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Method for producing jet fuel or jet fuel blending component

A technology of jet fuel and blending components, which is applied in the petroleum industry, hydrotreating process, hydrocarbon oil treatment, etc., can solve the problems of low smoke point, high smoke point, unsatisfactory density, etc., to reduce operating costs, react The effect of easing conditions

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

Problems solved by technology

[0008] The kerosene fraction obtained by upgrading Fischer-Tropsch synthetic oil has the characteristics of low density and high smoke point, and the density is generally lower than 0.76g / cm 3 , the smoke point is higher than 40mm. Although the smoke point is high, the density cannot meet the requirements of jet fuel density greater than 0.775g / cm 3 Requirements; diesel oil obtained by direct liquefied oil modification of coal has the characteristics of high density and low smoke point, and the density is generally higher than 0.84g / cm 3 , although the density meets the requirements of jet fuel, the smoke point is generally lower than 20mm, which cannot meet the requirement of jet fuel greater than 25mm
Neither modified kerosene meets jet fuel standards

Method used

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  • Method for producing jet fuel or jet fuel blending component

Examples

Experimental program
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Effect test

Embodiment 1

[0036] Fischer-Tropsch synthetic oil and direct coal liquefied oil are mixed according to the ratio of 30:70 to obtain raw oil A, whose properties are shown in Table 2, and the hydrogenation and upgrading of the mixed oil is carried out according to the aforementioned process flow, and the feed amount of the mixed oil is 123g / h.

[0037] The operating conditions of the hydrofining reaction zone are: temperature 320°C, hydrogen partial pressure 11.0MPa, hydrogen to oil volume ratio 450.

[0038] The operating conditions of the hydroisomerization cracking reaction zone are: temperature 365°C, hydrogen partial pressure 11.0MPa, hydrogen to oil volume ratio 800.

[0039] The temperature range of fractionation tower B cutting distillate oil is: naphtha fraction I is 350°C.

[0040] The temperature range of fractionation tower D cutting distillate oil is: naphtha fraction II is 350°C.

[0041] The properties of kerosene 1 obtained by mixing kerosene fraction I and kerosene fracti...

Embodiment 2

[0043] Fischer-Tropsch synthetic oil and direct coal liquefaction oil were mixed according to the ratio of 50:50 to obtain raw material oil B, whose properties are shown in Table 2. Hydrogenation and upgrading of the mixed oil was carried out according to the aforementioned process flow, and the feed amount of the mixed oil was 138g / h.

[0044] The operating conditions of the hydrofining reaction zone are: temperature 315°C, hydrogen partial pressure 9.5MPa, hydrogen-to-oil volume ratio 400.

[0045] The operating conditions of the hydroisomerization cracking reaction zone are: temperature 365°C, hydrogen partial pressure 9.5MPa, hydrogen to oil volume ratio 800.

[0046] The temperature range of fractionation tower B cutting distillate oil is: naphtha fraction I is 350°C.

[0047] The temperature range of fractionation tower D cutting distillate oil is: naphtha fraction II is 350°C.

[0048] The properties of the kerosene 2 obtained by mixing the kerosene fraction I and th...

Embodiment 3

[0050] Fischer-Tropsch synthetic oil and direct coal liquefaction oil were mixed according to the ratio of 80:20 to obtain raw oil C, whose properties are shown in Table 2, and the hydrogenation and upgrading of the mixed oil was carried out according to the aforementioned process flow, and the feed amount of the mixed oil was 150g / h.

[0051] The operating conditions of the hydrofining reaction zone are: temperature 310°C, hydrogen partial pressure 9.0MPa, hydrogen-to-oil volume ratio 400.

[0052] The operating conditions of the hydroisomerization cracking reaction zone are: temperature 365°C, hydrogen partial pressure 9.0MPa, hydrogen to oil volume ratio 800.

[0053] The temperature range of fractionation tower B cutting distillate oil is: naphtha fraction I is 350°C.

[0054] The temperature range of fractionation tower D cutting distillate oil is: naphtha fraction II is 350°C.

[0055] The properties of the kerosene 3 obtained by mixing the kerosene fraction I and the...

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Abstract

The invention discloses a method for producing a jet fuel or a jet fuel blending component. A mixed oil is obtained by mixing a Fischer-Tropsch synthesis fuel and a direct coal liquefaction oil; and the jet fuel or jet fuel blending component is obtained by hydrorefining, hydrocracking, isocracking and fractionating the mixed oil. According to the method provided by the invention, two prepared coal oils can be converted into the high-quality jet fuel or jet fuel blending component. Compared with hydro-upgrading of the direct coal liquefaction oil, the method has the advantages of mild reaction conditions, low device investment cost and low operation cost.

Description

technical field [0001] The present invention relates to a method for producing jet fuel or jet fuel blending components from oil obtained from coal. More specifically, it is a method of producing jet fuel or jet fuel 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...

Claims

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Application Information

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IPC IPC(8): C10G65/12
Inventor 吴昊胡志海董建伟聂红张毓莹蒋东红董松涛
Owner CHINA PETROLEUM & CHEM CORP
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