Liquid phase hydrogenation catalytic reaction system

Abstract

The utility model belongs to the technical field of chemical equipment, concretely relates to a liquid phase hydrogenation catalytic reaction system, the liquid phase hydrogenation catalytic reaction system includes: gas phase feed pipe, liquid phase feed pipe, main reactor, gas -liquid separator and liquid phase hydrogenation finishing reactor, gas phase feed pipe and liquid phase hydrogenation finishing reactor's gas phase feed port and main reactor's air inlet intercommunication, liquid phase feed pipe and main reactor's liquid inlet intercommunication, main reactor's discharge port and gas -liquid separator's import intercommunication, gas -liquid separator's liquid outlet and liquid phase hydrogenation finishing reactor's liquid phase feed port intercommunication, gas -liquid separator's gas outlet and main reactor's air inlet intercommunication, liquid phase hydrogenation finishing reactor's gas phase export and main reactor's air inlet intercommunication.

Description

Technical Field

[0001] This application belongs to the field of chemical equipment technology, specifically relating to a liquid-phase hydrogenation catalytic reaction system. Background Technology

[0002] Liquid-phase hydrogenation reactions are typically exothermic and are carried out in fixed-bed reactors. The reactants flow from top to bottom through the catalyst bed and react under its influence.

[0003] Currently, hydrogenation reactors are becoming increasingly larger, which can lead to reduced feed conversion rates during the reaction process due to uneven gas-liquid distribution in the catalyst bed. Excessive unconverted feed content at the reactor outlet can also increase energy consumption in subsequent separation processes and reduce product quality. Utility Model Content

[0004] To address the aforementioned technical problems, this invention provides a liquid-phase hydrogenation catalytic reaction system, aiming to overcome the issue of low feed conversion rates caused by the excessively large size of the liquid-phase hydrogenation reactor in the prior art.

[0005] The technical solution of this utility model is as follows:

[0006] A liquid-phase hydrogenation catalytic reaction system includes: a gas-phase feed pipe, a liquid-phase feed pipe, a main reactor, a gas-liquid separator, and a liquid-phase hydrogenation refining reactor; the gas-phase feed pipe is connected to the gas-phase inlet of the liquid-phase hydrogenation refining reactor and the gas inlet of the main reactor; the liquid-phase feed pipe is connected to the liquid inlet of the main reactor; the outlet of the main reactor is connected to the inlet of the gas-liquid separator, the liquid outlet of the gas-liquid separator is connected to the liquid-phase feed inlet of the liquid-phase hydrogenation refining reactor, the gas outlet of the gas-liquid separator is connected to the gas inlet of the main reactor; and the gas inlet of the main reactor is connected to the gas-phase outlet of the liquid-phase hydrogenation refining reactor.

[0007] In some embodiments, the liquid-phase hydrogenation catalytic reaction system further includes a compressor connected to the inlet of the main reactor, the outlet of the gas-liquid separator, and the gas phase outlet of the liquid-phase hydrogenation refining reactor.

[0008] In some embodiments, the liquid-phase hydrorefining reactor includes: a body having a gas phase inlet, a liquid phase inlet, a gas phase outlet, and a liquid phase outlet, wherein the gas phase inlet, the liquid phase inlet, the gas phase outlet, and the liquid phase outlet are spaced apart from top to bottom along the axial direction of the body, and a gas-liquid phase separation space communicating with the gas phase outlet and the liquid phase outlet is formed within the body; an inlet distribution plate disposed within the body and communicating with the gas phase inlet, the inlet distribution plate being located between the gas phase inlet and the liquid phase inlet; a liquid distributor disposed within the body and communicating with the liquid phase inlet; and at least one catalyst assembly disposed within the body and located between the liquid distributor and the gas-liquid phase separation space; wherein the liquid phase inlet is located between the liquid distributor and the gas phase inlet, and the gas phase outlet is located between the catalyst assembly and the liquid phase outlet.

[0009] In some embodiments, the number of catalyst components is one or more, and when the number of catalyst components is multiple, the multiple catalyst components are arranged side by side at intervals along the axial direction of the body.

