Hydrocracking method for producing chemical materials

A technology for hydrocracking and chemical raw materials, which is applied in the fields of hydroprocessing process, petroleum industry, and hydrocarbon oil treatment, etc. It can solve the problem of reducing the aromatic potential and selectivity of heavy naphtha fractions, affecting the long-term operation of hydrocracking units, Increase the volume of the device and the amount of catalyst, etc., to achieve the effect of low nitrogen content, light distillation range, and difficult dehydrocoking reaction

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

AI Technical Summary

Problems solved by technology

For the hydrocracking unit under the one-pass process, in order to increase the yield of heavy naphtha, the method of increasing the conversion rate can be adopted to convert more heavy fractions into light products, but at the same time it will also lead to the selectivity of heavy naphtha and aroma potential decreased, hydrogen consumption increased
[0005] Adding heavy naphtha can also carry out recycling and refining of all middle distillates. This method can effectively increase the yield of heavy naphtha.

Method used

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  • Hydrocracking method for producing chemical materials
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  • Hydrocracking method for producing chemical materials

Examples

Experimental program
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Effect test

Embodiment 1

[0047] Using the method provided by the present invention, at a reaction pressure of 13.0MPa, a reaction temperature of a hydrotreating reactor of 365°C, and a space velocity of 1.0h -1 ; The reaction temperature of the first hydrocracking reactor is 368°C and the space velocity is 1.5h -1 ; The temperature of the second hydrocracking reactor is 368°C and the space velocity is 1.5h -1 Under the reaction conditions that the volume ratio of hydrogen to oil in a reverse inlet standard state is 1200, the hydrocracking test is carried out using raw material A (the catalyst used in the second hydrocracking reactor is a low metal loading hydrocracking catalyst II). During the test, 50% (accounting for the total volume of diesel fraction at 175-320°C) of the diesel fraction was recycled to the inlet of the second hydrocracking reactor. The test results are shown in Table 2.

[0048] As can be seen from Table 2, under the condition that the first hydrocracking reactor > 350 DEG C conv...

Embodiment 2

[0055]Adopt the method provided by the present invention, control the first hydrocracking reactor > 350 ℃ conversion rate 72%, under reaction pressure 13.0MPa, hydrorefining reactor reaction temperature 365 ℃, space velocity 1.0h -1 ; The reaction temperature of the first hydrocracking reactor is 374°C and the space velocity is 1.5h -1 ; Under the reaction condition that the volume ratio of hydrogen to oil in a reverse inlet standard state is 1200, the hydrocracking test is carried out by using raw material A (the second hydrocracking reactor is filled with hydrocracking catalyst II). 50% of the 175-320°C diesel fraction was recycled to the inlet of the second hydrocracking reactor. The reaction temperature of the second hydrocracking reactor was 370°C. The product distribution and product quality data of heavy naphtha are listed in Table 2. It can be seen from Table 2 that under the conditions of the first hydrocracking reactor>350°C conversion rate of about 72%, the yield of...

Embodiment 3

[0057] Adopt the method provided by the present invention, control first hydrocracking reactor > 350 ℃ conversion rate about 59%, at reaction pressure 13.0MPa, hydrotreating reactor reaction temperature 365 ℃, space velocity 1.0h -1 ; The reaction temperature of the first hydrocracking reactor is 369°C and the space velocity is 1.5h -1 ; Under the reaction condition that the volume ratio of hydrogen to oil in a reverse inlet standard state is 1200, the hydrocracking test is carried out by using raw material A (the second hydrocracking reactor is filled with hydrocracking catalyst II). 100% of the obtained 175-320°C diesel fraction is recycled to the inlet of the second hydrocracking reactor. The reaction temperature of the second hydrocracking reactor is 377°C. The product distribution and product quality data of heavy naphtha are listed in the table 3. It can be seen from Table 3 that under the conditions of the first hydrocracking reactor > 350 °C conversion rate of about 5...

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Abstract

The invention discloses a hydrocracking method for producing chemical materials. The method comprises the steps of: orderly entering material oil and hydrogen into a hydrorefining reactor and a first hydrocracking reactor to react after being mixed; and cooling and separating reactants, and then entering obtained 10-100% of diesel fraction with the temperature of 175-320 DEG C into a second hydrocracking reactor to further react, wherein a hydrocracking catalyst II is a hydrocracking catalyst with low metal content; the metal content of the hydrocracking catalyst II is lower than that of a hydrocracking catalyst I. By adopting the hydrocracking method, the yield and the selectivity of heavy naphtha can be effectively improved; the aromatic latent of the heavy naphtha is improved, and hydrogen consumption is reduced.

Description

technical field [0001] The invention belongs to a method for obtaining cracked hydrocarbon oil in the presence of hydrogen, more specifically, a hydrocracking method for producing chemical raw materials. 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 proportion of medium reformed gasoline...

Claims

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Application Information

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IPC IPC(8): C10G67/02
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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