A solid catalyst catalytic gas-liquid reaction device with cyclone separation

Abstract

This utility model relates to the technical field of gas-liquid reaction devices, and more particularly to a solid catalyst catalytic gas-liquid reaction device with cyclone separation. By incorporating a cyclone separator within the reaction body, the reaction body is divided from bottom to top into a reaction zone, a sedimentation separation zone, and an escape buffer zone. Combined with raw material inlet, gas inlet, and cyclone liquid inlet located at the bottom of the reaction body, the material and solid catalyst in the reaction zone are suspended upwards after material flows in. As the material feed rate gradually increases, the reaction products and solid catalyst enter the sedimentation separation zone. The free sedimentation of particles in the slurry and the cyclone separation by the cyclone separator cause the solids and particles discharged from the solid outlet to settle and return to the reaction zone to participate in the reaction. Furthermore, the cyclone liquid from the cyclone separator circulates back into the reaction zone for further reaction. Simultaneously, the product outlet gradually discharges the products, helping to improve the completeness of the raw material reaction and enhance the quality of the reaction products.

Description

Technical Field

[0001] This utility model relates to the field of gas-liquid reaction device technology, and in particular to a solid catalyst catalytic gas-liquid reaction device with swirl separation. Background Technology

[0002] Gas-liquid catalytic reactions are common in the chemical industry. They are chemical reactions that occur when gas and liquid come into contact under the catalysis of a catalyst. Common reactions include: (1) waste gas treatment, such as waste gas containing harmful elements such as S, N, and F being absorbed and purified by liquid under the action of a solid catalyst. (2) organic liquid hydrogenation reaction, such as the hydrogenation reaction of cyclohexene. After cyclohexene is prepared into an organic solution, the hydrogen pumping pressure is controlled, and the reaction is carried out at 80°C under the catalysis of a palladium-on-carbon catalyst. However, these reactions all require the use of a catalytic reaction device, and the structure of the catalytic reaction device is closely related to the catalyst utilization efficiency and product quality.

[0003] Currently, existing gas-liquid catalytic reaction devices mainly fall into two categories: batch reactors and tower reactors. Batch reactors require stirring paddles to suspend the solid catalyst and gas-liquid mixture. However, experimental verification shows that a 10m³ batch reactor consumes up to 8 kW·h / ton of product for suspension, which is relatively high. Furthermore, the catalyst settling rate in stirred reactors is high, resulting in a large amount of catalyst not participating in the recycling reaction, leading to low catalyst utilization. Tower reactors mainly consist of a spray-treatment tower structure. Due to the short contact time between gas and liquid in the spray tower, the product residue rate is high, resulting in low reaction efficiency. Therefore, improving catalyst utilization and the quality of reaction products has become a key research focus in the field of gas-liquid catalytic reaction devices, and has been studied accordingly.

[0004] For example, patent application number 201910342691.6 discloses a method and apparatus for in-situ online cyclone activity recovery of catalyst in a fluidized bed hydrogenation reactor. This method discloses a fluidized bed hydrogenation reactor shell and a catalyst cyclone activity recovery device built into the top of the reactor. The catalyst cyclone activity recovery device consists of a column section, a conical section connected to the column section, a cyclone guide ring placed within the column section, a catalyst return pipe connected to the conical section, a check cone connected to the catalyst return pipe, a liquid overflow pipe placed within and extending out of the column section, and a liquid outlet pipe connected to the column section. The upper end of the liquid overflow pipe is higher than the liquid level in the fluidized bed hydrogenation reactor. Therefore, this prior art document discloses adding a cyclone separator within the hydrogenation reactor to achieve solid catalyst return reaction, thereby improving catalyst utilization, reaction efficiency, and the quality of reaction products.

[0005] However, existing gas-liquid reaction devices still have the following drawbacks: the liquid product is discharged directly through the top of the cyclone separator, resulting in insufficient reaction of the raw material liquid, leading to a low product yield and unsatisfactory product quality; at the same time, the direct discharge from the top of the cyclone separator as a product causes the gas involved in the gas-liquid reaction to be carried out without free escape, resulting in a large gas demand and high cost.

