A parallel fixed bed reactor

Abstract

The utility model discloses a kind of parallel fixed bed reactors, belong to fixed bed reactor technical field, the parallel fixed bed reactor includes reaction layer, reaction layer includes at least one reaction tube, be located in reactor inner cavity, wherein, the reaction tube includes inner tube and outer tube, the outer tube is used to pass into heat exchange medium, inner tube fills catalyst, for passing into catalyst and reaction raw material, under the action of catalyst, reaction product is generated;Support layer is located above and below heat exchange layer, the support layer is communicated with the inner tube of reaction tube, for supporting catalyst, the application adopts porcelain ball as support layer, for supporting catalyst, reaction raw material is entered into each reaction tube through support layer, pre-distribution is carried out to gas-liquid mixture, it is favorable to improve the uniformity of reactant distribution in each reaction tube, while being equipped with booster assembly, by artificially increasing pressure drop, increase overall pressure drop, and then reduce the difference of pressure drop in different reaction tube.

Description

Technical Field

[0001] This utility model belongs to the field of fixed bed reactor technology, and more specifically, relates to a parallel fixed bed reactor. Background Technology

[0002] A fixed-bed reactor is a device in which a catalyst or solid reactant is fixed within a bed, and a fluid (gas or liquid) flows through the bed to carry out the reaction. It is widely used in chemical, energy, and other fields. For strongly endothermic or strongly exothermic fixed-bed reactors, to maintain the reaction under relatively stable temperature conditions, certain requirements are generally placed on the heat exchange performance of the fixed-bed reactor. Traditional fixed-bed reactors enhance the heat exchange effect by extending the heat exchange path, but the heat exchange effect is limited. Heat exchange tube fixed-bed reactors use heat exchange tubes installed within or around the bed, and control the reaction temperature through a heat transfer medium (such as water or thermal oil). However, using heat exchange tubes as reaction tubes also has some problems. When the reactants enter the reactor through the inlet, compared to the reaction tubes at the two ends with longer paths, gases are more likely to enter the middle reaction tube first, leading to uneven distribution of reactants in each reaction tube. This is especially true in gas-liquid reactions, where the gas-liquid ratio varies greatly. Furthermore, because the reactants enter different reaction tubes via different paths, the residence time of the reactants in each reaction tube varies, resulting in inconsistent final reaction products. Utility Model Content

[0003] 1. The problem to be solved To address the problem of uneven gas-liquid feeding in existing parallel fixed-bed reactors for gas-liquid reactions, the present invention aims to provide a parallel fixed-bed reactor.

[0004] 2. Technical Solution To solve the above problems, the present invention adopts the following technical solution.

[0005] The purpose of this invention is to provide a parallel fixed-bed reactor, which includes: The reactor shell forms the reactor cavity, with an inlet at the bottom for the reaction raw materials to enter and an outlet at the top for the reaction products to exit. A reaction layer includes at least one reaction tube disposed in the inner cavity of a reactor. The reaction tube includes an inner tube and an outer tube. The outer tube is used to introduce a heat exchange medium, and the inner tube is filled with a catalyst and used to introduce reaction raw materials to generate reaction products under the action of the catalyst. A support layer is disposed above and below the heat exchange layer, and the support layer is connected to the inner tube of the reaction tube to support the catalyst.

[0006] According to one embodiment of the present invention, multiple reaction tubes are arranged vertically and parallel inside the reactor shell.

[0007] According to one embodiment of the present invention, the support layer is composed of ceramic balls, which fill the space above and below the reaction layer to form a support layer for supporting the catalyst. Specifically, the ceramic balls fill the space between the top of the reaction layer and the outlet, preferably filling the space between the top of the reaction layer and the outlet; the ceramic balls also fill the space between the bottom of the reaction layer and the inlet, preferably filling the space between the bottom of the reaction layer and the inlet, forming a support layer for supporting the catalyst.

