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Method for producing naphtha and clean gasoline by catalytic cracking diesel oil

A technology for catalytic cracking of diesel oil and naphtha, which is applied in the fields of hydrocarbon oil treatment products, petroleum industry, treatment of hydrocarbon oil, etc., can solve the problems of large volume of hydrocracking reactor, decreased activity of cracking catalyst, large catalyst loading, etc. To achieve the effect of long operation cycle of the device, effective utilization and low nitrogen content

Active Publication Date: 2016-06-22
CHINA NAT OFFSHORE OIL CORP +3
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

For the presence of sulfur and nitrogen compounds in catalytic cracking diesel raw materials, hydrogen sulfide and ammonia are generated after hydrofining, and the effluent from the hydrofinishing reactor directly enters the hydrocracking reactor. Due to the existence of basic nitrogen compounds and ammonia, it will definitely affect the The acidic center of the hydrocracking catalyst leads to a decrease in the activity and stability of the cracking catalyst
In order to ensure the yield of naphtha, the distillation range of the refractory fraction is generally controlled at less than 300°C; at the same time, based on the sum of the fresh feed and the refractory fraction, in order to ensure the conversion rate of the cracking section, the volume of the hydrocracking reactor is large and the catalyst loading Large quantity, resulting in large equipment investment

Method used

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  • Method for producing naphtha and clean gasoline by catalytic cracking diesel oil
  • Method for producing naphtha and clean gasoline by catalytic cracking diesel oil
  • Method for producing naphtha and clean gasoline by catalytic cracking diesel oil

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0048] According to the method of the invention, catalytic cracking diesel oil is processed to produce naphtha and clean gasoline products.

[0049] Catalytic cracking diesel oil I is used as raw material, mixed with new hydrogen and circulating hydrogen, and then enters the middle part of the reverse sequence series hydrocracking-hydrofining high-pressure hydrogenation unit, and then enters the second-stage hydrofinishing reactor downward. The hydrorefining catalyst loading capacity of the hydrorefining section is 200mL, and the hydrocracking catalyst loading volume of the hydrocracking section is 200mL. After gas-liquid separation, the hydrofinishing product enters the continuous distillation unit and cuts the fractions. After the distillate oil at 205-320°C is returned and mixed with new hydrogen and circulating hydrogen, it enters the hydrocracking-hydrofining high-pressure hydrogenation unit in reverse series The first hydrocracking reactor at the top, and then through th...

Embodiment 2～5

[0052] FCC diesel I and FCC diesel II were processed respectively according to the method steps of Example 1, the difference was the choice of reaction conditions, the selected test conditions are shown in Table 2.

[0053] The properties of different distillate oil products are shown in Table 3 to Table 4, and the yields of different distillate oil products are shown in Table 5.

[0054] Table 2 Test conditions

[0055]

[0056] Table 365~165℃ naphtha properties

[0057] project

Example 1

Example 2

Example 3

Example 4

Example 5

Density(20℃),g / cm 3

0.705

0.701

0.730

0.728

0.732

Sulfur content, μg / g

0.3

0.2

0.2

0.2

0.2

Nitrogen content, μg / g

0.2

0.1

0.1

0.1

0.2

Aromatics, mass%

35.1

33.2

40.8

40.5

42.6

Cycloalkane, mass%

40.1

42.6

44.2

44.1

41.3

[0058] Table 4165~205℃ distillate oil properties

[005...

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Abstract

The invention provides a method for producing naphtha and clean gasoline by catalytic cracking diesel oil. The method comprises the following steps of mixing the catalytic cracking diesel oil and hydrogen gas; enabling the mixture to enter the middle part of a reverse sequence filling hydrocracking reactor-hydrofining reactor to be mixed with cracking products from the hydrocracking reactor; enabling the mixture to enter the hydrofining reactor to perform a hydrofining reaction so as to remove impurities such as sulfur and nitrogen; performing an olefin saturated reaction and arene hydrogenation saturation; performing cutting processing on products after the hydrofining; using distillate oil below 165 DEG C as a naphtha product to be used as a raw material for a catalytic reforming unit; using distillate oil being 165 to 205 DEG C as a clean gasoline conditioning ingredient; returning distillate oil being 205 to 320 DEG C into the top of the reverse sequence filling hydrocracking reactor-hydrofining reactor; performing hydrocracking and hydrofining reactions; returning distillate oil being higher than 320 DEG C into a catalytic cracking device for further cracking, or enabling the distillate oil being higher than 320 DEG C to enter other hydrogenation devices for processing treatment. The method has the advantages that high yield of naphtha products is taken as the goal; the clean gasoline can be produced at the same time.

Description

technical field [0001] The invention is a method for producing naphtha and clean gasoline by using catalytic cracking diesel oil. Background technique [0002] Under the situation of developing low-carbon economy, circular economy and achieving sustainable development, the pace of upgrading the quality of oil products in my country has been significantly accelerated, and the requirements for the content of aromatics in diesel are becoming more and more stringent. The production of clean oil products has become one of the key points in the development of my country's oil refining industry. In my country's diesel composition, 25-30% is FCC diesel. FCC diesel has the characteristics of high aromatics content (aromatics content generally > 60%), low cetane number, and its quality is poor. It must be hydrorefined or hydro-upgraded before it can be used as a fuel oil blending component. However, the cost of hydro-upgrading operation is high, the conditions are harsh, and the ...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G65/12
CPCC10G65/12C10G2300/202C10G2300/301C10G2400/02
Inventor 于海斌南军于群刘艳冯俊发张鹏张景成臧甲忠耿姗张玉婷肖寒朱金剑张国辉宋国良张尚强王帅
Owner CHINA NAT OFFSHORE OIL CORP
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