[0006] In view of the above-mentioned technical deficiencies, based on the project research on improving catalyst utilization efficiency by solid catalyst catalysis of gas-liquid reaction in continuous flow reaction system, our research team studied gas-liquid reaction device and constructed a research and development concept system of horizontal S-shaped flow channel, horizontal swirling flow channel, tower swirling separation and vertical stirring suspension filtration. Taking into account the gas-liquid reaction principle and continuous production, we have provided a new device for the gas-liquid reaction process. Utility Model Content

[0007] Based on the above-mentioned technical problems, the present invention provides a solid catalyst catalytic gas-liquid reaction device with cyclone separation, which can cyclone separate particulate matter (catalyst particles) suspended in the liquid within the reaction body and return them to the bottom of the reaction body to contact the raw material liquid and the gas to be reacted, thereby promoting a more thorough gas-liquid reaction and improving catalyst utilization. Furthermore, it can also circulate the liquid raised from the bottom of the reaction body after cyclone separation back to the bottom of the reaction body to continue participating in the reaction, thereby improving the thoroughness of the reaction of the raw material liquid and helping to improve the quality of the reaction products.

[0008] The specific technical solution is as follows:

[0009] A solid catalyst catalytic gas-liquid reaction device with cyclone separation includes a reaction body, within which a cyclone separator is installed, forming a reaction zone, a sedimentation separation zone, and an escape buffer zone from bottom to top. The cyclone separator has a cyclone slurry inlet, a cyclone liquid inlet, and a solid outlet. The bottom of the reaction body has a raw material inlet, a gas inlet, and a cyclone liquid inlet. The sidewall of the reaction body has a slurry outlet, a slurry inlet, a cyclone liquid outlet, and a product outlet from bottom to top, with the slurry outlet located in the sedimentation separation zone and the product outlet located in the escape buffer zone. The cyclone liquid outlet is connected to the cyclone liquid inlet, and a second pump is installed between the cyclone liquid outlet and the cyclone liquid inlet. The slurry outlet is connected to the slurry inlet, and a first pump is installed between the slurry outlet and the slurry inlet. The slurry inlet is connected to the cyclone slurry inlet, and the cyclone liquid outlet is connected to the cyclone liquid inlet. An exhaust port is provided at the top of the escape buffer zone.

[0010] By incorporating a cyclone separator within the reactor body, the reactor body is divided into a reaction zone, a sedimentation separation zone, and a gas escape buffer zone from bottom to top. Combined with raw material inlets, gas inlets, and cyclone liquid inlets at the bottom of the reactor body, the material and solid catalyst in the reaction zone are suspended upwards upon inflow. As the feed rate gradually increases, the reaction products and solid catalyst enter the sedimentation separation zone. The free settling of particles in the slurry and the cyclone separation by the separator cause the solids and particles discharged from the solid outlet to settle and return to the reaction zone to participate in the reaction. Furthermore, the cyclone liquid from the separator is recycled back into the reaction zone for further reaction. Simultaneously, the product outlet gradually discharges the products, contributing to a more thorough reaction of the raw material liquid and improving the quality of the reaction products.

[0011] To improve the efficiency of gas utilization and facilitate the recirculation of escaped gas into the reaction zone, a circulating gas inlet is preferably provided at the bottom of the reaction body, the exhaust port is connected to the circulating gas inlet, and a third pump is provided between the exhaust port and the circulating gas inlet.

[0012] To ensure that the gas enters the bottom of the reactor and forms a large number of microbubbles within the reaction liquid, preferably, the gas inlet is located at the inner end of the reactor body and has a distribution head with several micropores. The distribution head is designed with reference to the structure of a bathroom heater.

[0013] To simplify the bottom structure of the reactor, a three-way pipe is used instead, thereby reducing the cost of equipment modification. Preferably, the circulating gas inlet is connected to the gas inlet. More preferably, the swirling liquid inlet is connected to the raw material inlet.

[0014] To facilitate cleaning of the reaction body during shutdown, it is preferable that a cleaning port is provided at the bottom of the reaction body.

[0015] To enhance the installation stability of the cyclone separator within the reactor body and to enable the reactor body to be divided into a reaction zone, a sedimentation separation zone, and an escape buffer zone from bottom to top via the cyclone separator, preferably, the reactor body is provided with several fixing rods, and the fixing rods support and fix the cyclone separator in the middle of the reactor body.

[0016] To regulate the temperature within the reactor body, preferably, a plurality of heat exchange plates are arranged radially within the reactor body. These heat exchange plates are hollow inside, and adjacent heat exchange plates are connected outside the reactor body via a connecting pipe. Preferably, the connecting pipe has a medium inlet and a medium outlet to facilitate the delivery of heat exchange medium into the heat exchange plates, thereby achieving the purpose of regulating the temperature within the reactor body.

[0017] To improve the heat exchange regulation effect, preferably, the reactant has a double-layer structure consisting of an outer wall and an inner wall, and a medium cavity is formed between the inner wall and the outer wall; a plurality of heat exchange plates are arranged radially inside the inner wall, the heat exchange plates are hollow inside and communicate with the medium cavity; a medium inlet and a medium outlet are provided on the outer wall, and the medium inlet and the medium outlet are connected through the medium cavity.

