A liquid phase hydrogenation reactor for chemical production

Abstract

The present invention belongs to the technical field of hydrogenation reactors, and specifically relates to a liquid-phase hydrogenation reactor for chemical production, comprising a shell, an upper head, a top diffuser and a distribution plate, wherein the upper head is located at the top of the shell, a feed port is provided on the upper head, the top diffuser is installed inside the upper head, and the distribution plate is located below the top diffuser. The present invention also comprises: a reaction bed, wherein the reaction bed has several layers, which are evenly arranged at equal intervals from top to bottom; a central axis, which is driven by a motor located at the top of the upper head; the reaction bed comprises, from top to bottom, an upper partition, a stirring device and a catalyst support plate, wherein the stirring device is located between the upper partition and the catalyst support plate. By changing the reaction bed structure of the existing hydrogenation reactor, adding a stirring mechanism, and driving the mixture and the catalyst in the reaction bed to rotate by the motor, the reactants are fully mixed and the reaction degree is improved.

Description

Technical Field

[0001] The invention belongs to the technical field of hydrogenation reactors, and in particular relates to a liquid phase hydrogenation reactor for chemical production. Background Art

[0002] Hydrogenation reactors have a wide range of applications in the pharmaceutical industry. They serve as fundamental equipment for product development, organic chemical and pharmaceutical research, and can also be used to quantitatively analyze catalyst activity in industrial processes. Commonly used hydrogenation reactors can be broadly divided into two categories: one is used for liquid-phase hydrogenation of high-boiling-point liquid or solid (solids must first be dissolved in a solvent or heated to melt) feedstocks, such as oil hydrogenation and heavy oil hydrocracking. Liquid-phase hydrogenation is often performed under pressure and can be either batch or continuous. Batch liquid-phase hydrogenation often utilizes autoclaves or bubble reactors equipped with stirring mechanisms. Continuous liquid-phase hydrogenation can utilize trickle-bed reactors or tubular reactors with continuous co-current flow of gas, liquid, and solid phases. The other type of reactor is used for continuous gas-phase hydrogenation processes, such as the atmospheric-pressure gas-phase hydrogenation of benzene to cyclohexane and the high-pressure gas-phase hydrogenation of carbon monoxide to methanol. These reactors can be either shell-and-tube or tower-type.

[0003] Hydrogenation reactors operate under high temperature and high pressure in the presence of hydrogen. The materials entering the reactor often contain impurities such as sulfur and nitrogen, which react with hydrogen to produce corrosive hydrogen sulfide and ammonia. Furthermore, hydrogenation is exothermic, raising the bed temperature, yet localized overheating is essential. Hydrocarbon hydrogenation is exothermic. In multi-bed hydrogenation reactors, the temperature of the oil, gas, and hydrogen rises after reacting in the upper bed. To ensure efficient reaction in the lower bed, cold hydrogen must be introduced between the two beds to control the temperature. The pipes that introduce and distribute the cold hydrogen into the reactor are called cold hydrogen pipes. Cold hydrogen pipes are categorized by their design: inline, dendritic, or ring-shaped. For smaller diameter reactors, the simple, easy-to-install inline design is suitable. For larger diameter reactors, the cold hydrogen injected by inline cold hydrogen pipes mixes poorly with the oil and gas reacting in the upper layer, directly impacting the remixing efficiency of the cold hydrogen tank. In these cases, dendritic or ring-shaped structures are preferred. The cold purge pipe is typically located within a cold hydrogen tank. The first layer of the tank consists of baffle plates with orifices. Cold hydrogen exiting the cold hydrogen pipe is premixed with the reacted oil and gas from the upper bed on the baffle plates before entering the cold hydrogen tank through the orifices. The cold hydrogen entering the cold hydrogen tank and the hot oil and gas from the upper layer undergo repeated deflections and mixing before flowing to the second layer of the cold hydrogen tank—the sieve plates. There, the flow is further deflected to enhance mixing before distribution. Below the sieve plates, a bubble cap distribution plate is sometimes added for final distribution of the pre-distributed oil and gas.

[0004] However, existing hydrogenation reactors typically use multi-stage reaction beds to provide multi-stage distribution plates, which further mix the mixture by continuously disrupting the flow of the mixed reactants. Compared with stirring, this method can only ensure uniform dispersion of the reactants but cannot ensure uniform mixing, resulting in incomplete and incomplete reaction of the reactants.