[0010] In some embodiments, when there are multiple catalyst components, the liquid-phase hydrorefining reactor further includes a liquid redistributor disposed between two adjacent catalyst components.

[0011] In some embodiments, the catalyst assembly includes: a catalyst bed disposed within the body; and a support member disposed within the body for supporting the catalyst bed.

[0012] In some embodiments, the liquid-phase hydrogenation refining reactor further includes: a plurality of temperature sensing components, which are inserted through the body and disposed within the catalyst bed, and are spaced apart from top to bottom along the axial direction of the body; a thermometer, disposed outside the body and located at the bottom of the catalyst bed; wherein, along the axial direction of the body, the projections of the plurality of temperature sensing components on the body are staggered, and along the radial direction of the body, the projection of the thermometer falls on the catalyst bed.

[0013] In some embodiments, along the axial direction of the body, the projections of multiple temperature sensing components on the body are evenly spaced at equal angles.

[0014] In some implementations, the body has a discharge port that communicates with the body.

[0015] In some embodiments, the liquid-phase hydrogenation refining reactor further includes packing material disposed within the body and located between the liquid distributor and the catalyst assembly.

[0016] The beneficial effects of this utility model include at least the following:

[0017] Hydrogen enters the main reactor through the gas phase feed pipe and the main reactor inlet, while liquid material enters through the liquid phase feed pipe and the main reactor liquid inlet, where the reaction takes place. Unreacted liquid material and excess hydrogen in the main reactor enter the gas-liquid separator through the main reactor outlet and the gas-liquid separator inlet. The gas-liquid separator separates the main reactor outlet into hydrogen and liquid material. Hydrogen enters the main reactor through the gas-liquid separator outlet and the main reactor inlet, allowing for hydrogen recycling. Liquid material enters the main body through the gas-liquid separator outlet and the liquid phase feed inlet, while hydrogen from the gas phase feed pipe enters the main body through the gas phase feed inlet, enabling hydrogen to react with the liquid material. This ensures that the unconverted liquid raw material in the main reactor can fully react, improving the overall raw material conversion rate. The raw material conversion rate at the main body inlet can reach over 98%, reducing subsequent separation energy consumption and improving product quality. Excess hydrogen in the main body can enter the main reactor through the gas phase outlet and the main reactor inlet, thus realizing the recycling of hydrogen. Attached Figure Description

[0018] To more clearly illustrate the technical solutions in the embodiments of this application, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0019] Figure 1 These are schematic diagrams of the liquid-phase hydrogenation catalytic reaction system in some embodiments;

[0020] Figure 2 for Figure 1 A schematic diagram of the liquid-phase hydrogenation refining reactor in a liquid-phase hydrogenation catalytic reaction system;

[0021] Figure 3 for Figure 2 A schematic projection of multiple temperature components in the liquid-phase hydrogenation refining reactor.

[0022] In the attached image:

[0023] Body 10, gas phase inlet 11, liquid phase inlet 12, gas phase outlet 13, liquid phase outlet 14, gas-liquid phase separation space 15, discharge port 16.

[0024] Packing material 20;

[0025] Catalyst assembly 30, support 31, catalyst bed 32;

[0026] Liquid redistributor 40;

[0027] Temperature detection component 50, third support 51, temperature detector 52;

[0028] Thermometer 60;

[0029] Entrance distribution plate 70;

[0030] Liquid distributor 80;

[0031] 90° gas phase feed pipe;

[0032] Liquid feed pipe 100;

[0033] Main reactor 110;

[0034] Gas-liquid separator 120;

[0035] Compressor 130. Detailed Implementation

[0036] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0037] It should be noted that all directional indications in this utility model embodiment are only used to explain the relative positional relationship and movement of each component in a specific posture. If the specific posture changes, the directional indications will also change accordingly.

[0038] In this utility model, unless otherwise explicitly specified and limited, the terms "connection," "fixing," etc., should be interpreted broadly. For example, "fixing" can mean a fixed connection, a detachable connection, or an integral part; it can mean a mechanical connection or an electrical connection; it can mean a direct connection or an indirect connection through an intermediate medium; it can mean the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this utility model according to the specific circumstances.