[0008] According to one embodiment of the present invention, the lower end of the reaction tube is connected to a pressurization assembly. The pressurization assembly includes a guide pipe and a sieve plate with several through holes. The through holes of the sieve plate are connected to the lower end of the inner tube of the reaction tube through the guide pipe.

[0009] According to one embodiment of the present invention, the number of the guide tubes corresponds to the number of reaction tubes, that is, the upper end of each guide tube is connected to the inner tube of a reaction tube. Preferably, the lower end of each guide tube is connected to a through hole, so that the reaction raw materials below the sieve plate enter the inner tube of the reaction tube along the guide tubes and generate reaction products under the action of the catalyst.

[0010] According to one embodiment of the present invention, the upper end of the reaction tube is connected to a pressurizing component. The pressurizing component includes a guide tube and a sieve plate with several through holes. The through holes of the sieve plate are connected to the upper end of the inner tube of the reaction tube through the guide tube. The number of guide tubes corresponds to the number of reaction tubes, that is, the lower end of each guide tube is connected to the inner tube of a reaction tube. Preferably, the upper end of each guide tube is connected to a through hole, so that the reaction products enter the guide tube along the inner tube of the reaction tube and are then discharged from the sieve plate.

[0011] According to one embodiment of the present invention, the diameter of the guide tube is smaller than the diameter of the inner tube of the reaction tube, which is used to increase the pressure drop of the inner tube of the reaction tube. The ratio of the diameter of the guide tube to the diameter of the inner tube of the reaction tube is (0.3-0.8):1, preferably (0.3-0.5):1.

[0012] According to one embodiment of the present invention, the length of the guide tube is 0.1m-0.20m, and the length of the reaction tube is generally 3-13m. The length of the reaction tube can be adjusted according to the reaction requirements.

[0013] According to one embodiment of the present invention, the inner wall of the guide tube is provided with at least one fin to increase the resistance of the reactants, thereby increasing the pressure drop. At the same time, the reactants are mixed back and forth under the guiding action of the fins, improving the uniformity of gas-liquid mixing. The fins can be arranged in a circle along the inner wall of the guide tube or at intervals, and their shape can be a sloping surface or a circular arc surface.

[0014] According to one embodiment of the present invention, the end of the guide tube extends into the inner tube of the reaction tube, and the end of the guide tube is provided with an end cap. The opening diameter of the end cap is smaller than the minimum particle size of the catalyst to prevent the catalyst from falling into the guide tube.

[0015] It should be noted that catalysts of different particle sizes and shapes have different pressure drops. For example, the smaller the particles, the greater the pressure drop produced by the catalyst. Long, strip-shaped catalysts produce a greater pressure drop than round catalysts.

[0016] According to one embodiment of the present invention, the pressure drop in the guide tube is greater than or equal to the pressure drop in the reaction tube. Preferably, the pressure drop in the guide tube : pressure drop in the reaction tube is (1-8):1. More preferably, the pressure drop in the guide tube : pressure drop in the reaction tube is (1-5):1. By artificially increasing the pressure drop, the overall pressure drop is increased, thereby reducing the difference in pressure drop between different reaction tubes. For example, if the maximum difference in pressure drop between reaction tubes is 20%, by adding a guide tube, the difference in pressure drop is reduced to only 5%, thus reducing the difference in pressure drop between different reaction tubes.

[0017] According to one embodiment of the present invention, the heat exchange medium inlet is connected above the outer tube of the reaction tube, and the heat exchange medium outlet is connected below the outer tube, so that the heat exchange medium and the reactants flow in opposite directions. By using a reaction tube with a sleeve structure, the flow path of the heat exchange medium is strictly constrained, making it flow in the opposite direction to the reactants, thereby improving heat exchange efficiency.

[0018] According to one embodiment of the present invention, the reaction tube is fixed in the inner cavity of the reactor by a fixing plate, and the upper end and the lower end of the reaction tube are respectively fixed by the fixing plate.

