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Method for producing diesel oil or diesel oil blending component

A technology for blending components and diesel oil, which is applied in the petroleum industry, hydrocarbon oil treatment, hydrotreating process, etc., can solve the problems of low density, low cetane number, low sulfur and nitrogen content, etc., and achieves moderate reaction conditions, The effect of reducing operating costs

Active Publication Date: 2010-12-29
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0010] Liquid hydrocarbons prepared by Fischer-Tropsch synthesis have the advantage of extremely low sulfur and nitrogen content, and the cetane number of diesel oil can reach more than 70-80, but its density is low, generally lower than 0.78g / cm 3 , can not be directly used as diesel for vehicles, but can only be used as a blending component
Coal direct liquefaction is another way of coal to oil, but the quality of direct coal liquefaction oil is very poor, the cetane number of diesel fraction is very low, generally lower than 30, it is difficult to produce high quality under conventional hydro-upgrading conditions diesel fuel

Method used

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  • Method for producing diesel oil or diesel oil blending component

Examples

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Embodiment 1

[0038] Fischer-Tropsch synthetic oil and coal direct liquefied oil are mixed according to the ratio of 30:70 to obtain stock oil A, whose properties are shown in Table 2. According to the method provided by the present invention, the hydrotreating and upgrading of the mixed oil is carried out, and the feed amount of the mixed oil is 123g / h.

[0039] The operating conditions of the hydrofining reaction zone are: temperature 320°C, hydrogen partial pressure 6.4MPa, hydrogen-to-oil volume ratio 450.

[0040] The operating conditions of the hydroisomerization cracking reaction zone are: temperature 365°C, hydrogen partial pressure 6.4MPa, hydrogen to oil volume ratio 800.

[0041] The temperature range of fractionation tower B cutting distillate oil is: naphtha fraction I is 340°C.

[0042] The temperature range of fractionation tower D cutting distillate oil is: naphtha fraction II is 370°C.

[0043] Diesel oil fraction I and diesel oil fraction II of fractionation tower B and ...

Embodiment 2

[0045] Fischer-Tropsch synthetic oil and coal direct liquefied oil are mixed according to the ratio of 50:50 to obtain raw oil B, its properties are shown in Table 2, and the hydrotreating and upgrading of the mixed oil is carried out according to the method provided by the present invention, and the feed amount of the mixed oil is 138g / h.

[0046] The operating conditions of the hydrofining reaction zone are: temperature 315°C, hydrogen partial pressure 6.4MPa, hydrogen to oil volume ratio 400.

[0047] The operating conditions of the hydroisomerization cracking reaction zone are: temperature 365°C, hydrogen partial pressure 6.4MPa, hydrogen to oil volume ratio 800.

[0048] The temperature range of fractionation tower B cutting distillate oil is: naphtha fraction I is 330°C.

[0049] The temperature range of fractionation tower D cutting distillate oil is: naphtha fraction II is 370°C.

[0050] Diesel fraction I and diesel fraction II of fractionation tower B and fractiona...

Embodiment 3

[0052] Fischer-Tropsch synthetic oil and coal direct liquefied oil are mixed according to the ratio of 80:20 to obtain raw material oil C, whose properties are shown in Table 2. According to the method provided by the present invention, the hydrotreating and upgrading of the mixed oil is carried out, and the feed amount of the mixed oil is 150g / h.

[0053] The operating conditions of the hydrofining reaction zone are: temperature 310°C, hydrogen partial pressure 6.0MPa, hydrogen-to-oil volume ratio 400.

[0054] The operating conditions of the hydroisomerization cracking reaction zone are: temperature 365°C, hydrogen partial pressure 6.0MPa, hydrogen to oil volume ratio 800.

[0055] The temperature range of fractionation tower B cutting distillate oil is: naphtha fraction I is 320°C.

[0056] The temperature range of fractionation tower D cutting distillate oil is: naphtha fraction II is 370°C.

[0057] Diesel fraction I and diesel fraction II of fractionation tower B and f...

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Abstract

The invention discloses a method for producing diesel oil or a diesel oil blending component. The method comprises the following steps of: mixing Fischer-Tropsch synthetic oil and direct coal liquefaction oil to obtain mixed oil; and performing hydrofining and hydrogenation isocracking on the mixed oil and performing fractionation to obtain a diesel oil product or the diesel oil blending component. In the method provided by the invention, two types of oil prepared from coal can be transformed into clean diesel oil which is accordant with a European IV standard or the diesel oil blending component with a large cetane number. Compared with hydrogenation modification of the direct coal liquefaction oil, the method has the advantages of temperate reaction condition, low device investment costand low operation cost.

Description

technical field [0001] The present invention relates to a method for producing diesel or diesel blending components from oil produced from coal. More specifically, it is a method for producing diesel oil or diesel blending components from direct coal liquefied oil and coal indirect liquefied oil in the presence of hydrogen. Background technique [0002] The rapid development of my country's national economy has a strong demand for energy. Since my country became a net importer of oil in 1993, the gap between oil supply and demand has expanded year by year, and the dependence on foreign crude oil has increased year by year. In 2006, the foreign dependence of crude oil was 43%. It is more than 46% in 2020 and is expected to reach 60% in 2020. Fluctuations and changes in the international oil market will directly affect the security and stability of our country's economy and politics. Solving the supply and demand problem of liquid fuels by synthesizing liquid fuels through no...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G65/12
Inventor 吴昊董建伟胡志海聂红张毓莹蒋东红董松涛
Owner CHINA PETROLEUM & CHEM CORP
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