[0039] Furthermore, in this utility model, descriptions involving "first," "second," etc., are for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined with "first" or "second" may explicitly or implicitly include at least one of that feature. Additionally, the technical solutions of the various embodiments can be combined with each other, but only on the basis of being achievable by those skilled in the art. When the combination of technical solutions is contradictory or impossible to implement, such a combination of technical solutions should be considered non-existent and not within the scope of protection claimed by this utility model.

[0040] This application is described below with reference to the accompanying drawings and specific embodiments:

[0041] The liquid-phase hydrogenation catalytic reaction system provided in this embodiment aims to overcome the problem of low feed conversion rate caused by the excessive size of the liquid-phase hydrogenation reactor in the prior art.

[0042] Figure 1 This is a schematic diagram of the structure of a liquid-phase hydrogenation catalytic reaction system according to some embodiments. (Combined with...) Figure 1 This application provides a liquid-phase hydrogenation catalytic reaction system, including: a gas-phase feed pipe 90, a liquid-phase feed pipe 100, a main reactor 110, a gas-liquid separator 120, and a liquid-phase hydrogenation refining reactor. The gas-phase feed pipe 90 is connected to the gas-phase inlet 11 of the liquid-phase hydrogenation refining reactor and the gas inlet of the main reactor 110. The liquid-phase feed pipe 100 is connected to the liquid inlet of the main reactor 110. The outlet of the main reactor 110 is connected to the inlet of the gas-liquid separator 120, the liquid outlet of the gas-liquid separator 120 is connected to the liquid-phase feed inlet 12 of the liquid-phase hydrogenation refining reactor, and the gas outlet of the gas-liquid separator 120 is connected to the gas inlet of the main reactor 110. The gas-phase outlet 13 of the liquid-phase hydrogenation refining reactor is connected to the gas inlet of the main reactor 110.

[0043] Hydrogen enters the main reactor 110 through the gas phase feed pipe 90 and the gas inlet of the main reactor 110, while liquid materials enter the main reactor 110 through the liquid phase feed pipe 100 and the liquid inlet of the main reactor 110, and the reaction takes place in the main reactor 110. Unreacted liquid material and excess hydrogen in the main reactor 110 enter the gas-liquid separator 120 through the outlet of the main reactor 110 and the inlet of the gas-liquid separator 120. The gas-liquid separator 120 separates the effluent from the main reactor 110 into hydrogen and liquid material. Hydrogen enters the main reactor 110 through the outlet of the gas-liquid separator 120 and the inlet of the main reactor 110, allowing for hydrogen recycling. Liquid material enters the main body 10 through the liquid outlet of the gas-liquid separator 120 and the liquid inlet 12. Hydrogen from the gas inlet pipe 90 enters the main body 10 through the gas inlet 11, allowing hydrogen to react with the liquid material. This ensures that the unconverted liquid raw material in the main reactor 110 can fully react, improving the overall conversion rate of the raw material. The conversion rate of the raw material at the inlet of the main body 10 can reach over 98%, reducing subsequent separation energy consumption and improving product quality. Excess hydrogen in the main body 10 can enter the main reactor 110 through the gas phase outlet 13 and the gas inlet of the main reactor 110, thus realizing the recycling of hydrogen.

[0044] In some embodiments, in order to achieve hydrogen recycling, the liquid-phase hydrogenation catalytic reaction system further includes a compressor 130. The compressor 130 is connected to the inlet of the main reactor 110, the outlet of the gas-liquid separator 120, and the gas phase outlet 13 of the liquid-phase hydrogenation refining reactor.

[0045] Start the compressor 130 so that the hydrogen discharged from the outlet of the gas-liquid separator 120 and the hydrogen discharged from the gas phase outlet 13 enter the main reactor 110 through the compressor 130 and the inlet of the main reactor 110, so that the hydrogen can be recycled and the cost can be reduced.