[0019] According to one embodiment of the present invention, the reactor cavity is further provided with at least one baffle plate, the baffle plates are parallel to each other and fixed to the side wall of the reactor cavity, the baffle plate is perpendicular to the side wall of the reactor cavity, and is fixedly connected to the reaction tube to support the reaction tube. The flow of reactants in the reaction tube causes the reaction tube to vibrate unavoidably. By supporting the reaction tube with the baffle plate, the reaction tube is fixed on the one hand, and the structural stability of the reaction tube is improved on the other hand.

[0020] According to one embodiment of the present invention, the connection between the guide tube and the sieve plate is provided with a flared opening, the diameter of which is larger than the diameter of the guide tube, thereby reducing the resistance of the reaction raw materials entering and exiting the guide tube.

[0021] According to one embodiment of the present invention, a feeder is also included, which is located at the feed inlet of the reactor and is used to evenly distribute the reaction raw materials into the reactor. The reaction raw materials are introduced into the reaction tube after being fully mixed. For example, when the introduced reaction raw materials are a gas-liquid mixture, they are mixed into an emulsion to make them evenly mixed.

[0022] The reactor described in this application is suitable for gas-gas reactions, gas-liquid reactions, and liquid-liquid reactions.

[0023] 3. Beneficial effects Compared with the prior art, the beneficial effects of this utility model are as follows: (1) The reaction tube of this application uses ceramic balls as a support layer to support the catalyst. The reaction raw materials enter each reaction tube through the support layer formed by the ceramic ball particles, pre-distributing the gas-liquid mixture, avoiding the gas from directly entering the middle reaction tube, and improving the uniformity of the distribution of reactants in each reaction tube. (2) The reaction tube of this application uses ceramic balls as a support layer. The support layer is evenly distributed under the catalyst, which reduces the risk of the catalyst falling off. When it needs to be replaced and disassembled, the ceramic balls are released by opening the unloading port of the support layer, and the catalyst is also completely removed, which realizes the rapid replacement of the catalyst and reduces maintenance costs and reaction risks. (3) The present application further provides a pressurization component at the upper and lower ends of the reaction tube. By artificially increasing the pressure drop, the overall pressure drop is increased, thereby reducing the pressure drop difference in different reaction tubes, thereby improving the consistency of the residence time of reactants in each reaction tube and improving the consistency of the reaction. (4) This application will use a heat exchange tube containing an inner tube and an outer tube as the reaction tube. The catalyst is placed in the inner tube and the heat exchange medium flows in the outer tube. The flow direction of the heat exchange medium is opposite to the flow direction of the reaction raw materials, so as to ensure that the heat exchange medium flows countercurrently on the outer layer of the catalyst, thereby improving the heat exchange effect. The heat in the reaction process can be quickly discharged to avoid high temperature deactivation of the catalyst, reduce safety risks, reduce the occurrence of side reactions, and improve reaction selectivity. Attached Figure Description

[0024] The technical solution of this utility model will be further described in detail below with reference to the accompanying drawings and embodiments. However, it should be understood that these drawings are designed for illustrative purposes only and are not intended to limit the scope of this utility model. In addition, unless otherwise specified, these drawings are intended only to conceptually illustrate the structural construction described herein and are not necessarily drawn to scale.

[0025] Figure 1 This is a schematic diagram of the parallel fixed-bed reactor of this application; Figure 2 This is a schematic diagram of the structure of the reaction tube and the flow guide tube of this application; Figure 3This is a schematic diagram of the flow guide tube in this application; In the diagram: 1. Reactor shell; 11. Inlet; 111. Feeder; 12. Outlet; 2. Reaction layer; 21. Reaction tube; 211. Inner tube; 212. Outer tube; 22. Pressurization assembly; 221. Guide tube; 2211. Flange; 2212. End cap; 222. Sieve plate; 23. Heat exchange medium inlet; 24. Heat exchange medium outlet; 25. Exhaust port; 26. Manhole; 27. Fixing plate; 28. Baffle plate; 3. Support layer; 31. Catalyst and ceramic ball inlet; 32. Discharge port. Detailed Implementation

[0026] The following detailed description and exemplary embodiments of the present invention can be better understood in conjunction with the accompanying drawings, wherein the elements and features of the present invention are identified by reference numerals.