[0005] In view of this, the present invention is proposed to solve the above problems. Summary of the Invention

[0006] The object of the present invention is to provide a liquid-phase hydrogenation reactor for chemical production. The specific problem to be solved by the present invention is that existing hydrogenation reactors generally use multi-stage reaction beds to provide multi-stage distribution plates, which can only ensure uniform dispersion of reactants but not uniform mixing, resulting in insufficient and incomplete reaction of the reactants.

[0007] To achieve the above object, the present invention provides the following technical solutions:

[0008] A liquid-phase hydrogenation reactor for chemical production, comprising a shell, an upper head, a top diffuser, and a distribution plate, wherein the upper head is located at the top of the shell, a feed port is provided on the upper head, the top diffuser is installed inside the upper head, and the distribution plate is located below the top diffuser, and further comprising:

[0009] A reaction bed, wherein the reaction bed has several layers, which are evenly arranged with equal spacing from top to bottom;

[0010] The central shaft is driven by a motor located on top of the upper head;

[0011] The reaction bed comprises an upper partition, a stirring device and a catalyst support plate from top to bottom, and the stirring device is located between the upper partition and the catalyst support plate.

[0012] Preferably, the central shaft is a multi-stage structure, and the relative cross-sectional position between two adjacent stages is a bevel gear structure;

[0013] The stirring device comprises:

[0014] A protective cover, the protective cover being a conical structure with upper and lower surfaces protruding outwards;

[0015] There are two stirring shafts in the same reaction bed, and they are installed horizontally;

[0016] The stirring shaft is fixedly connected to stirring rods, the number of the stirring rods is greater than one and the stirring rods are linearly arranged on both sides of the stirring shaft;

[0017] One end of the stirring shaft is a bevel gear structure. The two stirring shafts in the same reaction bed layer are cross-engaged with the upper and lower center shafts through the bevel gear and bevel gear structure in the same vertical plane, and the engagement position is located inside the protective cover.

[0018] Preferably, the central shaft is a hollow tubular structure, and the central shaft is fixedly connected to the top motor via a rotary joint;

[0019] The stirring shaft is a hollow structure and a vertical through hole is opened on the side wall.

[0020] Preferably, the central shaft, the stirring shaft and the protective cover in each section are connected through a bearing sliding seal.

[0021] Preferably, the catalyst support plate is provided with a number of through holes greater than one, the upper diameter of the through hole is smaller than the lower diameter, the top of the through hole is a pedestal structure, an L-shaped joint is fixed to the pedestal structure, a pipe is provided in the L-shaped joint, the bottom of the pipe is connected to the through hole, and the inlet is arranged horizontally.

[0022] Preferably, the spacing between the stirring rods on the stirring shaft is greater than the diameter of the porcelain balls used in the reactor, and the inlet diameter of the L-shaped joint is less than one-third of the diameter of the porcelain balls.

[0023] Preferably, a scraper is fixedly connected to the end of the stirring shaft, the scraper is in contact with the inner wall of the shell, and the scraper is made of rubber material.

[0024] Preferably, the central axis and each layer are connected by sliding sealing.

[0025] Preferably, the shell is provided with a pair of catalyst discharge pipes at the bottom of each layer of reaction bed, and the shell is provided with a catalyst addition port at the middle of each layer of reaction bed, and the catalyst addition port is provided with a sealing cover connected with a flange.

[0026] Preferably, a discharge port is provided at the bottom of the shell, and a collector is installed above the discharge port at the bottom inside the shell. The collector is a cap-shaped component with a round hole on the top and a long hole on the side wall. The top of the collector is slidably connected to the central axis through a bearing.

[0027] Compared with the prior art, the present invention has the following beneficial effects:

[0028] 1. By modifying the existing hydrogenation reactor bed structure, adding a stirring mechanism, and rotating it with a motor, the mixture and catalyst in the reactor bed are stirred to fully mix the reactants and enhance the reaction rate. Compared with reactors without a stirring mechanism, this can further enhance the mixing level and make the reaction more thorough. In addition, stirring also reduces the reaction time and improves efficiency. During the rotation of the stirring shaft, in addition to stirring the reactants and catalyst, the scraper at the end of the stirring shaft can also clean the inner wall of the reactor bed shell, reducing attachment waste and reducing the cost and time of subsequent cleaning.

