Combined hydrogenation method of producing chemical materials

A chemical raw material, hydrocracking technology, applied in hydrotreating process, petroleum industry, treatment of hydrocarbon oil, etc. process and other problems, to achieve the effect of increasing productivity, small size, and improving economy.

Active Publication Date: 2013-04-24
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

The patent does not mention the specific distillation range of middle distillates,

Method used

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  • Combined hydrogenation method of producing chemical materials
  • Combined hydrogenation method of producing chemical materials
  • Combined hydrogenation method of producing chemical materials

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Experimental program
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Effect test

Embodiment 1

[0052] In the wax oil hydrocracking unit, the reaction pressure is 13.0MPa, the reaction temperature of the hydrofinishing reactor is 370°C, and the volume space velocity is 1.0h -1 ; The reaction temperature of the first hydrocracking reactor is 366°C, and the volume space velocity is 1.4h -1 ; The temperature of the second hydrocracking reactor in the diesel hydrotreating unit is 405°C and the volume space velocity is 10.0h -1 1. Under the reaction condition of reaction pressure 8.0MPa, with the method provided by the invention, adopt raw material A to carry out experiment. Among them, 100% of the diesel fraction (175-320° C.) obtained from the first hydrocracking reactor was re-refined to the second hydrocracking reactor under pressure. The distribution of the test products and the properties of the main products are shown in Table 2.

[0053] As can be seen from Table 2, under the condition of > 350 DEG C conversion rate is about 57%, the productive rate of heavy naphtha ...

Embodiment 2

[0055] Adopt the method provided by the present invention, control > 350 ℃ conversion rate about 79%, under reaction pressure 13.0MPa, hydrogenation reactor reaction temperature 370 ℃, volume space velocity 1.0h -1 ; The reaction temperature of the first hydrocracking reactor is 376°C, and the volume space velocity is 1.4h -1 Under the condition, with the method provided by the invention, adopt raw material A to carry out experiment. 50% of the 175-320°C diesel fraction is recycled to the inlet of the second hydrocracking reactor, the reaction temperature of the second hydrocracking reactor is 385°C, and the volume space velocity is 4.5h -1 . The distribution of test products and the properties of main products are shown in Table 3. It can be seen from Table 3 that under the condition of >350°C conversion rate of about 79%, the yield of heavy naphtha obtained by back refining can reach 39.1%, the selectivity of heavy naphtha is 84.6%, and the aromatic potential is 64.0%. In ...

Embodiment 3

[0057] Adopt the method provided by the present invention, control > 350 ℃ conversion rate about 78%, under reaction pressure 13.0MPa, hydrogenation reactor reaction temperature 370 ℃, volumetric space velocity 1.0h -1 ; The reaction temperature of the first hydrocracking reactor is 376°C, and the volume space velocity is 1.4h -1 Under the condition, with the method provided by the invention, adopt raw material A to carry out experiment. Among them, 100% of the 175-320°C diesel fraction is recycled to the inlet of the second hydrocracking reactor, the reaction temperature of the second hydrocracking reactor is 406°C, and the volume space velocity is 9.0h-1 , product distribution and product quality data of heavy naphtha are listed in Table 4. It can be seen from Table 4 that under the condition of >350°C with a conversion rate of about 78%, the yield of heavy naphtha obtained by back refining can reach 48.15%, the selectivity of heavy naphtha is 85.1%, and the aromatic potenti...

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Abstract

The invention discloses a combined hydrogenation method of producing chemical materials. The method comprises the steps of: mixing hydrocracking material oil with hydrogen, and then entering a mixture into a hydrorefining reactor and a first hydrocracking reactor by adopting a once serial process; further cracking 10-100% diesel fraction with the temperature of 175-320 DEG C in the second hydrocracking reactor which is arranged in a diesel refining unit, wherein the cracked oil is a mixed fraction of naphtha and diesel; and further fractioning the mixed fraction in a fractionating system of the diesel refining device to obtain light naphtha, high-aromatic latent heavy naphtha and the diesel fraction. By adopting the method disclosed by the invention, the hydrocracking device and the diesel refining device are combined to produce the chemical material; and the reaction pressure of the diesel refining device is low and middle pressure, and improvement of the aromatic latent of the heavy naphtha and reduction of hydrogen consumption are facilitated in the second hydrocracking process.

Description

technical field [0001] The invention belongs to a method for obtaining cracked hydrocarbon oil in the presence of hydrogen, more specifically, a method for producing chemical raw materials by combining hydrocracking and diesel hydrofinishing. Background technique [0002] The reforming unit is an important secondary processing unit in a refinery, used to produce high-octane gasoline blending components or to produce aromatic hydrocarbon base materials. Reformed gasoline has the characteristics of high octane number, no olefins, no sulfur and nitrogen impurities, and is a high-quality gasoline blending component. Compared with European and American countries, reformed gasoline components in the current domestic gasoline composition are relatively small, while catalytic cracking gasoline components account for a relatively high proportion, resulting in high sulfur and olefin content in domestic commodity gasoline and relatively low aromatic content; increase gasoline pool The...

Claims

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Application Information

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IPC IPC(8): C10G67/00
Inventor 赵阳董建伟陈元君胡志海王子文董松涛龙湘云聂红
Owner CHINA PETROLEUM & CHEM CORP
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