[0027] Example This embodiment includes a parallel fixed-bed reactor, such as... Figure 1-3 As shown, it includes: The reactor shell 1 forms the reactor cavity. The lower part of the cavity is provided with an inlet 11 for the introduction of reaction raw materials, and the upper part of the cavity is provided with an outlet 12 for the discharge of reaction products. The reaction layer 2 includes at least one reaction tube 21 located in the inner cavity of the reactor. The reaction tube 21 includes an inner tube 211 and an outer tube 212. The outer tube 212 is used to introduce a heat exchange medium, and the inner tube 211 is filled with a catalyst and used to introduce reaction raw materials to generate reaction products under the action of the catalyst. Support layers 3 are respectively disposed above and below reaction layer 2 to support the catalyst, wherein the inner tube 211 of reaction tube 21 is connected to support layer 3.

[0028] This embodiment contains multiple reaction tubes 21, which are arranged vertically and parallel to each other inside the reactor shell 1.

[0029] The support layer 3 is made of ceramic balls, which fill the space between the top of the reaction layer 2 and the outlet 12, and fill the space between the bottom of the reaction layer 2 and the inlet 11, forming the support layer 3 that supports the catalyst.

[0030] The reaction tube 21 is fixed in the inner cavity of the reactor by a fixing plate 27, and both its upper and lower ends are fixed by the fixing plate 27.

[0031] The reactor cavity is also provided with at least one baffle 28, which are parallel to each other and fixedly installed on the side wall of the reactor cavity. The baffle 28 is perpendicular to the side wall of the reactor cavity and is fixedly connected to the reaction tube 21 to support the reaction tube 21. The flow of reactants in the reaction tube 21 causes the reaction tube 21 to vibrate unavoidably. By supporting the reaction tube 21 with the baffle 28, the reaction tube 21 is fixed. On the other hand, the actual material flows in the reaction tube 21, and the reaction tube 21 will vibrate to a certain extent. By fixing the reaction tube 21 with the baffle 28, the impact of vibration on the structural stability of the reaction tube 21 is reduced.

[0032] Traditional fixed-bed reactors typically use sieve plates to support the catalyst, forming a fixed bed with cavities at both ends. When the reactants enter the reactor through the feed inlet 11, they first enter the cavities. Compared to the longer reaction tubes 21 at the ends, the gas in the reactants is more likely to enter the middle reaction tube 21 first, resulting in uneven distribution of the reactants in each reaction tube 21. This is especially true in gas-liquid reactions, where the gas-liquid ratio varies greatly, leading to more byproducts in the final reaction. Furthermore, because the reactants enter different reaction tubes 21 via different paths, the residence time of the reactants in each reaction tube 21 varies. For example, in the reaction tube 21 perpendicular to the inlet and outlet, the reactants follow a straight path and have a short residence time. In contrast, in the reaction tubes at both ends, the reactants follow a longer path and have a longer residence time, resulting in inconsistent reaction products.

[0033] To address the aforementioned issues, this application incorporates ceramic spheres above and below the catalyst. These spheres serve as a support layer 3, supporting the catalyst and forming a stable fixed bed. They also pre-distribute the gas-liquid mixture. The ceramic spheres accumulate to form a porous layer with uniform pores. When the reactants enter the reactor cavity through the feed inlet 11, the gas enters the reaction tube 21 through the gaps in the ceramic spheres. Experiments have shown that after distribution by the ceramic spheres, the amount of gas entering each reaction tube 21 is approximately the same, effectively improving the consistency of the reactant ratio in each reaction tube 21.

[0034] It should be noted that another function of using ceramic balls as the support layer 3 in this application is to reduce maintenance costs and reaction risks. When the catalyst in the traditional reaction tube 21 is supported by a sieve plate instead of ceramic balls, the bottom of the reaction tube 21 is connected and fixed to the sieve plate. When it needs to be replaced or disassembled, the reaction tubes 21 need to be disassembled one by one. When the reactor is large, there may be thousands of reaction tubes 21, and disassembling them one by one is a huge workload. In addition, if the connecting parts at the bottom of the reaction tube 21 fail and the catalyst falls off, the reactor cannot operate normally. The reaction raw materials tend to rise directly from the empty reaction tube 21 with less resistance, causing the reaction to fail.