[0046] In related technologies, an excess of hydrogen is required to ensure the liquid-phase hydrogenation reaction proceeds fully. Due to the excess hydrogen, the reactor output is a two-phase gas-liquid mixture, necessitating gas-liquid separation. To achieve this separation, a gas-liquid separator is installed at the reactor outlet, increasing equipment investment and floor space requirements.

[0047] Figure 2 for Figure 1 A schematic diagram of the liquid-phase hydrogenation refining reactor in a medium-liquid-phase hydrogenation catalytic reaction system. (Combined with...) Figure 2The liquid-phase hydrogenation refining reactor includes a body 10, an inlet distribution plate 70, a liquid distributor 80, and a catalyst assembly 30. The body 10 has a gas inlet 11, a liquid inlet 12, a gas outlet 13, and a liquid outlet 14, which are spaced apart from top to bottom along the axial direction of the body 10. A gas-liquid phase separation space 15 communicating with the gas outlet 13 and the liquid outlet 14 is formed within the body 10. The inlet distribution plate 70 is located within the body 10 and communicates with the gas inlet 11, situated between the gas inlet 11 and the liquid inlet 12. The liquid distributor 80 is located within the body 10 and communicates with the liquid inlet 12. At least one catalyst assembly 30 is located within the body 10 and between the liquid distributor 80 and the gas-liquid phase separation space 15. The liquid phase inlet 12 is located between the liquid distributor 80 and the gas phase inlet 11, and the gas phase outlet 13 is located between the catalyst assembly 30 and the liquid phase outlet 14.

[0048] The liquid distributor 80 can be a tank-type liquid distributor.

[0049] Since the main body 10 has a gas phase inlet 11, a liquid phase inlet 12, a gas phase outlet 13, and a liquid phase outlet 14, arranged at intervals from top to bottom along the axial direction of the main body 10, and a gas-liquid phase separation space 15 communicating with the gas phase outlet 13 and the liquid phase outlet 14 is provided inside the main body 10, the packing 20 is disposed inside the main body 10, and at least one catalyst assembly 30 is disposed inside the main body 10 and located between the packing 20 and the gas-liquid phase separation space 15, the liquid phase inlet 12 is located between the liquid distributor 80 and the gas phase inlet 11, and the gas phase outlet 13 is located between the catalyst assembly 30 and the liquid phase outlet 14, liquid materials can enter the main body 10 through the liquid phase inlet 12, and hydrogen can enter through the gas phase inlet. 11. Liquid material enters the main body 10 through the liquid phase inlet 12 into the liquid distributor 80. Under the action of gravity, the liquid material is evenly distributed on the catalyst assembly 30. Under the action of pressure difference, hydrogen gas reaches the inlet distribution plate 70, so that the hydrogen gas is evenly distributed on the catalyst assembly 30. The liquid material and hydrogen gas react on the catalyst assembly 30, and reactants are produced after the reaction. The reactants and unreacted hydrogen gas enter the gas-liquid separation space 15. Since the density of the reactants is greater than that of hydrogen gas, the reactants will fall to the liquid phase outlet 14 under the action of gravity and be discharged through the liquid phase outlet 14. Hydrogen gas enters the gas phase outlet 13 and is discharged through the gas phase outlet 13, realizing gas-liquid separation. There is no need to set up a gas-liquid separation tank, which reduces equipment investment and land occupation.

[0050] In some embodiments, the number of catalyst components 30 is one or more in order to achieve a sufficient reaction of the liquid material. When there are multiple catalyst components 30, the multiple catalyst components 30 are arranged side by side at intervals along the axial direction of the body 10, and the liquid material and hydrogen can be fully reacted through the multiple catalyst components 30.

[0051] In some embodiments, to ensure uniform distribution of hydrogen and liquid materials reaching the catalyst assembly 30, when there are multiple catalyst assemblies 30, the liquid-phase hydrorefining reactor further includes a liquid redistributor 40. The liquid redistributor 40 is disposed between two adjacent catalyst assemblies 30, and redistributes the hydrogen and liquid materials to ensure uniform distribution of hydrogen and liquid materials on the lower catalyst assembly 30. The liquid redistributor 40 can be a disc distributor.