[0018] To improve heat exchange regulation, preferably, the heat exchange plate is provided with a partition plate that divides the heat exchange plate into a left flow cavity and a right flow cavity; a medium inlet / outlet mounting position is provided on the outer wall; a heat exchange plate with the left and right flow cavities separated by the partition plate is installed at the position corresponding to the medium inlet / outlet mounting position on the inner wall; the partition plate extends and is fixedly installed on the inner side of the outer wall, and a medium inlet and a medium outlet are provided at the medium inlet / outlet mounting position, with the medium inlet located on the left side of the partition plate and the medium outlet located on the right side of the partition plate; a heat exchange plate connecting the left and right flow cavities is installed at the position on the inner wall away from the position corresponding to the medium inlet / outlet mounting position.

[0019] To improve the heat exchange regulation effect, preferably, the heat exchange plate is provided with a partition plate, which divides the heat exchange plate into a left flow cavity and a right flow cavity, and the left flow cavity and the right flow cavity are connected at the ends away from the inner wall; the partition plate extends and is fixedly installed on the inner side of the outer wall, and a sealing block is provided in the medium cavity; the sealing block has a medium inlet on the left side and a medium outlet on the right side.

[0020] Compared with the prior art, the technical effects of this invention are reflected in:

[0021] This invention features a simple structure and is relatively easy to modify into existing tower-type gas-liquid reactors for industrial application, resulting in low cost and ease of implementation. Furthermore, by incorporating a cyclone separator within the reactor body, the reactor is sequentially divided into a reaction zone, a settling separation zone, and a gas escape buffer zone from bottom to top. After the material is fed into the reactor body from the bottom and reacts with the gas in the reaction zone, the liquid is continuously transported upwards and forced into the settling separation zone. Here, solids within the liquid undergo free settling and, combined with the slurry outlet and inlet, enter the cyclone separator for cyclone separation. This allows the slurry entering the settling separation zone to be separated and recycled back into the reaction zone for further gas reaction, improving the thoroughness of the liquid reaction. Additionally, the solids within the reactor body fall back into the reaction zone to participate in the reaction, improving the reaction effect and contributing to higher product quality.

[0022] This invention is applicable to catalytic hydrogenation reaction systems. It facilitates the reuse of catalysts in the sedimentation separation zone and liquid sedimentation separation zone, improving the utilization efficiency of catalysts (such as palladium-on-carbon catalysts with a particle size of about 1 mm). Furthermore, by using a cyclone separator, liquids with poor reaction incompleteness are recycled into the reaction zone to re-react with hydrogen, improving product quality. At the same time, the gas escape buffer promotes the escape of gas, which is discharged from the top, while the product is discharged from the side wall near the top of the reactant, which helps to return hydrogen to the reaction zone for reuse and reduces hydrogen consumption costs.

[0023] In addition, the device created by this invention can also be applied to other catalytic gas-liquid reaction systems, such as reaction systems that use iron-carbon catalysts to catalytically treat exhaust gas to reduce the organic content in the exhaust gas, and reaction systems that use liquids to absorb harmful components in the exhaust gas.

[0024] The present invention incorporates structures such as heat exchange plates within the reaction body, which helps to regulate the temperature within the reaction body and meet the temperature requirements of the reaction body.

[0025] This invention utilizes a specific structure for the gas inlet and the raw material liquid inlet, which allows reactants to form gas-liquid mixed micro- and nano-bubbles after entering the reaction body. Under the action of these micro- and nano-bubbles, the suspension reaction effect in the reaction zone is enhanced. Combined with the structural design of the sedimentation and separation zone, this will help improve the quality and grade of the reaction products. Attached Figure Description

[0026] To facilitate a thorough understanding of the technical solution of this invention by those skilled in the art, the following description is provided in conjunction with the technical solution and the accompanying drawings. The directional terms used in this invention, such as "up," "down," "front," "back," "left," and "right," are merely illustrative descriptions in conjunction with the accompanying drawings and are not intended to limit the technical solution of this invention.

[0027] Figure 1 A schematic diagram of the overall structure of this invention is provided.

[0028] Figure 2 for Figure 1 Schematic diagram of the cross-sectional structure of the reaction body.

[0029] Figure 3 This is a schematic diagram of the top view of the structure along the 2A-A direction in the figure.

[0030] Figure 4 for Figure 3 Another embodiment of the structural diagram.

[0031] Figure 5 for Figure 4 Enlarged structural diagram of Part I.

[0032] Figure 6 for Figure 4 Partial cross-sectional view of the heat exchanger plate structure in Section I.