[0035] This application uses ceramic balls as the catalyst support layer 3, eliminating the need for connecting components. The support layer 3 is evenly distributed below the catalyst, eliminating the risk of the catalyst falling off and effectively reducing the reaction risk. When replacement or disassembly is required, the ceramic balls are released by opening the discharge port 32 of the support layer 3, and the catalyst is also completely removed, achieving rapid catalyst replacement.

[0036] That is, the present application provides a reaction layer 2 composed of catalyst and a support layer 3 composed of ceramic balls in the inner cavity of the reactor. The support layer 3 is located at the upper and lower ends of the reaction layer 2. When the reaction raw materials enter the inner cavity of the reactor through the lower feed port 11, they first pass through the lower support layer 3, and through the distribution effect of the ceramic balls, they enter the catalyst bed relatively evenly, and then pass out through the discharge port 12, which effectively improves the consistency of the reaction.

[0037] However, reactions are generally strongly endothermic or exothermic. Without a heat exchange medium, the reaction temperature is difficult to control. To improve heat exchange, some existing technologies involve wrapping a jacket containing the heat exchange medium around the outer wall of the reactor for heat exchange during the reaction. However, this method cannot exchange heat in the middle part of the catalyst, especially for larger reactors, where heat exchange can only continue on the surface, resulting in concentrated heat and sustained high temperatures in the middle. Other methods involve introducing a heat exchange medium outside the reaction tube 21 and adding baffles to improve the heat exchange path. However, these methods have low heat exchange efficiency, and under high-temperature conditions, they can not only deactivate the catalyst but also... To prevent the generation of byproducts, this application divides the large-diameter reactor into several small-diameter (e.g., tens of micrometers) reactors to improve heat dissipation. A reaction tube 21 containing an inner tube 211 and an outer tube 212 is used. The catalyst is placed in the inner tube 211, and the heat exchange medium flows in the outer tube 212. The flow direction of the heat exchange medium is opposite to that of the reactants, ensuring countercurrent flow of the heat exchange medium on the outer layer of the catalyst. This improves the heat exchange effect, allows for rapid heat removal during the reaction process, avoids high-temperature deactivation of the catalyst, reduces safety risks, minimizes side reactions, and improves reaction selectivity.

[0038] In fact, the reaction tube 21 also serves to uniform the temperature, i.e., it is an isothermal reactor, which is especially suitable for reactions with high temperature requirements. The large-sized reaction tube 21 is long and the reaction path is also long, resulting in a large temperature difference between the top and bottom and inconsistent reaction temperatures. This application improves the heat exchange efficiency of the reaction tube 21 to keep the entire reactor at a relatively uniform temperature, which is beneficial to improving the consistency of the reaction and reducing the generation of by-products.