[0052] Combination Figure 2 In some embodiments, to enable the reaction between hydrogen and liquid materials, the catalyst assembly 30 includes a support 31 and a catalyst bed 32. The catalyst bed 32 is disposed within the body 10, and the hydrogen and liquid materials can react on the catalyst bed 32 upon arrival. The support 31, disposed within the body 10, supports the catalyst bed 32 to ensure the stability of its installation. Ceramic balls are provided at both the top and bottom of the catalyst bed 32.

[0053] Liquid material enters the liquid distributor 80 through the liquid inlet 12. Under the action of gravity, the liquid material is evenly distributed on the catalyst bed 32. Under the action of pressure difference, hydrogen gas reaches the inlet distribution plate 70, so that the hydrogen gas is evenly distributed on the catalyst bed 32. The liquid material and hydrogen gas react on the catalyst bed 32, and reactants are produced after the reaction.

[0054] In some embodiments, when the liquid material entering the body 10 through the liquid inlet 12 is acetone, the catalyst bed 32 can be an acetone hydrogenation catalyst bed. When the liquid material entering the body 10 through the liquid inlet 12 is Fischer-Tropsch oil, the catalyst bed 32 can be a Fischer-Tropsch oil hydrogenation catalyst bed.

[0055] Figure 3 for Figure 2 A schematic projection of multiple temperature components of the medium-liquid phase hydrorefining reactor onto the main body 10. (Combined with...) Figure 3To detect the temperature of the catalyst bed 32 within the main body 10, the liquid-phase hydrogenation refining reactor further includes a temperature detection assembly 50 and a thermometer 60. Multiple temperature detection assemblies 50 are inserted through the main body 10 and disposed within the catalyst bed 32, spaced apart from top to bottom along the axial direction of the main body 10. The thermometer 60 is located outside the main body 10 and at the bottom of the catalyst bed 32. Along the axial direction of the main body 10, the projections of the multiple temperature detection assemblies 50 on the main body 10 are staggered, and along the radial direction of the main body 10, the projection of the thermometer 60 falls on the catalyst bed 32.

[0056] Along the axial direction of the body 10, multiple temperature detection components 50 can detect the temperature of multiple cross sections of the catalyst bed 32 along the radial direction of the body. By comparing the temperatures detected by the multiple temperature detection components 50, the temperature of multiple cross sections can be obtained. In other words, the axial temperature change of the catalyst bed 32 can be obtained. If the highest temperature of the catalyst bed 32 moves to the bottom of the catalyst bed 32, the catalyst temperature is increased or the catalyst is replaced.

[0057] The thermometer 60 can detect the temperature of the outer wall of the reactor body 10 and compare it with the temperature obtained by the catalyst bed bottom temperature detection component 50, thereby monitoring the difference between the reactor outer wall temperature and the bed temperature. The thermometer 60 can be a patch thermometer.

[0058] In some embodiments, in order to detect the temperature at different locations of a cross section along the radial direction of the catalyst bed 32, the temperature detection assembly 50 includes a third support 51 and a plurality of temperature detectors 52, which are arranged side-by-side at intervals along the radial direction of the body 10 on the third support 51.

[0059] Multiple temperature detectors 52 can detect the temperature at different positions along a cross section of the catalyst bed 32 in the radial direction of the body. By comparing the temperatures detected by multiple temperature detectors 52, the temperature at different positions in a cross section can be obtained. In other words, the radial temperature difference of the catalyst bed 32 in that cross section can be obtained. If the temperature difference is greater than a first set threshold, it indicates that the catalyst bed 32 may have abnormal conditions such as uneven gas-liquid distribution or flow deviation. The reaction can be improved by increasing the reaction temperature. If the reaction continues to deteriorate, the catalyst needs to be replaced.

[0060] In some embodiments, to improve detection accuracy, multiple temperature detection components 50 are evenly spaced at equal angles along the axial direction of the body 10, allowing the temperature at different locations on each cross-section of the catalyst bed 32 along the radial direction of the body to be obtained, thus ensuring accurate cross-sectional temperature differences of the catalyst bed 32. The angle between the projections of two adjacent temperature detection components 50 onto the body 10 can be between 60° and 120°.

