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Diesel hydrogenation process

A technology for hydroprocessing and diesel oil, which is applied in the fields of hydroprocessing technology, petroleum industry, and hydrocarbon oil treatment. It can solve the problems of complex process and high energy consumption, and achieve the effects of simplifying the process, reducing energy consumption and difficulty of operation

Active Publication Date: 2015-03-11
SOUTH CHINA UNIV OF TECH
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] The purpose of the present invention is to overcome the disadvantages of complex process flow and high energy consumption of the existing diesel oil hydrogenation treatment process, and provide a diesel oil that integrates hydrogen sulfide stripping of the reaction product and product separation, and assists the reaction feed heating furnace to supply heat. Hydrotreating process

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0029] see figure 1 As shown, the diesel hydrotreating process described in this example is as follows: raw diesel oil 1 (120°C, 10.8MPag, 119048kg / h) from the upstream device and hydrogen (75°C, 10.8MPag, 130000Nm 3 / h, 24972kg / h) after mixing, enter the first heat exchanger E1 at 102°C to exchange heat with the hydrogenation reaction product for the second time (334°C, 10MPag, 153625kg / h), and then heat up to 276°C and enter the raw material heating furnace F1. After further raising the temperature to 321°C, it enters the hydrogenation reactor R1 (the effective heat load corresponding to the raw material heating furnace F1 is 7520.1kW). The temperature of the reaction product coming out of the hydrogenation reactor R1 is 368°C, and then the reaction product passes through the fifth heat exchanger E5 to exchange heat with the cold low fraction oil three times (215°C, 1.4MPag, 121816kg / h) and then cools down to 334°C ℃, and then mixed with hydrogen and cooled to 205℃ through...

Embodiment 2

[0031] The difference from Example 1 is the diesel hydrotreating process described in this example. The specific conditions are as follows: Raw diesel oil 1 (120°C, 10.8MPag, 119048kg / h) from the upstream device and hydrogen (75°C, 10.8MPag, 130000Nm 3 / h, 24972kg / h) after mixing, enter the first heat exchanger E1 at 102°C to exchange heat with the hydrogenation reaction product for the second time (334°C, 10MPag, 153625kg / h), and then heat up to 270°C and enter the raw material heating furnace F1. After further raising the temperature to 321°C, it enters the hydrogenation reactor R1 (the effective heat load corresponding to the raw material heating furnace F1 is 8513.6kW). The temperature of the reaction product coming out of the hydrogenation reactor R1 is 368°C, and then the reaction product passes through the fifth heat exchanger E5 to exchange heat with the cold low fraction oil three times (215°C, 1.4MPag, 121816kg / h) and then cools down to 334°C ℃, and then mixed with ...

Embodiment 3

[0033] The difference from Example 1 is the diesel hydrotreating process described in this example. The specific conditions are as follows: Raw diesel oil 1 (120°C, 10.8MPag, 119048kg / h) from the upstream device and hydrogen (75°C, 10.8MPag, 130000Nm 3 / h, 24972kg / h) after mixing, enter the first heat exchanger E1 at 102°C to exchange heat with the hydrogenation reaction product for the second time (334°C, 10MPag, 153625kg / h), and then heat up to 280°C and enter the raw material heating furnace F1. After further raising the temperature to 321°C, it enters the hydrogenation reactor R1 (the effective heat load corresponding to the raw material heating furnace F1 is 6910.7kW). The temperature of the reaction product coming out of the hydrogenation reactor R1 is 368°C, and then the reaction product passes through the fifth heat exchanger E5 to exchange heat with the cold low fraction oil three times (215°C, 1.4MPag, 121816kg / h) and then cools down to 334°C ℃, and then mixed with ...

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Abstract

The invention discloses a diesel hydrogenation process which is proposed based on the actual situations that in the diesel hydrogenation process, only diesel oil is a unique target product and needs to be subjected to strict quality index control, naphtha generally enters a catalytic reforming preprocessing section, sulfur-containing oil gas is generally fed to an adjacent absorption and stabilization system or a light hydrocarbon recovery device, and both the naphtha and the sulfur-containing oil gas have corresponding downstream processing means, so that the product quality does not need to be strictly controlled. By integrating a reaction product-hydrogen sulfide stripping tower with a product fractionating tower, single-tower running in the diesel hydrogenation process is achieved, and by arranging a fifth heat exchanger for exchanging heat with a reaction product for one time and exchanging heat with low oil for three times, heat integration of a reaction subsystem and a distillation subsystem is achieved, and that a reboiler furnace is started or stopped by a distillation system is made possible.

Description

technical field [0001] The invention relates to the technical field of diesel processing technology, in particular to a diesel hydroprocessing technology. Background technique [0002] Catalytic hydrogenation is of great significance to increase the depth of crude oil processing, rationally utilize petroleum resources, improve oil quality, increase light oil yield and reduce air pollution. The catalytic hydrogenation process is a general term for the catalytic processing of petroleum distillates under the condition of hydrogen. At present, the hydrogenation process adopted by the refinery is generally divided into three types according to the reaction depth from low to high: hydrorefining, hydroupgrading and hydrocracking. The reaction depth of diesel hydrogenation generally does not exceed that of upgrading, so there are two types: upgrading and refining, and its products are mainly diesel, naphtha (or gasoline) and sulfur-containing oil and gas. [0003] At present, the ...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G67/02
Inventor 李国庆姚振宇
Owner SOUTH CHINA UNIV OF TECH
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