[0039] However, the aforementioned reaction tubes 21 also have some problems: due to the different paths of the reactants entering different reaction tubes 21, the residence time of the reactants in each reaction tube 21 is different. For example, in reaction tubes 21 perpendicular to the inlet and outlet, the path of the reactants is a straight line, with a small pressure drop and a short residence time. In contrast, in reaction tubes 21 closer to the inner wall of the reactor, the path of the reactants is longer, with a large pressure drop and a long residence time. Although the porous structure of the ceramic balls can reduce the difference in the path of the reactants entering the reaction tubes 21 to some extent, some differences still exist. At the same time, the packing of the catalyst in the reaction tubes 21 also leads to differences in pressure drop. In fact, the packing density and distribution of the catalyst cannot be precisely controlled, resulting in different pressure drops in different reaction tubes 21. The above reasons lead to differences in the residence time of the reactants in different reaction tubes 21, for example, 20%-30%, which in turn leads to inconsistent reaction products. When the reaction is a gas-liquid reaction, the gas and liquid have different densities. Directly introducing the gas into the reactor can cause it to drift, resulting in different gas-to-liquid ratios in each reaction tube 21. For example, some reaction tubes 21 may have more gas and less liquid, while others may have less gas and more liquid, leading to different reactant compositions. Simultaneously, the different gas and liquid flow rates result in different residence times within the reaction tubes 21, causing varying reaction times and potentially leading to under- or over-reaction. Therefore, this application further provides a pressurization assembly 22 at the upper and lower ends of the reaction tube 21. The pressurization assembly 22 is embedded in ceramic balls, connected above to the inner tube 211 of the reaction tube 21, and its sidewalls and lower surface are embedded in a support layer 3 composed of ceramic balls. The specific structure of the pressurization assembly 22 is as follows: Figure 2-3 As shown: Below the reaction tube 21, a pressurizing component 22 is provided. The pressurizing component 22 includes a sieve plate 222 with several through holes. A guide tube 221 is provided between the through holes of the sieve plate 222 and the lower end of the inner tube 211 of the reaction tube 21. The number of guide tubes 221 corresponds to the number of through holes and the number of reaction tubes 21. That is, the upper end of each guide tube 221 is connected to the inner tube 211 of a reaction tube 21, and the lower end of each guide tube 221 is connected to a through hole. This allows the reaction raw materials below the sieve plate 222 to pass through the gaps between the ceramic balls and enter the inner tube 211 of the reaction tube 21 along the guide tube 221, where they generate reaction products under the action of the catalyst.

[0040] A pressurizing component 22 is provided above the reaction tube 21. The pressurizing component 22 includes a sieve plate 222 with several through holes. A guide tube 221 is provided between the through holes of the sieve plate 222 and the upper end of the inner tube 211 of the reaction tube 21. The number of guide tubes 221 corresponds to the number of through holes and the number of reaction tubes 21. That is, the lower end of each guide tube 221 is connected to the inner tube 211 of a reaction tube 21, and the upper end of each guide tube 221 is connected to a through hole. This allows the reaction products to pass through the gaps between the ceramic balls and enter the guide tube 221 along the inner tube 211 of the reaction tube 21, and then be discharged from the sieve plate 222.

[0041] In fact, the number of guide tubes 221 and the number of through holes may not correspond. The sieve plate 222 serves to support the ceramic balls and the guide tubes 221. A very small amount of reaction material passes through the gaps between the ceramic balls and enters the space above the sieve plate 222 through the through holes. However, since the gap between the inner tube 211 of the reaction tube 21 and the guide tube 221 is small, the reaction material is difficult to enter the inner tube 211 of the reaction tube 21 directly through this point, and has little impact on the reaction.

[0042] The diameter of the guide tube 221 is smaller than the diameter of the inner tube 211 of the reaction tube 21, which is used to increase the pressure drop in the inner tube 211 of the reaction tube 21. Preferably, the ratio of the diameter of the guide tube 221 to the diameter of the reaction tube 21 is (0.3-0.8):1, more preferably (0.3-0.5):1. For example, the inner tube 211 of the reaction tube 21 can have a diameter of 25mm, 38mm, or 45mm; the guide tube 221 can have a diameter of 17mm, 25mm, or 32mm.

[0043] The length of the guide tube 221 is 0.05m-0.20m, and the length of the reaction tube 21 is generally 1-12m. Preferably, the ratio of the length of the guide tube 221 to the length of the reaction tube 21 is (5-240):1. The length of the reaction tube 21 can be adjusted according to the reaction requirements.

[0044] To increase the resistance of the reactants and thus increase the pressure drop, a ring of fins is provided on the inner wall of the guide tube 221. While increasing the pressure drop, the reactants are mixed back and forth under the guiding action of the fins, thereby improving the uniformity of gas-liquid mixing.