[0061] Combination Figure 2 In some embodiments, in order to replace the catalyst bed 32, the body 10 has a discharge port 16 communicating with the body 10. When the catalyst bed 32 needs to be replaced, the discharge port 16 is opened to discharge the catalyst bed 32.

[0062] In some embodiments, a thermometer 60 is installed at the bottom of the catalyst bed 32. When the catalyst bed 32 needs to be replaced, the temperature detected by the thermometer 60 is obtained. If the temperature detected by the thermometer 60 is less than a second set threshold, it indicates that the temperature of the catalyst bed 32 will not burn the staff. Then the discharge port 16 is opened for unloading, ensuring safety.

[0063] In some embodiments, to ensure uniform distribution of hydrogen and liquid materials, the liquid-phase hydrogenation refining reactor further includes a packing 20. The packing 20 is disposed within the body 10 and located between the liquid distributor 80 and the catalyst assembly 30. Hydrogen and liquid materials flow to the packing 20, thereby ensuring uniform mixing of hydrogen and liquid materials.

[0064] In some embodiments, the filler 20 may be made of 304 stainless steel or 316L stainless steel.

[0065] Example 1:

[0066] The inner diameter of the main reactor 110 is 2.6m. The raw material conversion is incomplete, and the raw material content at the outlet of the main reactor 110 is too high, generally around ~6wt%, which causes raw material loss and unqualified product indicators, and also leads to high separation energy consumption.

[0067] By adding a liquid-phase hydrogenation refining reactor after the main reactor 110, the unreacted liquid material and excess hydrogen in the main reactor 110 are introduced into the gas-liquid separator 120 through the outlet of the main reactor 110 and the inlet of the gas-liquid separator 120. The gas-liquid separator 120 separates the gas and liquid components of the main reactor 110, obtaining hydrogen and liquid material. The hydrogen enters the main reactor 110 through the outlet of the gas-liquid separator 120 and the inlet of the main reactor 110, allowing for hydrogen recycling. The liquid material enters the main body 10 through the liquid outlet of the gas-liquid separator 120 and the liquid phase inlet 12. Hydrogen from the gas phase feed pipe 90 enters the main body 10 through the gas phase inlet 11, allowing the hydrogen to react with the liquid material. This ensures that the unconverted liquid raw material in the main reactor 110 can fully react, improving the overall conversion rate of the raw material. The content of the raw material at the liquid outlet 14 of the body 10 is reduced to 95 ppm (wt), and the conversion rate of the raw material at the inlet of the body 10 is 99.84 wt%.

[0068] The liquid-phase hydrogenation refining reactor is a fixed-bed reactor with an inner diameter of 1.1 m for the main body 10, a reaction temperature of 100–130 °C, and a reaction pressure of 3 MPaG. There are two catalyst modules 30, meaning there are two catalyst beds 32, with each catalyst module 30 having a catalyst bed 32 height of 2.5 m.

[0069] Liquid material enters the main body 10 through the outlet of the gas-liquid separator 120 and the liquid inlet 12. A liquid distributor 80 distributes the liquid material evenly across the catalyst bed 32. The liquid distributor 80 is a trough-type liquid distributor. Hydrogen gas from the gas inlet pipe 90 enters the main body 10 through the gas inlet 11. An inlet distribution plate 70 distributes the hydrogen evenly across the catalyst bed 32, allowing the hydrogen and liquid material to react on the first catalyst bed 32. The reactants flowing out of the first catalyst bed 32 enter the liquid redistributor 40, which distributes them evenly onto the second catalyst bed 32, allowing the hydrogen and liquid material to react on the second catalyst bed 32. The liquid redistributor 40 is a disc-type distributor. The product leaving the second catalyst bed 32 enters the gas-liquid separation space 15 at the bottom of the liquid-phase hydrorefining reactor for gas-liquid separation. The separated hydrogen is recycled to the inlet of the main reactor 110, and the separated liquid phase enters the subsequent separation and purification unit.

