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A method of hydrocracking

A hydrocracking and hydrogenation reaction technology, applied in the field of hydrocracking, can solve the problems of insufficient heavy naphtha yield to meet product demand, high light naphtha or light hydrocarbon yield, and increased device complexity. , to achieve the effect of excellent quality, small investment in equipment and increased yield

Active Publication Date: 2022-04-12
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0019] (1) The yield of heavy naphtha under the one-pass process is not enough to meet the product demand of the enterprise;
[0020] (2) After ensuring that the yield of heavy naphtha meets the requirements of the enterprise, the yield of light naphtha or light hydrocarbons is relatively high;
[0022] (4) Circulating diesel oil or middle distillate oil to the second cracking reactor is equivalent to adding a section of hydrocracking unit, requiring additional reactors and circulating hydrogen systems, increasing the complexity of the device and increasing the investment

Method used

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  • A method of hydrocracking

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specific Embodiment approach

[0079] The following combination figure 1 A preferred embodiment of the hydrocracking method of the present invention is provided, the method comprising:

[0080] (1) Enter VGO fraction 1 and hydrogen into high-pressure reaction zone 3 to carry out the first hydrogenation reaction to obtain effluent I;

[0081] (2) introducing hydrogen, raw diesel oil 2 and the effluent I into the low-pressure reaction zone 4 to carry out the second hydrogenation reaction to obtain the effluent II;

[0082] (3) introducing the effluent II into the separation and fractionation unit 5 for fractionation to obtain a light naphtha fraction 6, a heavy naphtha fraction 7, a diesel fraction 8 and a tail oil fraction 9;

[0083] Wherein, the hydrogen partial pressure in the low-pressure reaction zone 4 is 20-80% of the hydrogen partial pressure in the high-pressure reaction zone 3 .

[0084] Particularly preferably, in the present invention, during the practical production process, while the VGO frac...

Embodiment 1

[0099]Hydrogenation pretreatment catalyst RN-410 and hydrocracking catalyst RHC-210 are used, and hydrogenation pretreatment catalyst RN-410 is filled in the high-pressure reaction zone, and hydrogenation pretreatment catalyst RN-410 is filled in the low-pressure reaction zone in sequence according to the flow direction. 410 and hydrocracking catalyst RHC-210, with the VGO raw material and catalytic diesel oil in Table 1 as the feed, the mass fraction of VGO and catalytic diesel oil in the total feed is 50%, wherein the VGO raw material enters the high-pressure reaction zone, and the catalytic diesel oil enters Low pressure reaction zone. In the production scheme of embodiment 1 (using figure 1 Shown technological process carries out) obtain light naphtha fraction, heavy naphtha fraction, diesel oil fraction and tail oil fraction under.

[0100] Process conditions, product distribution, and key product properties are listed in Tables 3 and 4.

[0101] table 3

[0102]

...

Embodiment 2

[0111] Hydrogenation pretreatment catalyst RN-410 and hydrocracking catalyst RHC-210 are used, and hydrogenation pretreatment catalyst RN-410 is filled in the high-pressure reaction zone, and hydrogenation pretreatment catalyst RN-410 is filled in the low-pressure reaction zone in sequence according to the flow direction. 410 and hydrocracking catalyst RHC-210, with the VGO raw material and catalytic diesel oil in Table 1 as the feed, the mass fraction of VGO and catalytic diesel oil in the total feed is 50%, wherein the VGO raw material enters the high-pressure reaction zone, and the catalytic diesel oil enters Low pressure reaction zone. In the production scheme of embodiment 2 (using figure 1 Shown technological process carries out) obtain light naphtha fraction, heavy naphtha fraction, diesel oil fraction and tail oil fraction under.

[0112] Process conditions, product distribution, and key product properties are listed in Tables 3 and 4.

[0113] As shown in Table 3 an...

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Abstract

The present invention relates to the field of hydrocracking, and discloses a method for hydrocracking. The method comprises: (1) introducing a VGO fraction into a high-pressure reaction zone to perform a first hydrogenation reaction to obtain effluent I; (2) The raw material diesel oil and the effluent I are introduced into the low-pressure reaction zone for the second hydrogenation reaction to obtain the effluent II; (3) the effluent II is subjected to fractional distillation; wherein, the hydrogen partial pressure in the low-pressure reaction zone It is 20-80% of the hydrogen partial pressure in the high-pressure reaction zone. By adopting the method provided by the invention, the heavy naphtha yield of the hydrocracking unit can be greatly increased, and at the same time, high-quality tail oil can also be produced.

Description

technical field [0001] The invention relates to the field of hydrocracking, in particular to a method for hydrocracking. Background technique [0002] Ethylene is the basic raw material of petrochemical industry. With the development of the national economy, my country's ethylene production capacity has increased rapidly, but it still cannot meet the demand for ethylene in the domestic market, and about half of it depends on imports. Therefore, the development of petrochemical basic raw material olefin production increase technology is a direction of petrochemical industry development. [0003] Hydrocarbon steam cracking is the main means of producing ethylene. In the process of steam cracking to ethylene production, the cost of feedstock oil accounts for a large proportion of the total cost, generally more than 60%. Therefore, the optimal selection of feedstock oil is an important factor affecting the efficiency of ethylene plants. [0004] From a global perspective, ste...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G67/02
CPCC10G67/02
Inventor 赵阳赵广乐毛以朝龙湘云
Owner CHINA PETROLEUM & CHEM CORP