[0033] Figure 7 for Figure 4 Part II: Partial sectional view of the heat exchanger plate structure.

[0034] Figure 8 for Figure 3 Another embodiment of the structural diagram.

[0035] Figure 9 for Figure 1 Another embodiment of the structural diagram.

[0036] Figure 10 for Figure 9 Schematic diagram of cross-section structure.

[0037] 1-Reaction body 2-Exhaust port 3-Product outlet 4-Swirl liquid outlet 5-Pulp inlet 6-Pulp outlet 7-First pump 8-Second pump 9-Swirl liquid inlet 10-Cleaning port 11-Circulating gas inlet 12-Raw material inlet 13-Gas inlet 14-Third pump 15-Swirl slurry port 16-Swirl liquid port 17-Swirl separator 18-Heat exchange plate 19-Fixing rod 20-Solid outlet 21-Outer wall 22-Inner wall 23-Media cavity 24-Sealing block 25-Media inlet 26-Media outlet 27-Reaction bottom 28-Separator plate Detailed Implementation

[0038] To facilitate a correct understanding of the present invention by those skilled in the art, and to enable them to fully understand the technical content of the present invention, the technical solution of the present invention will be further described below in conjunction with specific embodiments and accompanying drawings. However, this description does not limit the scope of protection claimed by the present invention. Those skilled in the art should not limit the scope of protection of the present invention to the following description. Any equivalent substitutions or changes made by those skilled in the art or those familiar with the art based on the present invention, and based on the technical solution and inventive concept of the present invention, should be covered within the scope of protection of the present invention.

[0039] like Figure 1 and Figure 2As shown, in some embodiments, a solid catalyst catalytic gas-liquid reaction device with cyclone separation includes a reaction body 1, within which a cyclone separator 17 is provided, forming a reaction zone, a sedimentation separation zone, and an escape buffer zone from bottom to top; the cyclone separator 17 is provided with a cyclone slurry inlet 15, a cyclone liquid inlet 16, and a solid outlet 20; the bottom of the reaction body 1 is provided with a raw material inlet 12, a gas inlet 13, and a cyclone liquid inlet 9; the sidewall of the reaction body 1 is provided with a slurry outlet 6, a slurry outlet 7, a slurry outlet 8, a slurry outlet 9, and a solid outlet 10 from bottom to top. The system includes an inlet 5, a cyclone outlet 4, and a product outlet 3, with the slurry outlet 6 located in the sedimentation separation zone and the product outlet 3 located in the escaping buffer zone. The cyclone outlet 4 is connected to the cyclone inlet 9, and a second pump 8 is provided between the cyclone outlet 4 and the cyclone inlet 9. The slurry outlet 6 is connected to the slurry inlet 5, and a first pump 7 is provided between the slurry outlet 6 and the slurry inlet 5. The slurry inlet 5 is connected to the cyclone slurry outlet 15, and the cyclone outlet 4 is connected to the cyclone outlet 16. An exhaust port 2 is provided at the top of the escaping buffer zone.

[0040] In operation, the gas to be reacted is introduced into the reaction body 1 through gas inlet 13, while the raw material liquid to be reacted (for reactions requiring a catalyst, the catalyst is added directly to the raw material liquid here) is pumped into the reaction body 1 through raw material inlet 12. This causes the gas and raw material liquid to come into contact at the bottom (reaction bottom 27) of the reaction body 1, forming several bubbles. As the raw material liquid is pumped in, the number of bubbles increases. Simultaneously, as more raw material liquid is added, the liquid in the reaction body 1 continuously rises until it is level with the product outlet 3 near the top of the reaction body 1. At this point, the product outlet 3 is opened, allowing the product flowing out of the product outlet 3 to be released. The liquid volume is equal to the total liquid flowing into the bottom of reaction body 1, which in turn promotes the reaction-sedimentation separation-gas release process in reaction body 1 from bottom to top. At the same time, a hydrocyclone separator is installed in the sedimentation separation area. The slurry is drawn from the middle of reaction body 1 and enters the hydrocyclone separator for hydrocyclone separation. This allows the raw material liquid that has not participated in the reaction or the raw material liquid containing insufficient product concentration to return to the bottom of reaction body 1 to re-participate in the reaction after hydrocyclone separation. In addition, the added solid catalyst is directly separated and enters the bottom of reaction body 1 from the solid outlet on the hydrocyclone separator to continue participating in the reaction. This helps to improve the utilization rate of catalyst and other particulate matter and improve the quality of the product.