[0029] 2. The gear shape design of the shaft ends of the central shaft and the stirring shaft makes the rotation directions of the two adjacent central shafts opposite. In addition to stirring the reactants and catalysts, the stirring shaft also plays a transmission role. The stirring shafts of the two adjacent layers of reaction beds are reversed in the horizontal direction, which enhances the stirring effect. In addition to rotating around its own axis, the stirring shaft also rotates around the axis of the central shaft, further improving the stirring effect. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 It is a visual diagram of the present invention;

[0031] Figure 2 A top view of the present invention;

[0032] Figure 3 For the present invention Figure 2 AA cross-section of

[0033] Figure 4 A visual diagram of the top diffuser of the present invention;

[0034] Figure 5 A diagram showing the distribution tray of the present invention;

[0035] Figure 6 A bottom view of the distribution tray of the present invention;

[0036] Figure 7 A direct view of the catalyst support plate of the present invention;

[0037] Figure 8 It is an intuitive diagram of the collector of the present invention.

[0038] In the figure: shell 1, catalyst unloading pipe 11, catalyst addition port 12, sealing cover 13, discharge port 14, upper head 2, feed port 21, top diffuser 3, distribution plate 4, reaction bed 5, upper partition 51, stirring device 52, protective cover 521, stirring shaft 522, stirring rod 523, scraper 524, catalyst support plate 53, L-shaped joint 531, central shaft 6, rotary joint 7, collector 8. DETAILED DESCRIPTION

[0039] The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, rather than all the embodiments; based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present invention.

[0040] The embodiments of the present invention provide a liquid-phase hydrogenation reactor for chemical production, which solves the technical problem that existing hydrogenation reactors generally use multi-stage reaction beds to provide multi-stage distribution plates, which can only ensure uniform dispersion of reactants but cannot ensure uniform mixing, resulting in insufficient and incomplete reaction of the reactants.

[0041] The technical solution in the embodiments of the present invention is to solve the above technical problems. The overall idea is as follows: by changing the reaction bed structure of the existing hydrogenation reactor, adding a stirring mechanism, and driving the rotation by a motor, the mixture and catalyst in the reaction bed are stirred to ensure that the reactants are fully mixed and the reaction degree is improved.

[0042] To better understand the technical solution of the present invention, please refer to Figures 1 to 8 In an embodiment of the present invention, a liquid-phase hydrogenation reactor for chemical production includes a shell 1, an upper head 2, a top diffuser 3, and a distribution plate 4. The upper head 2 is located at the top of the shell 1 and is provided with a feed inlet 21. The top diffuser 3 is installed inside the upper head 2. The distribution plate 4 is located below the top diffuser 3. The reactor further includes:

[0043] The reaction bed 5 has several layers, which are evenly arranged with equal spacing from top to bottom;

[0044] The central shaft 6 is driven by a motor located on the top of the upper head 2;

[0045] The reaction bed 5 comprises an upper baffle 51, a stirring device 52 and a catalyst support plate 53 from top to bottom. The stirring device 52 is located between the upper baffle 51 and the catalyst support plate 53.

[0046] The number of reaction beds 5 can be appropriately adjusted according to the processing raw materials during manufacturing. For different reactants, increasing the number of reaction beds 5 can increase the number of reactions and further improve the degree of reaction. The mixture of raw materials and hydrogen enters the reactor through the feed port 21 of the upper head 2, and is diffused to the entire cross-section of the reactor after rectification, throttling and collision by the diffuser. Then, it is further collided and broken up by the distribution plate 4 and the upper partition 51 to achieve the effect of improving the flow condition, and then enters the reaction bed 5. Ceramic balls and catalysts are added between the catalyst support plate 53 and the upper partition 51. It is stirred by the stirring device 52. Compared with the reactor without stirring function, it can further improve the degree of mixing and make the reaction more thorough. In addition, stirring also reduces the time required for the hydrogenation reaction and improves the reaction efficiency.

[0047] As an embodiment of the present invention, the central shaft 6 is a multi-stage structure, and the relative cross-sectional position between two adjacent stages is a bevel gear structure;

[0048] The stirring device 52 comprises:

[0049] The protective cover 521 is a conical structure with upper and lower surfaces protruding outwards;

[0050] Stirring shaft 522, there are two stirring shafts in the same reaction bed 5 layer, and they are installed horizontally;

[0051] The stirring shaft 522 is fixedly connected to stirring rods 523 . The number of stirring rods 523 is greater than one and they are linearly arranged on both sides of the stirring shaft 522 .

[0052] One end of the stirring shaft 522 is a bevel gear structure. The two stirring shafts 522 in the same reactor bed 5 layer are cross-engaged with the upper and lower central shafts 6 through the bevel gear and bevel gear structure in the same vertical plane, and the meshing position is located inside the protective cover 521.

