping hydrogen mixing device, removing hydrogen sulfide and ammonia dissolved in the oil, and letting hydrogen in the oil reach a dissolved saturation status, then letting the processed reaction effluent and supplemental hydrogen enter a second reactor to contact with a noble metal hydrogenating catalyst, and carrying out deep dearomatization reaction to obtain a good effect. The method aims at low quality catalytic diesel oil distillates of petrochemical enterprises or high aromatic hybrid diesel oil distillates. According to the method, ultra low sulfur clean diesel having a sulfur content of less than 10 mu g / g can be produced, and the cetane number of the product can directly satisfy the requirements of national standard.

Description

technical field [0001] The invention relates to a method for hydrogenation and upgrading of diesel oil with high aromatic content, in particular to a process method for hydrogenation of diesel fractions which needs to greatly increase the cetane number. Background technique [0002] With the increasingly stringent requirements of environmental protection laws and regulations around the world, the indicators of diesel for vehicles are becoming more and more stringent. In addition to the increasingly stringent regulations on the content of impurities such as sulfur and nitrogen, the requirements on the content of aromatics are also more stringent. European and American automobile emission standards stipulate that the content of polycyclic aromatic hydrocarbons in diesel is not more than 11v%, and the cetane number is not less than 51. In recent years, with the continuous attention of the Chinese government to environmental protection, the quality requirements for vehicle dies...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G65/08
Inventor 徐大海李扬刘继华丁贺牛世坤李士才
Owner CHINA PETROLEUM & CHEM CORP
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