[0041] This invention involves designing the reaction body 1 with a diameter of 1.2m and controlling the swirling circulation volume from the slurry outlet 6 to be 1.2 times the amount of raw material liquid introduced into the raw material inlet 12. The liquid flowing out of the swirling liquid outlet 4 is then returned to the reaction body 1 for recycling. Product samples are taken from the product outlet 3 for analysis. Compared with direct sampling and analysis from the swirling liquid outlet 4, the product purity is about 10 percentage points higher, which greatly improves the gas-liquid reaction efficiency.

[0042] Because a cyclone separator 17 is provided in the reaction body 1, the cyclone liquid can flow from the cyclone liquid outlet 4 into the cyclone liquid inlet 9 even without the second pump 8. However, in order to enhance the intensity of liquid pumping, a preferred embodiment is to use a second pump 8 to enhance the pumping pressure of the cyclone liquid into the reaction body 1, thereby improving the effect of forming a suspension reaction at the bottom of the reaction body 1.

[0043] In some embodiments, a filter plate (not shown) is provided between the cyclone outlet 4 and the product outlet 3. The filter plate divides the reactant 1 into a lower reaction settling zone and an upper escaping buffer zone. This prevents the solid catalyst added to the feed liquid from being discharged along with the product discharged from the product outlet 3, thereby improving catalyst utilization. In this embodiment, the filter plate can be a plate-like structure of a nanofiltration membrane module or a microporous membrane module.

[0044] like Figure 1 and Figure 2 As shown, in some embodiments, the bottom of the reactor 1 is provided with a circulating gas inlet 11, the exhaust port 2 is connected to the circulating gas inlet 11, and a third pump 14 (compressor) is provided between the exhaust port 2 and the circulating gas inlet 11. This enables the gas escaping from the top to be recycled back into the reactor 1, improving gas utilization.

[0045] In some embodiments, the gas inlet is located at the inner end of the reactor body and has a distribution head with several micropores. For example, referring to the design of a bathroom heater, a gas inlet 13 is used instead of the water inlet pipe of the bathroom heater. Several micropores are provided on the bathroom heater head, so that the gas in the gas inlet 13 enters the distribution head and is distributed in the reactor body 1 through the micropores on the distribution head. This allows the gas to fully contact the liquid material in the reactor body, and the distribution of the micropores enables the formation of a large number of bubbles, so that microbubbles continuously rise from the bottom of the reactor body 1. This structural design helps to improve the efficiency and effect of the gas-liquid contact reaction.

[0046] like Figure 9 and Figure 10 As shown, in some embodiments, the circulating gas inlet 11 is connected to the gas inlet 13. For example, a three-way pipe is installed on the gas inlet 13, with one end installed on the reaction bottom 27 of the reaction body 1 to allow gas to be blown into the reaction body 1, and the other end connected to the external storage tank of the gas to be reacted. The remaining end is used as the circulating gas inlet 11 to connect to the exhaust port 2. This simplifies the improvement of the bottom of the reaction body 1 during industrialization and promotion, and reduces the difficulty of improvement.

[0047] like Figure 9 and Figure 10As shown, in some embodiments, the cyclone inlet 9 is connected to the raw material inlet 12. For example, a three-way pipe is installed on the raw material inlet 12, with one end installed on the reaction bottom 27 of the reaction body 1 to pump the raw material liquid to be reacted into the reaction body 1, and the other end connected to the external storage tank of the raw material liquid to be reacted. The remaining end is used as the cyclone inlet 9 to connect to the cyclone outlet 4. This simplifies the improvement of the bottom of the reaction body 1 during industrialization and reduces the difficulty of improvement.

[0048] like Figure 1 , Figure 2 , Figure 9 and Figure 10 As shown, in some embodiments, a cleaning port 10 is provided at the bottom of the reaction body 1. This facilitates the discharge of cleaning slurry during cleaning of the reaction body 1, or the raw material inlet 12 can be used directly instead.

[0049] like Figure 2 and Figure 10 As shown, in some embodiments, the reaction body 1 is provided with a plurality of fixing rods 19, and the fixing rods 19 support and fix the cyclone separator 17 in the middle of the reaction body 1. This helps to enhance the stability of the installation of the cyclone separator 17 and makes it easier to install the cyclone separator 17 in the middle position of the reaction body 1.

