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Method for removing olefins from reformate through liquid phase circulation selective hydrogenation

A technology of reforming to generate oil and selectivity, which is applied in the fields of hydrotreating process, petroleum industry, and hydrocarbon oil treatment. It can solve the problems of high equipment construction cost and large cost ratio, and achieve short material contact time and flexible operation. Big, easy-to-process effects

Active Publication Date: 2013-02-06
CHINA NAT OFFSHORE OIL CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The disadvantage of this process is that it is only suitable for reformed gasoline raw materials after removal of heavy components
[0011] When hydrogenation technology is used to generate oil from industrial reforming, the construction cost of the device is high, and the investment in the hydrogen circulation link accounts for a large proportion of the entire process cost

Method used

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  • Method for removing olefins from reformate through liquid phase circulation selective hydrogenation
  • Method for removing olefins from reformate through liquid phase circulation selective hydrogenation
  • Method for removing olefins from reformate through liquid phase circulation selective hydrogenation

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0043] A two-stage series fixed-bed hydrogenation reactor is adopted, and the filling amount of the first reaction catalyst and the second reaction catalyst are both 100 mL. The raw material is the reformed oil from the continuous reformer, the distillation range is 26.2-218.2°C, the aromatic content is 60.5wt%, and the bromine value is 3640mgBr / 100g oil. According to the catalyst E prepared in Example 1 of CN100596285C, the catalyst was pre-reduced in hydrogen at 170°C for 8 hours, and then lowered to the reaction temperature for selective hydrogenation reaction. Control the circulation of product oil into the first and second reactors, the liquid hourly volumetric space velocity of the first and second reactors are 4.0 h respectively -1 , 6.0 h -1 , Process conditions are shown in Table 1-1, and the properties of refined reforming oil are shown in Table 1-2.

[0044] Table 1-1 Process conditions

[0045] Process conditions

Example 1

reactor

Two-stage series

Reacti...

Embodiment 2

[0049] Two-stage series hydrogenation reactors are used, with 80 mL of the first reaction catalyst and 120 mL of the second reaction catalyst. The raw material used is a semi-regenerative fixed-bed reformer to reform the whole oil fraction, the distillation range is 46.2-167.5°C, the aromatic content is 53.4wt%, and the bromine value is 1870mgBr / 100g oil. The catalyst is based on the catalyst A prepared in Example 1 of CN100596285C, reduced in advance in hydrogen at 170°C for 8 hours, and then lowered to the reaction temperature for selective hydrogenation reaction. Control the circulation of product oil into the first and second reactors, the liquid hourly volumetric space velocity of the first and second reactors are 4.0 h respectively -1 , 6.0 h -1 , The process conditions are shown in Table 2-1, and the properties of refined reforming oil are shown in Table 2-2.

[0050] Table 2-1 Process conditions

[0051] Process conditions

Example 2

reactor

Two-stage series

...

Embodiment 3

[0055] A two-stage series hydrogenation reactor is used, and the loading capacity of the first reaction catalyst and the second reaction catalyst are both 100 mL. The raw materials used are the same as in Example 1. The catalyst was pre-reduced in hydrogen at 180° C. for 8 hours according to the catalyst E prepared in Example 1 of CN100596285C, and then lowered to the reaction temperature for long-term stability test. Control the circulation of product oil into the first and second reactors, the liquid hourly volumetric space velocity of the first and second reactors are 4.0 h respectively -1 , 6.0 h -1 , The process conditions are shown in Table 3-1, and the properties of refined reforming oil are shown in Table 3-2.

[0056] Table 3-1 Process conditions

[0057] Process conditions

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Abstract

The invention relates to a method for removing olefins from reformate through liquid phase circulation selective hydrogenation. The method is characterized in that performing hydrogen saturation in a pipeline to form a raw material / hydrogenation product / hydrogen liquid phase mixture, and adding the liquid phase mixture to a multistage conventional hydrogenation reactor in sections under the hydrogenation condition; and entering a catalyst bed area in sections for reaction, wherein part of reaction products discharged from the bottom of the reactor circulate and are mixed with fresh raw materials, and part of reaction products discharged from the reaction system enter a follow-up separating device, the ratio of the circulation volume and the raw materials in the circulating liquid hydrogenation products is 1: (1-5): 1 by volume, the hydrogenation process conditions include that the reaction temperature is 80-180 DEG C, the pressure is 1.5-2.0MPa, and the fresh feed volume space velocity is 2.0-4.0hr-1.

Description

Technical field [0001] The invention belongs to the technical field of hydrorefining of petroleum hydrocarbon products, and more specifically, it relates to a method for selective hydrogenation and deolefination of liquid phase circulation of reformed oil. Background technique [0002] The main function of the process of selective hydrogenation and deolefination of gasoline from catalytic reforming is to carry out selective hydrogenation of reformed oil to remove olefins in the presence of hydrogen, and to achieve deepening without hydrogenation saturation of aromatics. Hydrogenation removes olefins. [0003] After the naphtha fraction is catalytically reformed, the resulting oil is rich in aromatics and solvent oil fractions, and also contains a small amount of olefins. Regarding the reformer units producing chemical grade BTX aromatics, they all face the problem of how to remove olefins in the reformed oil. Because to produce qualified chemical raw material aromatic products an...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G65/08
Inventor 南军于海滨张景成曲晓龙张玉婷耿姗史玉琳张雪梅王庆波王栋
Owner CHINA NAT OFFSHORE OIL CORP
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