[0045] like Figure 3 As shown, the connection between the guide pipe 221 and the sieve plate 222 is provided with a flared opening 2211. The diameter of the flared opening 2211 is larger than the diameter of the guide pipe 221, which reduces the resistance of the reaction raw materials entering and exiting the guide pipe 221, so that the reaction raw materials enter the guide pipe 221 through the lower end of the guide pipe 221, and then enter the inner tube 211 of the reaction pipe 21.

[0046] The end of the guide tube 221 extends into the inner tube 211 of the reaction tube 21. An end cap 2212 is provided at the end of the guide tube 221. The opening diameter of the end cap 2212 is smaller than the minimum particle size of the catalyst to prevent the catalyst from falling into the guide tube 221. In this embodiment, the opening diameter is less than 2 μm, and preferably, its ratio to the size of the catalyst is 0.2-0.5 to prevent catalyst particles from falling out.

[0047] It should be noted that catalysts of different particle sizes and shapes have different pressure drops. For example, the smaller the particles, the greater the pressure drop produced by the catalyst. Long, strip-shaped catalysts produce a greater pressure drop than round catalysts.

[0048] The pressure drop generated in the guide tube 221 is greater than or equal to the pressure drop in the reaction tube 21. Preferably, the pressure drop in the guide tube 221 : pressure drop in the reaction tube 21 is (1-8):1. More preferably, the pressure drop in the guide tube 221 : pressure drop in the reaction tube 21 is (1-5):1. For example, if the maximum pressure drop difference in the reaction tube 21 is 20%, by adding the guide tube 221, the pressure drop difference is reduced to only 5%, thus reducing the pressure drop difference in different reaction tubes 21. The pressure drop generated in the guide tube 221 cannot be too low, otherwise it will not be able to increase the pressure drop. The pressure drop in the guide tube 221 cannot be too high either. When the reactants are a gas-liquid mixture, if the pressure is too high, the mixture will be directly discharged from the guide tube 221, causing a sudden drop in pressure above the guide tube 221. This decompression leads to the vaporization of some reactants.

[0049] The heat exchange medium inlet 23 is connected above the outer tube 212 of the reaction tube 21, and the heat exchange medium outlet 24 is connected below the outer tube 212 of the reaction tube 21, so that the heat exchange medium and the reactants flow in opposite directions. The reaction tube 21, with its sleeve structure, strictly restricts the flow path of the heat exchange medium, making it flow in the opposite direction to the reactants, thereby improving heat exchange efficiency.

[0050] The parallel fixed-bed reactor also includes a feeder 111, located at the reactor inlet 11, for uniformly distributing the reaction raw materials into the reactor. The feeder 111 introduces the reaction raw materials into the reaction tube 21 after thorough mixing. For example, when the introduced reaction raw materials are a gas-liquid mixture, they are mixed into an emulsion to ensure uniform mixing.

[0051] The reactor described in this application is suitable for gas-gas reactions, gas-liquid reactions, and liquid-liquid reactions.

[0052] When the reactor is used for gas-liquid reaction, the support layer 3 below the reaction tube 21 is first filled with ceramic balls; then the catalyst is filled into the inner tube 211 of the reaction tube 21 through the catalyst and ceramic ball inlet 31; finally, the support layer 3 above the reaction tube 21 is filled with ceramic balls.

[0053] The reaction material is fed into the pre-filled reactor to carry out the reaction. The reaction material first enters the reactor through the feeder 111, then enters the guide pipe 221 through the support layer 3 filled with ceramic balls, and then flows to the reaction pipe 21 to carry out the reaction. The mixture after the reaction flows out through the guide pipe 221.

[0054] An exhaust port 25 is opened on the side wall of the cavity formed between the two fixed plates 27. When the reaction temperature changes and causes the air pressure in the cavity to change, the air pressure is balanced through the exhaust port 25.

[0055] In addition, a manhole 26 is provided on the side wall of the reactor to facilitate the installation and disassembly of components inside the parallel fixed bed reactor.

[0056] The above description is only a preferred embodiment of this application and an explanation of the technical principles used. Those skilled in the art should understand that the scope involved in this application is not limited to the technical solutions formed by a specific combination of the above technical features, but should also cover other technical solutions formed by any combination of the above technical features or their equivalent features without departing from the inventive concept. For example, technical solutions formed by replacing the above features with (but not limited to) technical features with similar functions disclosed in this application.