[0070] There are two catalyst components 30, each containing four temperature detection components 50, and each temperature detection component 50 has three temperature detectors 52. The angle between the projections of two adjacent temperature detection components 50 onto the body 10 is 60°. There are two thermometers 60, both located outside the body 10 and at the bottom of the two catalyst components 30, respectively, to detect the temperature of the outer wall surface of the body 10. The thermometers 60 are patch thermometers.

[0071] Example 2:

[0072] The main reactor 110 has an inner diameter of 2m. The raw material conversion is incomplete, and the raw material content at the reactor outlet is too high, generally around 5wt%, which causes raw material loss and product indicators to be unqualified, while also resulting in high separation energy consumption.

[0073] By adding a refining reactor after the main reactor 110, the unreacted liquid material and excess hydrogen in the main reactor 110 are introduced into the gas-liquid separator 120 through the outlet of the main reactor 110 and the inlet of the gas-liquid separator 120. The gas-liquid separator 120 separates the gas and liquid components of the main reactor 110, obtaining hydrogen and liquid material. The hydrogen enters the main reactor 110 through the outlet of the gas-liquid separator 120 and the inlet of the main reactor 110, allowing for hydrogen recycling. The liquid material enters the main body 10 through the liquid outlet of the gas-liquid separator 120 and the liquid phase inlet 12. Hydrogen from the gas phase feed pipe 90 enters the main body 10 through the gas phase inlet 11, allowing the hydrogen to react with the liquid material. This ensures that the unconverted liquid raw material in the main reactor 110 can fully react, improving the overall conversion rate of the raw material. The feed content at the liquid outlet 14 of the bulk 10 decreased to 67 ppm (wt), and the feed conversion rate at the inlet of the bulk 10 was 99.87 wt%.

[0074] The liquid-phase hydrogenation refining reactor is a fixed-bed reactor with an inner diameter of 1.0 m, a reaction temperature of 280–320 °C, and a reaction pressure of 8 MPaG. There are two catalyst modules 30, meaning there are two catalyst beds 32, with each catalyst module 30 having a catalyst bed 32 height of 2 m.

[0075] Liquid material enters the main body 10 through the outlet of the gas-liquid separator 120 and the liquid inlet 12. A liquid distributor 80 distributes the liquid material evenly across the catalyst bed 32. The liquid distributor 80 is a trough-type liquid distributor. Hydrogen gas from the gas feed pipe 90 enters the main body 10 through the gas inlet 11. An inlet distribution plate 70 distributes the hydrogen evenly across the catalyst bed 32, allowing the hydrogen and liquid material to react on the first catalyst bed 32. The reactants flowing out of the first catalyst bed 32 enter the liquid redistributor 40, which distributes them evenly onto the second catalyst bed 32, allowing the hydrogen and liquid material to react on the second catalyst bed 32. The liquid redistributor 40 is a disc-type liquid distributor. The product leaving the second catalyst bed 32 enters the gas-liquid separation space 15 at the bottom of the liquid-phase hydrorefining reactor for gas-liquid separation. The separated hydrogen is recycled to the inlet of the main reactor 110, and the separated liquid phase enters the subsequent separation and purification unit.

[0076] There are two catalyst components 30, each containing three temperature detection components 50, and each temperature detection component 50 has three temperature detectors 52. The angle between the projections of two adjacent temperature detection components 50 onto the body 10 is 90°. There are two thermometers 60, both located outside the body 10 and at the bottom of the two catalyst components 30 respectively, to detect the temperature of the outer wall surface of the body 10. The thermometers 60 are patch thermometers.

[0077] In the description of this application, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this application.

[0078] In the description of this utility model, unless otherwise expressly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0079] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of this application. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. In addition, those skilled in the art can combine and integrate the different embodiments or examples described in this specification.

[0080] Although preferred embodiments of this application have been described, those skilled in the art, upon learning the basic inventive concept, can make other changes and modifications to these embodiments. Therefore, the appended claims are intended to be interpreted as including the preferred embodiments as well as all changes and modifications falling within the scope of this application.

[0081] Obviously, those skilled in the art can make various modifications and variations to this application without departing from the spirit and scope of this application. Therefore, if such modifications and variations fall within the scope of the claims of this application and their equivalents, this application also intends to include such modifications and variations.