[0053] The gear shape design of the shaft ends of the central shaft 6 and the stirring shaft 522 makes the directions of the two adjacent sections of the central shaft 6 opposite. In addition to stirring the reactants and catalyst, the stirring shaft 522 also plays a transmission role; the stirring shafts 522 of the two adjacent layers of reaction beds 5 are reversed in the horizontal direction, thereby enhancing the stirring effect; in addition to rotating around its own axis, the stirring shaft 522 also rotates around the axis of the central shaft 6, further enhancing the stirring effect; the protective cover is used to seal and protect the gear set from the influence of external reactants, and lubricating oil is added to the protective cover to achieve the effect of heat dissipation and lubrication. The top of the protective cover is set to a conical structure to facilitate the normal falling flow of reactants, while further reducing the space occupied by the protective cover to increase the capacity of the reaction bed.

[0054] As an embodiment of the present invention, the central shaft 6 is a hollow tubular structure, and the central shaft 6 is fixedly connected to the top motor via a rotary joint 7;

[0055] The stirring shaft 522 is a hollow structure and has vertically penetrating air holes on its side wall.

[0056] As an embodiment of the present invention, each section of the central shaft 6 is connected to the stirring shaft 522 and the protective cover 521 through a bearing sliding seal.

[0057] In addition to its transmission function, the central shaft 6 also serves as a cold hydrogen pipe. Hydrogen is pressurized and added to the central shaft 6 through the rotary joint 7 provided at the top of the central shaft 6. The hydrogen flows into the protective cover 521 and then flows into the stirring shaft 522. It is discharged into the reaction bed 5 through the air holes on the side wall of the stirring shaft 522. Because the stirring shaft 522 is in a rotating state, the hydrogen is fully mixed with the reactants. At the same time, under the stirring action, the degree of mixing is further improved, making the reaction more thorough. At the same time, the hydrogen in the stirring shaft is in a pressurized state, and the reactants flowing outside will not enter the stirring shaft. The addition of cold hydrogen not only replenishes the consumption of hydrogen in the mixed reactants, but also controls the temperature of the reactants, providing basic conditions for the next bed layer to continue the effective reaction.

[0058] As an embodiment of the present invention, the catalyst support plate 53 is provided with a number of through holes greater than one, wherein the upper diameter of the through hole is smaller than the lower diameter, the top of the through hole is a pedestal structure, an L-shaped joint 531 is fixed to the pedestal structure, a pipe is provided in the L-shaped joint 531, the bottom of the pipe is connected to the through hole, and the inlet is arranged horizontally;

[0059] The reaction zone is located above the catalyst support plate 53. The catalyst support plate 53 is used to support the catalyst. Through the design of the L-shaped joint 531, the catalyst will fall above the L-shaped joint 531 or between the pedestals during the stirring process, ensuring that the catalyst will not easily fall to the lower layer with the reactants. Instead, the reactants will flow normally into the L-shaped joint 531 as a fluid and then fall into the lower reaction bed 5, thereby ensuring the hydrogenation reaction effect of each layer of the reaction bed 5; the diameter of the through hole of the catalyst support plate 53 is small at the top and large at the bottom, ensuring the catalyst support effect without affecting the falling of the reactants.

[0060] As an embodiment of the present invention, the spacing between the stirring rods 523 on the stirring shaft 522 is greater than the diameter of the porcelain balls used in the reactor, and the inlet diameter of the L-shaped joint 531 is less than one-third of the diameter of the porcelain balls.

[0061] The inlet of the L-shaped joint 531 is smaller than one-third of the diameter of the porcelain ball, which ensures that the porcelain ball will not enter the L-shaped joint 531 and block the through hole. In addition, the large diameter difference also prevents the porcelain ball from being blocked at the inlet of the L-shaped joint 531, ensuring the smooth fall of the reactants in each layer of the reaction bed 5.

[0062] As an embodiment of the present invention, a scraper 524 is fixedly connected to the end of the stirring shaft 522 . The scraper 524 contacts the inner wall of the housing 1 and is made of rubber material.

[0063] During the rotation of the stirring shaft 522, in addition to stirring the reactants and catalyst, the scraper 524 at the end of the stirring shaft 522 can also clean the inner wall of the shell 1 of the reaction bed 5, reducing attachment waste and reducing the cost and time of subsequent cleaning.

