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Method of producing jet fuel from coking distillate

A technology for coking distillate oil and jet fuel, which is applied in the petroleum industry, processing hydrocarbon oil, etc., and can solve the problems of complicated operation, difficult realization, and high cost.

Inactive Publication Date: 2004-03-03
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

However, one disadvantage of hydrocracking is that it is more expensive, whether it is equipment investment or operating costs
However, the disadvantage of this technology is that the process is long, the operation is complicated, and it is difficult to realize
However, since the process is a scrubbing / adsorption process that does not change the hydrocarbon composition of the feedstock, the refining effect is not particularly good and jet fuel fractions are not obtained

Method used

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Examples

Experimental program
Comparison scheme
Effect test

preparation example Construction

[0014] The preparation method of this catalyst comprises:

[0015] The precursor of alumina is mixed with zeolite, calcined, impregnated with an aqueous solution containing nickel and / or cobalt and molybdenum and / or tungsten, then dried and calcined, the precursor of alumina is a pore with a diameter of less than 80 angstroms A mixture of the precursor of small-pore alumina whose pore volume accounts for more than 95% of the total pore volume and the precursor of macro-porous alumina whose pore volume accounts for more than 70% of the total pore volume, and small-pore alumina The amount of precursor, macroporous alumina precursor and zeolite makes the weight ratio of small-porous alumina and macroporous alumina in the catalyst 75:25 to 50:50, and the ratio of the total weight of alumina to zeolite is 90: 10 to 50:50, preferably 90:10 to 60:40. The precursor of the small-pore alumina is hydrated alumina with a gibbsite content greater than 60% by weight, and the precursor of t...

Embodiment 1

[0042] Coked diesel and hydrogen enter the hydrogenation reactor, at a hydrogen partial pressure of 6.4MPa, a temperature of 360°C, and a hydrogen-to-oil volume ratio of 700Nm 3 / m 3 , liquid hourly space velocity is 1.0 hours -1 Under certain conditions, contact with hydrogenation catalyst and hydrorefining catalyst RN-10 (the volume ratio of the former to the latter is 4:1) without intermediate separation, and the effluent after the reaction is cooled and separated, and the hydrogen-containing gas is recycled , the liquid product enters the fractionation system and is separated into naphtha fraction, jet fuel fraction and diesel fraction.

[0043] The test results are shown in Table 2. It can be seen from Table 2 that the jet fuel distillate product has a smoke point of 28.2 mm, aromatics of 6.5v%, and a freezing point of <-47°C, which is a qualified 3# jet fuel product.

Embodiment 2

[0045] Coked gasoline and diesel and hydrogen enter the hydrogenation reactor, at a hydrogen partial pressure of 6.4MPa, a temperature of 360°C, and a hydrogen-to-oil volume ratio of 700Nm 3 / m 3 , liquid hourly space velocity is 1.0 hours -1 Under certain conditions, contact with hydrogenation catalyst and hydrorefining catalyst RN-10 (the volume ratio of the former to the latter is 4:1) without intermediate separation, and the effluent after the reaction is cooled and separated, and the hydrogen-containing gas is recycled , the liquid product enters the fractionation system and is separated into naphtha fraction, jet fuel fraction and diesel fraction.

[0046] The test results are shown in Table 2. It can be seen from Table 2 that the smoke point of the jet fuel distillate product is 25.1 mm, the aromatics are 14.9V%, and the freezing point is -48 ° C, which is a qualified 3 # Jet fuel products.

[0047] raw material

[0048] Example 1

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Abstract

A process for preparing the jet fuel from coking distillate features that the coking distillate and hydrocatalyst take part in reaction in the conditions of 3-12 MPa for hydrogen pressure, 300-400 deg.c, 400-1000 Ncu.m / cu.m for H2 / oil ratio, and 0.5-5 / hr for space speed. Said hydrocatalyst is composed of the active component chosen from the metals in VIII or VIB family and the carrier (the mixture of alumina and zeolite).

Description

technical field [0001] This invention pertains to a method of refining hydrocarbon oils in the presence of hydrogen, and more particularly to a method of producing jet fuel from coker distillates. Background technique [0002] With the development of the aviation transportation industry worldwide, the demand for aviation fuel at home and abroad is growing rapidly. By 1999, the annual demand for aviation kerosene in my country had grown to 5 million tons per year. Usually, the production of jet fuel is to obtain the appropriate kerosene fraction from the atmospheric and vacuum device, and then go through hydrogenation or non-hydrogenation refining means for refining, and finally the qualified jet fuel product can be obtained. The amount of jet fuel available from this conventional route is limited and cannot meet the growing demand. Therefore, in order to obtain more high-quality jet fuel products, people have developed the technology of hydrocrackin...

Claims

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Application Information

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IPC IPC(8): C10G49/04
Inventor 蒋东红胡志海王哲陈水银
Owner CHINA PETROLEUM & CHEM CORP
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