[0050] like Figure 2-8 and Figure 10 As shown, in some embodiments, a plurality of heat exchange plates 18 are radially arranged inside the reaction body 1. The heat exchange plates 18 are hollow inside, and adjacent heat exchange plates 18 are connected to each other outside the reaction body 1 via a connecting pipe. The heat exchange plates 18 can be used to regulate the temperature inside the reaction body 1 to meet its temperature requirements. For example, when it is necessary to increase the temperature inside the reaction body 1, a heat exchange medium can be filled into the heat exchange plates 18 to provide heat to the reaction body 1; when it is necessary to decrease the temperature inside the reaction body 1, a cooler heat exchange medium can be filled into the heat exchange plates 18 to remove heat from the reaction body 1 and lower the temperature. In some embodiments, preferably, the connecting pipe has a medium inlet and a medium outlet to facilitate the delivery of the heat exchange medium into the heat exchange plates, thereby achieving the purpose of regulating the temperature inside the reaction body.

[0051] In some embodiments, a combined heating and cooling unit is installed outside the device to regulate the temperature of the heat exchange medium entering the heat exchange plate 18. In some operating schemes, based on common knowledge and conventional technical means, several temperature monitoring points (temperature sensors) can be installed inside the reaction body 1 to monitor the temperature inside the reaction body 1, and the temperature inside the reaction body 1 can be accurately adjusted and controlled by combining the monitored temperature with the heat exchange plate 18.

[0052] like Figure 3As shown, in some embodiments, the reactant 1 has a double-layer structure consisting of an outer wall 21 and an inner wall 22, and a medium cavity 23 is formed between the inner wall 22 and the outer wall 21; a plurality of heat exchange plates 18 are arranged radially inside the inner wall 22, the heat exchange plates 18 are hollow inside and communicate with the medium cavity 23; a medium inlet 25 and a medium outlet 26 are provided on the outer wall 21, and the medium inlet 25 and the medium outlet 26 are connected through the medium cavity 23. In operation, the heat exchange medium is pumped in through the medium inlet 25, entering the medium chamber 23 and distributing to the heat exchange plate 18. This allows the temperature inside the reaction body 1 to exchange with the heat exchange medium. Once the temperature inside the medium chamber 23 matches the temperature inside the reaction body 1, the medium inlet 25 is closed, and the medium outlet 26 is opened to discharge the heat exchange medium from the medium chamber 23. After discharge, the medium outlet 26 is closed again, and the medium inlet 25 is opened. This cycle is repeated to achieve heat exchange within the reaction body 1 and regulate its temperature. In some operating schemes, based on common knowledge and conventional techniques, temperature sensors are installed in both the medium chamber 23 and the reaction body 1.

[0053] like Figure 4 , Figure 5 , Figure 6 and Figure 7 As shown, in some embodiments, the heat exchange plate 18 is provided with a partition plate 28, which divides the heat exchange plate 18 into a left flow chamber and a right flow chamber (e.g., Figure 6 and Figure 7 As shown); the outer wall 21 is provided with a medium inlet / outlet mounting position; a heat exchange plate 18 (as shown) is installed at the position corresponding to the inner wall 22, where the left flow cavity and the right flow cavity are separated by a partition plate 28. Figure 4 , Figure 5 and Figure 6 (As shown); the separator 28 extends and is fixedly installed on the inner side of the outer wall 21 (as shown). Figure 4 and Figure 5 As shown), a media inlet 25 and a media outlet 26 are provided at the media inlet / outlet installation position, with the media inlet 25 located to the left of the separator 28 and the media outlet 26 located to the right of the separator 28 (as shown). Figure 4 and Figure 5 As shown); a heat exchange plate 18 connecting the left and right flow chambers is installed on the inner wall 22 at a position away from the medium inlet / outlet mounting position (e.g. Figure 4 and Figure 7 (As shown). This allows the heat exchange medium to enter the medium cavity 23 through the medium inlet 25, and then enter the heat exchange plate 18 (as shown) which connects the left and right flow cavities. Figure 7 As shown, the medium passes through the medium cavity 23 and is finally discharged from the medium outlet 26, thus achieving the purpose of heat exchange and regulating the temperature inside the reaction body 1.

[0054] like Figure 7 and Figure 8 As shown, in some embodiments, the heat exchange plate 18 is provided with a partition 28, which divides the heat exchange plate 18 into a left flow cavity and a right flow cavity, and the left flow cavity and the right flow cavity are connected at the end away from the inner wall 22 (e.g. Figure 7 (As shown); the separator 28 extends and is fixedly installed on the inner side of the outer wall 21, and a sealing block 24 is provided in the medium cavity 23 (as shown). Figure 8 (As shown in the figure). The sealing block 24 has a medium inlet 25 on the left side and a medium outlet 26 on the right side. This allows the heat exchange medium to enter the medium cavity 23 through the medium inlet 25, then enter the heat exchange plate 18, and then re-enter the medium cavity 23 through the left and right flow chambers of the heat exchange plate 18. Finally, after flowing into the medium cavity 23 through the heat exchange plate 18, it is discharged through the medium outlet 26, thus achieving the purpose of heat exchange and regulating the temperature inside the reaction body 1.