[0064] As an embodiment of the present invention, the central shaft 6 and each layer are connected by sliding sealing.

[0065] Each layer of plates is fixed to the inside of the reactor, and the central axis 6 passes through each layer and is slidingly and sealingly connected to each layer. On the one hand, it prevents the leakage of reactants or catalysts from each layer. On the other hand, each layer of plates supports the central axis 6 and also plays a positioning role, thereby improving the stability of the reactor.

[0066] As an embodiment of the present invention, a pair of catalyst discharge pipes 11 are provided at the bottom of each layer of reaction bed 5 in the shell 1, and a catalyst addition port 12 is provided at the middle of each layer of reaction bed 5 in the shell 1. The catalyst addition port 12 is equipped with a flange-connected sealing cover 13.

[0067] Although the catalyst is not consumed during the reaction, the catalytic effect decreases as the number of reactions increases. After the reactor has been used for a period of time, the old catalyst needs to be unloaded through the catalyst unloading pipe 11, and new catalyst needs to be added to each layer of the reaction bed 5 through the catalyst addition port 12 to ensure the efficiency of the hydrogenation reaction; the sealing cover 13 of the catalyst addition port 12 is closed when the reactor is in operation, and the sealing cover 13 can be opened when the catalyst needs to be replaced.

[0068] As an embodiment of the present invention, a discharge port 14 is provided at the bottom of the shell 1, and a collector 8 is installed above the bottom discharge port 14 inside the shell 1. The collector 8 is a cap-shaped component with a circular hole on the top and a long hole on the side wall. The top of the collector 8 is slidably connected to the central shaft 6 through a bearing.

[0069] On the one hand, the collector 8 supports the central axis 6. On the other hand, the collector 8 also filters the output. The collector 8 can ensure that the bottom porcelain balls will not flow out, resulting in impure products. Furthermore, the size of the circular hole and the long hole on the top of the collector 8 needs to be adjusted according to the specifications of the porcelain balls used in the reactor.

[0070] Working principle: The mixture of raw materials and hydrogen enters the reactor through the feed port 21 of the upper head 2, and is diffused to the entire reactor cross section after rectification, throttling and collision by the diffuser. Then, the mixture passes through the distribution plate 4 and the upper partition 51 of the reaction bed 5 to further improve the flow condition, and enters the reaction bed 5. Ceramic balls and catalyst are added between the catalyst support plate 53 and the upper partition 51. The mixture is stirred by the stirring device 52. The gear shape design of the shaft end of the central shaft 6 and the stirring shaft 522 makes the directions of the adjacent central shaft 6 opposite. In addition to stirring the reactants and catalyst, the stirring shaft 522 also The stirring shafts 522 of the two adjacent layers of the reaction beds 5 are reversed in the horizontal direction, which enhances the stirring effect. In addition to rotating around its own axis, the stirring shaft 522 also rotates around the axis of the central shaft 6, further enhancing the stirring effect. In addition to playing a transmission role, the central shaft 6 also serves as a cold hydrogen pipe. Hydrogen is pressurized and added into the central shaft 6 through the rotary joint 7 provided at the top of the central shaft 6. The hydrogen flows into the protective cover 521 and then flows into the stirring shaft 522, and is discharged into the reaction bed 5 through the through-holes on the side wall of the stirring shaft 522. Because the stirring shaft 522 is in a rotating state, the stirring shaft 522 is rotated. The reaction zone is formed above the catalyst support plate 53, which is used to carry the catalyst. Through the design of the L-shaped joint 531, the catalyst will fall above the L-shaped joint 531 or between the pedestals during the stirring process, ensuring that the catalyst will not be easily moved by the reaction. The reactants fall to the lower layer, while the reactants as a fluid will normally flow into the L-shaped joint 531 and then fall to the lower reaction bed 5, thereby ensuring the hydrogenation reaction effect of each layer of the reaction bed 5; the diameter of the through hole of the catalyst support plate 53 is small at the top and large at the bottom, which ensures the catalyst support effect while not affecting the falling of the reactants; the reactants finally fall to the collector 8 area at the bottom, and the collector 8 plays a filtering role for the output, which can ensure that the bottom porcelain balls will not flow out, resulting in impure products. Furthermore, the size of the round hole and the long hole on the top of the collector 8 needs to be adjusted according to the specifications of the porcelain balls used in the reactor.

