Intelligent control strengthening system and process for direct coal liquefaction

Abstract

The invention discloses an intelligent control strengthening system and process for direct coal liquefaction, and belongs to the technical field of chemical engineering. According to the invention, the interphase area of hydrogen and coal-oil slurry is increased by arranging a micro-interface generator in a reactor to smash the hydrogen so as to improve the reaction efficiency of the hydrogen; a sensor and a controller are additionally arranged, so that the temperature and the pressure intensity in the reactor are accurately controlled, and important significance is achieved in reducing the material loss of the device and improving the safety; and a circulating unit is additionally arranged behind the reactor, so that the catalyst is recycled and reused, and the loss of materials is further reduced. Compared with the traditional direct coal liquefaction reaction, the micro-interface generator is additionally arranged in the reactor, and the intelligent controller is additionally arranged, so that the product yield is greatly improved.

Description

technical field

[0001] The invention relates to the technical field of coal-to-liquids, in particular to an intelligent control and strengthening system and process for direct coal liquefaction. Background technique

[0002] The process usually used for catalytic hydrogenation of coal liquefied oil is mainly fixed bed hydrogenation process. Fixed bed reactors are especially suitable for handling lighter and cleaner materials, such as naphtha, middle distillates, etc. The fixed bed reactor is characterized by relatively stable operation and easy control. Because coal liquefied oil is heavy and contains many mechanical impurities, the catalytic reaction conditions will be relatively harsh. At the same time, high-nitrogen raw materials will accelerate the deactivation of the catalyst, shorten the service life of the catalyst, make the product properties unstable, and the pressure drop of the catalyst bed is relatively low. high. In order to make the product meet the standard...

Examples

Embodiment 1

[0076] The reaction temperature during the hydrogenation liquefaction treatment of the reactor is 400°C, the pressure is 2-14MPa, preferably 3-8MPa, and the liquid hourly space velocity is 0.7-1.2h -1， The volume ratio of hydrogen to oil is 100-700; the material flow rate returned by the circulation unit to the reactor shell is 2-5 times that of the direct coal liquefied oil feed flow rate, and the filling volume of the catalyst is 30% of the effective volume of the ebullated bed reactor 25-65%. In addition, the range of preset operating conditions can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, which further ensures that the reaction is fully and effectively carried out, thereby ensuring the reaction rate and achieving the purpose of strengthening the reaction .

[0077] The reaction effect is shown in Table 1:

[0078] Table 1

[0079]

Embodiment 2

[0081] The reaction temperature during the hydrogenation liquefaction treatment of the reactor is 420°C, the pressure is 2-14MPa, preferably 2-6MPa, and the liquid hourly space velocity is 0.7-1.2h -1， The volume ratio of hydrogen to oil is 100-700; the material flow rate returned by the circulation unit to the reactor shell is 2-5 times that of the direct coal liquefied oil feed flow rate, and the filling volume of the catalyst is 30% of the effective volume of the ebullated bed reactor 25-65%. In addition, the range of preset operating conditions can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, which further ensures that the reaction is fully and effectively carried out, thereby ensuring the reaction rate and achieving the purpose of strengthening the reaction .

[0082] The reaction effect is shown in Table 2:

[0083]Table 2

[0084]

Embodiment 3

[0086] The reaction temperature during the hydrogenation liquefaction treatment of the reactor is 450°C, the pressure is 2-14MPa, preferably 2-8MPa, and the liquid hourly space velocity is 0.7-1.2h -1， The volume ratio of hydrogen to oil is 100-700; the material flow rate returned by the circulation unit to the reactor shell is 2-5 times that of the direct coal liquefied oil feed flow rate, and the filling volume of the catalyst is 100% of the effective volume of the ebullated bed reactor 25-65%. In addition, the range of preset operating conditions can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, which further ensures that the reaction is fully and effectively carried out, thereby ensuring the reaction rate and achieving the purpose of strengthening the reaction .

[0087] The reaction effect is shown in Table 3:

[0088] table 3

[0089]

[0090]

technical field

[0001] The invention relates to the technical field of coal-to-liquids, in particular to an intelligent control and strengthening system and process for direct coal liquefaction. Background technique

[0002] The process usually used for catalytic hydrogenation of coal liquefied oil is mainly fixed bed hydrogenation process. Fixed bed reactors are especially suitable for handling lighter and cleaner materials, such as naphtha, middle distillates, etc. The fixed bed reactor is characterized by relatively stable operation and easy control. Because coal liquefied oil is heavy and contains many mechanical impurities, the catalytic reaction conditions will be relatively harsh. At the same time, high-nitrogen raw materials will accelerate the deactivation of the catalyst, shorten the service life of the catalyst, make the product properties unstable, and the pressure drop of the catalyst bed is relatively low. high. In order to make the product meet the standard...

Examples

Embodiment 1

[0076] The reaction temperature during the hydrogenation liquefaction treatment of the reactor is 400°C, the pressure is 2-14MPa, preferably 3-8MPa, and the liquid hourly space velocity is 0.7-1.2h -1， The volume ratio of hydrogen to oil is 100-700; the material flow rate returned by the circulation unit to the reactor shell is 2-5 times that of the direct coal liquefied oil feed flow rate, and the filling volume of the catalyst is 30% of the effective volume of the ebullated bed reactor 25-65%. In addition, the range of preset operating conditions can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, which further ensures that the reaction is fully and effectively carried out, thereby ensuring the reaction rate and achieving the purpose of strengthening the reaction .

[0077] The reaction effect is shown in Table 1:

[0078] Table 1

[0079]

Embodiment 2

[0081] The reaction temperature during the hydrogenation liquefaction treatment of the reactor is 420°C, the pressure is 2-14MPa, preferably 2-6MPa, and the liquid hourly space velocity is 0.7-1.2h -1， The volume ratio of hydrogen to oil is 100-700; the material flow rate returned by the circulation unit to the reactor shell is 2-5 times that of the direct coal liquefied oil feed flow rate, and the filling volume of the catalyst is 30% of the effective volume of the ebullated bed reactor 25-65%. In addition, the range of preset operating conditions can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, which further ensures that the reaction is fully and effectively carried out, thereby ensuring the reaction rate and achieving the purpose of strengthening the reaction .

[0082] The reaction effect is shown in Table 2:

[0083]Table 2

[0084]

Embodiment 3

[0086] The reaction temperature during the hydrogenation liquefaction treatment of the reactor is 450°C, the pressure is 2-14MPa, preferably 2-8MPa, and the liquid hourly space velocity is 0.7-1.2h -1， The volume ratio of hydrogen to oil is 100-700; the material flow rate returned by the circulation unit to the reactor shell is 2-5 times that of the direct coal liquefied oil feed flow rate, and the filling volume of the catalyst is 100% of the effective volume of the ebullated bed reactor 25-65%. In addition, the range of preset operating conditions can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, which further ensures that the reaction is fully and effectively carried out, thereby ensuring the reaction rate and achieving the purpose of strengthening the reaction .

[0087] The reaction effect is shown in Table 3:

[0088] table 3

[0089]

[0090]

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