[0055] In some embodiments, the heat exchange plate 18 is provided with heat exchange fins (not shown in the figure), which helps to improve the heat exchange effect.

[0056] Compared to the technical content disclosed in the prior art (e.g., 201910342691.6), the greatest inventive advantage of this invention lies in the following: Both the gas to be reacted and the raw material liquid to be reacted are fed from the reaction bottom 27 of the reaction body 1. The compression pressure of the compressor during the gas injection process and the pump pressure of the raw material liquid injection promote the formation of a gas-liquid boiling suspension state at the bottom of the reaction body 1, improving the efficiency and effect of the gas-liquid contact catalytic reaction. Furthermore, the use of a cyclone separator and the structural design of connecting the slurry outlet and slurry inlet to the cyclone separator enables continuous... The slurry containing catalyst particles formed at the bottom of the chemical treatment reactor 1 is circulated, causing the catalyst to fall from the bottom of the hydrocyclone separator 17 to the bottom of the reactor 1, where it comes into contact with the raw material liquid and gas and acts. This allows the solid particle catalyst to fall freely from top to bottom into the raw material liquid, so that the catalyst acts on the bubbles formed by the gas-liquid contact during the falling process, improving the gas-liquid reaction efficiency and effect. At the same time, under the action of the slurry outlet, slurry inlet and the first pump, the liquid is continuously drawn upward, which improves the upward flow efficiency of the liquid, enhances the suspension effect, and improves the thoroughness of the gas-liquid reaction.

[0057] In some embodiments, the reaction base 27 is replaced by a microchannel mixer installed inside the reaction body 1. The microchannel mixer is designed according to existing technology, for example, referring to the microchannel mixer described in the fixed-bed reactor device for continuous preparation of polyetheramines in patent application number 201720959666.9. The microchannel mixer includes multiple sets of microchannel components, each set consisting of multiple microchannels connected in series. One end of the multiple sets of microchannel components connected in parallel is connected to a tee connector and leads out from the bottom of the reaction body 1. One end of the tee connector is connected to the gas inlet 13, and the other end is connected to the feed liquid inlet 12. When a third pump 14 (gas compressor) is set to circulate the gas discharged from the exhaust port 2 into the reaction body, one end of the tee connector is connected to the feed liquid inlet 12, the other end of the tee connector is connected to a new tee connector, and then one end of the new tee connector is connected to the gas inlet 13, and the other end of the new tee connector is connected to the circulating gas inlet 11. The other end of multiple sets of microchannel components connected in parallel is connected to a pipe extending into the reaction body 1. A distributor head is installed at the top of this pipe, and the bottom of the distributor head is in close contact with the upper surface of the microchannel mixer. This effectively avoids the defect of solid catalyst particles settling and accumulating at the bottom, unable to be suspended by the pumped gas-liquid mixture. The distributor head has several micropores. For example, referencing the design of a bathroom heater / ventilation unit.

[0058] In some embodiments of the present invention, a wire mesh demister (not shown in the figure) is provided between the product outlet 3 and the top of the reaction body 1, so that the gas escapes and is discharged directly from the exhaust port 2.

[0059] For any other matters not covered in this invention, conventional technical means can be used by referring to existing technologies (e.g., 201910342691.6) or common knowledge known to those skilled in the art. For example, this invention can be used in hydrogenation reactions during organic chemical reactions, that is, as a hydrogenation reaction device to achieve continuous hydrogenation reactions; it can also be used in tail gas treatment devices that use liquid absorption to achieve cyclic and continuous tail gas treatment. For corresponding structural components not shown in the accompanying drawings, those skilled in the art can adjust and set them as needed, which are conventional technical adjustments. For example, multiple temperature sensor points can be arranged in the reaction body 1 to monitor the temperature inside the reaction body 1, and then the temperature inside the reaction body 1 can be adjusted using the heat exchange plate 3. Another example is to add a catalyst addition port at the top of the reaction body 1 or directly add the catalyst to the reaction liquid through the feed pipe as needed.