[0071] The technical features of the above embodiments can be combined arbitrarily. In order to make the description concise, not all possible combinations of the technical features in the above embodiments are described. However, as long as the combination of these technical features does not exist, the above embodiments only express several implementation methods of the present invention. The description is relatively specific and detailed, but it cannot be understood as limiting the scope of the invention patent. It should be pointed out that for ordinary technicians in this field, without departing from the concept of the present invention, several variations and improvements can be made, which all fall within the scope of protection of the present invention. Therefore, the scope of protection of the patent of the present invention should be based on the attached claims.

Claims

1. A liquid phase hydrogenation reactor for chemical production, comprising a shell (1), an upper head (2), a top diffuser (3) and a distribution plate (4), wherein the upper head (2) is located at the top of the shell (1), a feed port (21) is provided on the upper head (2), the top diffuser (3) is installed inside the upper head (2), and the distribution plate (4) is located below the top diffuser (3), characterized in that: Also includes: A reaction bed (5), wherein the reaction bed (5) has a plurality of layers, which are evenly arranged with equal spacing from top to bottom; The central shaft (6) is driven by a motor located on the top of the upper head (2); the reaction bed (5) is composed of an upper partition (51), a stirring device (52) and a catalyst support plate (53) from top to bottom, and the stirring device (52) is located between the upper partition (51) and the catalyst support plate (53); porcelain balls and catalysts are added between the catalyst support plate (53) and the upper partition (51); The catalyst support plate (53) is provided with a number of through holes greater than one, the upper diameter of the through hole is smaller than the lower diameter, the top of the through hole is a pedestal structure, an L-shaped joint (531) is fixed to the pedestal structure, a pipe is provided in the L-shaped joint (531), the bottom of the pipe is connected to the through hole, and the inlet is arranged horizontally; The stirring device (52) comprises: a protective cover (521), wherein the protective cover (521) is a conical structure with upper and lower surfaces protruding outwards; The stirring shaft (522) has two stirring pumps in the same reaction bed (5) layer and is installed horizontally; the spacing between the stirring rods (523) on the stirring shaft (522) is greater than the diameter of the porcelain balls used in the reactor, and the inlet diameter of the L-shaped joint (531) is less than one-third of the diameter of the porcelain balls.

2. A liquid phase hydrogenation reactor for chemical production according to claim 1, characterized in that: The central shaft (6) is a multi-stage structure, and the relative cross-sectional position between two adjacent stages is a bevel gear structure; a stirring rod (523) is fixedly connected to the stirring shaft (522), and the number of the stirring rods (523) is greater than one and is linearly arranged on both sides of the stirring shaft (522); one end of the stirring shaft (522) is a bevel gear structure, and the two stirring shafts (522) in the same reaction bed (5) layer and the upper and lower central shafts (6) are cross-engaged in the same vertical plane through the bevel gear and bevel gear structure, and the engagement position is located inside the protective cover (521).

3. A liquid phase hydrogenation reactor for chemical production according to claim 2, characterized in that: The central shaft (6) is a hollow tubular structure, and the central shaft (6) is fixedly connected to the top motor via a rotary joint (7); the stirring shaft (522) is a hollow structure and a vertical through hole is opened on the side wall.

4. A liquid phase hydrogenation reactor for chemical production according to claim 2, characterized in that: The central shaft (6) of each section is connected to the stirring shaft (522) and the protective cover (521) through a bearing sliding seal.

5. A liquid phase hydrogenation reactor for chemical production according to claim 2, characterized in that: A scraper (524) is fixedly connected to the end of the stirring shaft (522), and the scraper (524) contacts the inner wall of the shell (1). The scraper (524) is made of rubber material.

6. A liquid phase hydrogenation reactor for chemical production according to claim 1, characterized in that: The central shaft (6) and each layer are connected by sliding sealing.

7. A liquid phase hydrogenation reactor for chemical production according to claim 1, characterized in that: The shell (1) is provided with a pair of catalyst discharge pipes (11) at the bottom of each layer of the reaction bed (5), and the shell (1) is provided with a catalyst addition port (12) at the middle of each layer of the reaction bed (5). The catalyst addition port (12) is provided with a sealing cover (13) connected with a flange.

8. The liquid phase hydrogenation reactor for chemical production according to claim 1, characterized in that: A discharge port (14) is provided at the bottom of the shell (1), and a collector (8) is installed above the discharge port (14) at the bottom of the shell (1). The collector (8) is a cap-shaped component with a circular hole on the top and a long hole on the side wall. The top of the collector (8) is slidably connected to the central shaft (6) through a bearing.

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