Hydrocracking method for catalytic cracking diesel

A catalytic cracking diesel and hydrocracking technology, applied in the field of hydrocarbon oil cracking, can solve the problems of little change in diesel density, limited improvement of cetane number, low octane number of naphtha fractions, etc. Alkane number, improvement of hydrocarbon composition, effect of high cetane number

Active Publication Date: 2014-05-07
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Using the conventional hydrorefining process to treat low-quality diesel oil, although it can effectively remove impurities such as sulfur and nitrogen in the diesel oil, the increase in the cetane number of the diesel product is limited, and the density of the diesel

Method used

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  • Hydrocracking method for catalytic cracking diesel
  • Hydrocracking method for catalytic cracking diesel
  • Hydrocracking method for catalytic cracking diesel

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0050] The raw material oil F enters the first reaction zone together with hydrogen, and reacts with the hydrofining catalyst A, and the reaction effluent from the first reaction zone enters the middle high-pressure stripping tower, and hydrogen sulfide and NH are removed by stripping 3 Finally, the liquid product is mixed with the refractory fraction from the fractionation part, and then enters the second reaction zone to contact and react with the hydrocracking catalyst D. The effluent after the reaction is cooled, separated and fractionated to obtain light naphtha fraction, gasoline fraction, recycle fraction and diesel fraction. The refined fraction is a narrow fraction at 200°C to 240°C, in which the total aromatic content of the refined fraction is 75.6% by mass, and the content of single-ring aromatics is 71% by mass. This part of the narrow fraction is all smelted back to the inlet of the second reaction zone. The reaction conditions are shown in Table 2, and the prod...

Embodiment 2

[0053] The raw material oil G enters the first reaction zone together with hydrogen, and contacts and reacts with the hydrotreating catalyst B, and the reaction effluent from the first reaction zone enters the second reaction zone to contact and react with the hydrocracking catalyst D without any intermediate separation. The effluent after the reaction is cooled, separated and fractionated to obtain light naphtha fraction, gasoline fraction, recycle fraction and diesel fraction. Among them, the refractory fraction is a narrow fraction at 200°C to 250°C, in which the total aromatics content of the refractory fraction is 82 mass%, and the single-ring aromatics content is 77 mass%, and this part of the narrow fraction is returned to the entrance of the second reaction zone, and the The effluent from one reaction zone is mixed and then passed to the second reaction zone. The reaction conditions are shown in Table 2, and the product properties are shown in Table 3.

[0054] It can...

Embodiment 3

[0056] The raw material oil G enters the first reaction zone together with hydrogen, and contacts and reacts with the hydrotreating catalyst C, and the reaction effluent from the first reaction zone enters the second reaction zone to contact and react with the hydrocracking catalyst D without any intermediate separation. The effluent after the reaction is cooled, separated and fractionated to obtain light naphtha fraction, gasoline fraction, recycle fraction and diesel fraction. Among them, the refined fraction is a narrow fraction at 200°C to 260°C, wherein the total aromatic content of the refined fraction is 78% by mass, and the content of single-ring aromatics is 72% by mass. And this part of the narrow fraction is returned to the inlet of the second reaction zone, mixed with the effluent of the first reaction zone, and then enters the second reaction zone. The reaction conditions are shown in Table 2, and the product properties are shown in Table 3.

[0057] It can be se...

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Abstract

The invention provides a hydrocracking method for catalytic cracking diesel. According to the method, a mixture of the diesel material and hydrogen is in contact reaction with a hydrorefining catalyst in a hydrorefining reactor, liquid efflux from the hydrorefining reactor is not separated and then enters a hydrocracking reactor to be in contact and react with a hydrocracking catalyst, the reaction efflux from the hydrocracking reactor is subjected to separation and fractional distillation to obtain hydrogen-rich gas, then light naphtha fraction, gasoline fraction, recycle fraction and diesel fraction are performed, in the distillation range of the recycle fraction, the temperature is 190 DEG C to 300 DEG C, and the recycle fraction returns to an inlet of the hydrocracking reactor. The method provided by the invention improves the composition of feed hydrocarbon of the hydrocracking reaction region, and the yield and the octane value of the gasoline fraction are effectively increased.

Description

technical field [0001] The present invention relates to a hydrocarbon oil cracking method for obtaining low-boiling fractions in the presence of hydrogen, more specifically, a process for producing high-octane gasoline components and low-sulfur diesel blending components from diesel raw materials hydrogen method. Background technique [0002] With the aggravation of heavy and inferior crude oil, the quality of FCC diesel is deteriorating and the output is increasing year by year. This part of FCC diesel accounts for about one third of my country's commercial diesel. At present, in order to extract more light oil products from crude oil, refineries continue to improve the processing capacity and processing depth of catalytic cracking units, resulting in further deterioration of the quality of catalytic cracking diesel oil, mainly manifested in high content of aromatics, sulfur and nitrogen, etc. High impurity content, low cetane number. At the same time, with the increasing...

Claims

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Application Information

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IPC IPC(8): C10G67/02
Inventor 张毓莹蒋东红辛靖任亮胡志海聂红
Owner CHINA PETROLEUM & CHEM CORP
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