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Hydrocarbon hydrogenation conversion process combined method

A combined method and hydroconversion technology, which is applied in the combination of hydrocarbon hydroconversion process, petroleum-based hydrocarbon hydrofinishing process and coal tar-based hydrocarbon hydroconversion process, and can solve problems such as technical solutions that have not been reported.

Inactive Publication Date: 2011-08-10
何巨堂
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0009] Technical scheme of the present invention has no report

Method used

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  • Hydrocarbon hydrogenation conversion process combined method

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0131] The annual start-up time of the device is calculated as 8000 hours / year.

[0132] In the first hydrogenation reaction process, the hydrocarbon feedstock F1 has a petroleum-based delayed coking diesel oil with a boiling range of 180-360° C., the sulfur content of F1 is 0.870% by weight, the nitrogen content is 0.12% by weight, and the F1 flow rate is 45t / h (20°C). The volume flow rate is 52.3m 3 / h), F1 hydrorefining reaction Desulfurization, denitrification, aromatic saturation and other reactions are carried out in a reactor using two hydrorefining catalyst beds, and the sulfur content of the produced hydrorefining diesel is less than 100PPm. The first hydrogenation reaction conditions are: the temperature is 320~370 ℃, the pressure is the medium pressure condition of 6.4~8.0MPa, the unit hydrogen consumption (including dissolved hydrogen) of the raw material hydrocarbon in this hydrorefining process is 1.05% (5253Nm 3 / h, ), the volume ratio of hydrogen to oil at the...

Embodiment 2

[0146] Based on Example 1, the first hydrocarbon feedstock F processed by the first reaction part of the present invention is narrow-cut diesel fuel in the fractionation part of the second reaction effluent, the narrow-cut diesel having a boiling range of 170-350° C. and a sulfur content of 3PPm (weight) , nitrogen content 8PPm (weight), aromatic content 43% (weight), cetane number 27, F1 flow rate 35t / h (20 ℃ volume flow rate 39.8m 3 / h), the F1 hydrorefining reaction is carried out in a reactor using 2 precious metal hydrogenation deep dearomatization catalyst beds to carry out reactions such as aromatic saturation, and the volume concentration of hydrogen sulfide in the first reaction part of the reaction gas is lower than 2PPm; The sulfur content of hydrorefined diesel is less than 1PPm, the nitrogen content is less than 1PPm, the aromatics content is less than 5%, and the cetane number is about 37. The first hydrogenation reaction conditions are: a high pressure condition...

Embodiment 3

[0150] Based on Example 1, the first hydrocarbon feedstock F processed by the first reaction part of the present invention is narrow-cut diesel fuel in the fractionation part of the second reaction effluent, the narrow-cut diesel having a boiling range of 170-335° C. and a sulfur content of 3PPm (weight) , nitrogen content 8PPm (weight), aromatic content 42% (weight), cetane number 31, F1 flow rate 29t / h (20 ℃ volume flow rate 33.1m 3 / h), the F1 hydrorefining reaction is carried out in a reactor using 2 precious metal hydrogenation deep dearomatization catalyst beds to carry out reactions such as aromatic saturation, and the volume concentration of hydrogen sulfide in the first reaction part of the reaction gas is lower than 2PPm; The sulfur content of hydrorefined diesel is less than 1PPm, the nitrogen content is less than 1PPm, the aromatics content is less than 5%, and the cetane number is about 38. The first hydrogenation reaction conditions are: the temperature is 260~34...

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Abstract

The invention relates to a hydrocarbon hydrogenation conversion process combined method which comprises steps as follows: a first reaction effluent E1 obtained by new hydrogen FH and a first hydrocarbon raw material F1 at a first reaction part R1 is separated into a first cold high-pressure hydrogen-rich gas V1 and a first cold high-pressure hydrocarbon liquid L1 at a first cold high-pressure separation part S1; at least part of V1 enters a second reaction part R2 for treating a second hydrocarbon raw material F2; and a second reaction effluent E2 is separated into a second cold high-pressure hydrogen-rich gas V2 and a second cold high-pressure hydrocarbon liquid L2 at a second cold high-pressure separation part S2. The invention also comprises the step of recovering dissolved hydrogen in the L2. The invention has obvious effects of saving the step of high-pressure operation, reducing the hydrogen consumption and the like, is suitable for the combination of a medium / low-pressure low-hydrogen-consumption hydrocarbon hydrogenation process (such as petroleum-based gasoline / diesel hydrofining, wax oil hydrodesulfurization or low-sulfur diesel hydrogenation and aroma removal process) and a high-pressure high-hydrogen-consumption hydrocarbon hydrogenation process (such as coal tar hydrogenation process).

Description

technical field [0001] The present invention relates to a combined method of hydrocarbon hydroconversion processes; in particular, the present invention relates to a combined method of hydrocarbon hydroconversion processes with relatively large differences in hydrogen consumption during the reaction process; more particularly, the present invention relates to a petroleum-based hydroconversion process A combined method of a hydrocarbon hydrorefining process and a coal tar based hydrocarbon hydroconversion process. Background technique [0002] As is well known, the hydrocarbon hydroconversion process is a hydrogen-consuming conversion process of a hydrocarbon feedstock in the presence of hydrogen. The hydrocarbon feedstock can be hydrocarbons from petroleum or kerogen shale or oil sands or coal. The fractions of feedstock hydrocarbons range from gasoline, Kerosene, diesel oil, wax oil to residual oil, in most cases, the above-mentioned raw materials contain heteroelements suc...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G67/02
Inventor 何巨堂
Owner 何巨堂
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