Claims

1. A solid catalyst catalytic gas-liquid reaction device with cyclone separation, characterized in that, The reaction body (1) includes a cyclone separator (17) which forms a reaction zone, a sedimentation separation zone, and an escape buffer zone from bottom to top. The cyclone separator (17) is provided with a cyclone slurry inlet (15), a cyclone liquid inlet (16), and a solid outlet (20). The bottom of the reaction body (1) is provided with a raw material inlet (12), a gas inlet (13), and a cyclone liquid inlet (9). The sidewall of the reaction body (1) is provided with a slurry outlet (6), a slurry inlet (5), a cyclone liquid outlet (4), and a product outlet (3) from bottom to top. The slurry outlet (6) is located in the sedimentation separation zone, and the product outlet (3) is located in the gas escape buffer zone; the cyclone liquid outlet (4) is connected to the cyclone liquid inlet (9), and a second pump (8) is provided between the cyclone liquid outlet (4) and the cyclone liquid inlet (9); the slurry outlet (6) is connected to the slurry inlet (5), and a first pump (7) is provided between the slurry outlet (6) and the slurry inlet (5); the slurry inlet (5) is connected to the cyclone slurry port (15), and the cyclone liquid outlet (4) is connected to the cyclone liquid port (16); the top of the gas escape buffer zone is provided with an exhaust port (2).

2. The solid catalyst catalytic gas-liquid reaction device with cyclone separation as described in claim 1, characterized in that, The bottom of the reaction body (1) is provided with a circulating gas inlet (11), the exhaust port (2) is connected to the circulating gas inlet (11), and a third pump (14) is provided between the exhaust port (2) and the circulating gas inlet (11). And / or the gas inlet (13) is provided with a distribution head at the inner end of the reactant (1), and the distribution head is provided with a plurality of micropores.

3. The solid catalyst catalytic gas-liquid reaction device with cyclone separation as described in claim 2, characterized in that, The circulating gas inlet (11) is connected to the gas inlet (13).

4. The solid catalyst catalytic gas-liquid reaction device with cyclone separation as described in claim 1, characterized in that, The swirling liquid inlet (9) is connected to the raw material inlet (12).

5. The solid catalyst catalytic gas-liquid reaction device with cyclone separation as described in claim 1, characterized in that, The bottom of the reaction body (1) is provided with a cleaning port (10).

6. The solid catalyst catalytic gas-liquid reaction device with cyclone separation as described in claim 1, characterized in that, The reaction body (1) is provided with several fixing rods (19), and the fixing rods (19) support and fix the cyclone separator (17) in the middle of the reaction body (1).

7. The solid catalyst catalytic gas-liquid reaction apparatus with cyclone separation as described in claim 1, 2, 5, or 6, characterized in that, The reaction body (1) is provided with a plurality of heat exchange plates (18) along the radial direction. The heat exchange plates (18) are hollow inside, and adjacent heat exchange plates (18) are connected outside the reaction body (1).

8. The solid catalyst catalytic gas-liquid reaction apparatus with cyclone separation as described in claim 1, 2, 5, or 6, characterized in that, The reactant (1) has a double-layer structure consisting of an outer wall (21) and an inner wall (22), and a medium cavity (23) is formed between the inner wall (22) and the outer wall (21); a plurality of heat exchange plates (18) are arranged radially inside the inner wall (22), the heat exchange plates (18) are hollow inside and communicate with the medium cavity (23); a medium inlet (25) and a medium outlet (26) are provided on the outer wall (21), and the medium inlet (25) and the medium outlet (26) are connected through the medium cavity (23).

9. The solid catalyst catalytic gas-liquid reaction device with cyclone separation as described in claim 8, characterized in that, The heat exchange plate (18) is provided with a partition plate (28), which divides the heat exchange plate (18) into a left flow cavity and a right flow cavity; the outer wall (21) is provided with a medium inlet / outlet mounting position; the heat exchange plate (18) with the left flow cavity and the right flow cavity separated by the partition plate (28) is installed at the position of the medium inlet / outlet mounting position corresponding to the inner wall (22); the partition plate (28) extends and is fixedly installed on the inner side of the outer wall (21), and a medium inlet (25) and a medium outlet (26) are provided at the medium inlet / outlet mounting position, with the medium inlet (25) located on the left side of the partition plate (28) and the medium outlet (26) located on the right side of the partition plate (28); the heat exchange plate (18) connecting the left flow cavity and the right flow cavity is installed at the position of the inner wall (22) away from the position of the medium inlet / outlet mounting position.

10. The solid catalyst catalytic gas-liquid reaction device with cyclone separation as described in claim 8, characterized in that, The heat exchange plate (18) is provided with a partition plate (28), which divides the heat exchange plate (18) into a left flow chamber and a right flow chamber, and the left flow chamber and the right flow chamber are connected at the end away from the inner wall (22); the partition plate (28) extends and is fixedly installed on the inner side of the outer wall (21), and a sealing block (24) is provided in the medium chamber (23); the sealing block (24) has a medium inlet (25) on the left side and a medium outlet (26) on the right side.

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