[0057] Apart from the technical features described in the specification, the other technical features are known to those skilled in the art. To highlight the innovative features of this utility model, the other technical features will not be described in detail here.

Claims

1. A parallel fixed-bed reactor, comprising: The reactor shell (1) forms the reactor cavity. The lower part of the reactor cavity is provided with an inlet (11) for the reaction raw materials to enter, and the upper part of the reactor cavity is provided with an outlet (12) for the reaction products to exit. The reaction layer (2) includes at least one reaction tube (21) disposed in the inner cavity of the reactor; The reaction tube (21) is characterized in that it includes an inner tube (211) and an outer tube (212), the outer tube (212) is used to introduce a heat exchange medium, and the inner tube (211) is filled with a catalyst and used to introduce reaction raw materials to generate reaction products under the action of the catalyst. It also includes a support layer (3), which is disposed above and below the reaction layer (2), and the support layer (3) is connected to the inner tube (211) of the reaction tube (21) to support the catalyst.

2. The parallel fixed-bed reactor according to claim 1, characterized in that, The support layer (3) is made of ceramic balls, which are filled between the top of the reaction layer (2) and the outlet (12), and between the bottom of the reaction layer (2) and the inlet (11), forming a support layer (3) that supports the catalyst.

3. The parallel fixed-bed reactor according to claim 1, characterized in that, Multiple reaction tubes (21) are arranged vertically and parallel inside the reactor shell (1).

4. The parallel fixed-bed reactor according to claim 1, characterized in that, The reaction tube (21) is provided with a pressurizing component (22) at both ends. The pressurizing component (22) includes a guide pipe (221) and a sieve plate (222) with through holes. One end of the guide pipe (221) is connected to the through hole of the sieve plate (222), and the other end is connected to the inner tube (211) of the reaction tube (21), so that the reaction raw materials below the sieve plate (222) enter the inner tube (211) of the reaction tube (21) along the guide pipe (221).

5. The parallel fixed-bed reactor according to claim 4, characterized in that, The pressure drop in the flow guide (221) is greater than or equal to the pressure drop in the reaction tube (21); and / or, Pressure drop in the flow guide tube (221): Pressure drop in the reaction tube (21) is (1-8):

1.

6. The parallel fixed-bed reactor according to claim 4, characterized in that, The diameter of the guide tube (221) is smaller than the diameter of the inner tube (211) of the reaction tube (21); and / or, The ratio of the diameter of the guide tube (221) to the diameter of the inner tube (211) of the reaction tube (21) is (0.3-0.8):

1.

7. The parallel fixed-bed reactor according to claim 4, characterized in that, The inner wall of the guide tube (221) is provided with at least one fin.

8. The parallel fixed-bed reactor according to claim 4, characterized in that, The end of the guide tube (221) extends into the inner tube (211) of the reaction tube (21), and the end of the guide tube (221) is provided with an end cap (2212), the opening diameter of the end cap (2212) being smaller than the minimum particle size of the catalyst.

9. The parallel fixed-bed reactor according to claim 1, characterized in that, The heat exchange medium inlet (23) is connected above the outer tube (212) of the reaction tube (21), and the heat exchange medium outlet (24) is connected below the outer tube (212) of the reaction tube (21), so that the heat exchange medium and the reaction raw materials flow in opposite directions.

10. The parallel fixed-bed reactor according to claim 1, characterized in that, The reaction tube (21) is fixed in the inner cavity of the reactor by a fixing plate (27), and the upper end and the lower end of the reaction tube (21) are fixed by the fixing plate (27) respectively; The reactor cavity is also provided with at least one baffle (28), which is parallel to each other and fixedly installed on the side wall of the reactor cavity. The baffle (28) is perpendicular to the side wall of the reactor cavity and is fixedly connected to the reaction tube (21) to support the reaction tube (21).

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