Claims

1. A liquid-phase hydrogenation catalytic reaction system, characterized in that, include: Gas-phase feed pipe, liquid-phase feed pipe, main reactor, gas-liquid separator, and liquid-phase hydrogenation refining reactor; The gas phase feed pipe is connected to the gas phase feed inlet of the liquid phase hydrogenation refining reactor and the gas inlet of the main reactor. The liquid feed pipe is connected to the liquid inlet of the main reactor; The discharge port of the main reactor is connected to the inlet of the gas-liquid separator, the liquid outlet of the gas-liquid separator is connected to the liquid inlet of the liquid phase hydrogenation refining reactor, and the gas outlet of the gas-liquid separator is connected to the gas inlet of the main reactor. The gas phase outlet of the liquid phase hydrogenation refining reactor is connected to the gas inlet of the main reactor.

2. The liquid-phase hydrogenation catalytic reaction system according to claim 1, characterized in that, The liquid-phase hydrogenation catalytic reaction system also includes: The compressor is connected to the air inlet of the main reactor, the air outlet of the gas-liquid separator, and the gas phase outlet of the liquid phase hydrogenation refining reactor.

3. The liquid-phase hydrogenation catalytic reaction system according to claim 1, characterized in that, The liquid-phase hydrogenation refining reactor comprises: The main body has a gas phase inlet, a liquid phase inlet, a gas phase outlet and a liquid phase outlet. Along the axial direction of the main body, the gas phase inlet, liquid phase inlet, gas phase outlet and liquid phase outlet are spaced apart from top to bottom. A gas-liquid phase separation space communicating with the gas phase outlet and liquid phase outlet is opened in the main body. An inlet distribution plate is disposed within the main body and communicates with the gas phase feed inlet. The inlet distribution plate is located between the gas phase feed inlet and the liquid phase feed inlet. A liquid distributor is located inside the main body and is connected to the liquid phase inlet; At least one catalyst assembly is disposed within the body and located between the liquid distributor and the gas-liquid phase separation space; The liquid phase inlet is located between the liquid distributor and the gas phase inlet, and the gas phase outlet is located between the catalyst assembly and the liquid phase outlet.

4. The liquid-phase hydrogenation catalytic reaction system according to claim 3, characterized in that, The number of catalyst components is one or more. When the number of catalyst components is multiple, the multiple catalyst components are arranged side by side at intervals along the axial direction of the body.

5. The liquid-phase hydrogenation catalytic reaction system according to claim 4, characterized in that, When the number of catalyst components is multiple, the liquid-phase hydrorefining reactor further includes: A liquid redistributor is located between two adjacent catalyst assemblies.

6. The liquid-phase hydrogenation catalytic reaction system according to any one of claims 3-5, characterized in that, The catalyst assembly includes: The catalyst bed is disposed within the main body; A support member, disposed within the body, is used to support the catalyst bed.

7. The liquid-phase hydrogenation catalytic reaction system according to claim 6, characterized in that, The liquid-phase hydrogenation refining reactor also includes: Multiple temperature detection components are inserted through the body and disposed within the catalyst bed. Along the axial direction of the body, the multiple temperature detection components are spaced apart from top to bottom. A thermometer is located outside the main body and at the bottom of the catalyst bed; Along the axial direction of the body, the projections of multiple temperature sensing components on the body are staggered, and along the radial direction of the body, the projection of the thermometer falls on the catalyst bed.

8. The liquid-phase hydrogenation catalytic reaction system according to claim 7, characterized in that, Along the axial direction of the body, the projections of multiple temperature detection components on the body are evenly spaced at equal angles.

9. The liquid-phase hydrogenation catalytic reaction system according to claim 6, characterized in that, The main body has a discharge port that communicates with the main body.

10. The liquid-phase hydrogenation catalytic reaction system according to any one of claims 3-5, characterized in that, The liquid-phase hydrogenation refining reactor also includes: The packing material is disposed within the body and located between the liquid distributor and the catalyst assembly.

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