Solid catalyst configuration and reactive distillation column using the same

Abstract

The application discloses a solid catalyst configuration and a reactive rectifying tower using the solid catalyst, the solid catalyst is granular and in a turbine type as a whole, and comprises a columnar part, a fin part and a columnar part and a fin part are in an integral structure and extend tangentially along the outer wall surface of the columnar part, the fin surface is provided with a catalyst active component, and the fin interior is a catalyst carrier. The reactive rectifying tower of the application can make the catalyst particles do reciprocating fluidization motion through the combined action of the lifting force of the gas phase and the self-gravity of the turbine type solid catalyst particles and the liquid drop drag force in the gas-liquid mass transfer space, and the gas and liquid form a flow state of coexisting countercurrent and cross flow, so that the efficient gas-liquid mass transfer reaction can be completed.

Description

Technical Field

[0001] This invention relates to the field of petrochemical gas-liquid mass transfer technology, and particularly to a solid catalyst configuration and a reactive distillation column using the solid catalyst. Background Technology

[0002] A reactive distillation column is a gas-liquid mass transfer device that combines reaction and distillation processes. Reactive distillation technology has wide applications in etherification, esterification, and alkylation reactions. Compared to traditional processes where reactors and distillation columns are used independently, reactive distillation columns can significantly reduce operating and investment costs. They can be plate columns or packed columns. Plate columns are widely used due to their simple structure and adaptability.

[0003] In reactive distillation, gas-liquid mass transfer efficiency is crucial. Gas-liquid reactions generally require the participation of solid catalysts, but for gas-liquid-solid three-phase reactive distillation, achieving uniform mixing and efficient mass transfer between the three phases between the trays is a technical challenge in this field. To ensure good contact and reaction space between the gas, liquid, and solid phases, the arrangement of the catalyst and the structure of the internal components of the column need to be rationally designed and optimized.

[0004] In existing plate reactive distillation columns, solid catalysts are generally placed in the liquid layer on the tray in a bulk or packaged manner, that is, the solid catalyst is immersed in the liquid phase. Under this arrangement, the mass transfer efficiency of the gas-liquid-solid three-phase contact reaction is low, and multiple layers of trays and catalysts are often required to achieve the ideal reaction and mass transfer separation effect.

[0005] Chinese patent application CN108261792A discloses a novel pneumatically driven stirred catalytic distillation device, primarily addressing the problem of uneven three-phase mixing of gas, liquid, and solid phases between trays in existing catalytic distillation columns. Each tray employs a separate side-mounted pneumatic stirrer, with the stirrer suspended from the top of the tray. Each tray is equipped with a riser and a downcomer. The riser inlet is located on the opposite side of the pneumatic pump mounting side of each tray, and a gas distributor is connected to the upper part of the riser. Gas from the lower tray is evenly sprayed into the liquid-solid mixture on the tray through the gas distributor. A filter screen is installed at the upper part of the downcomer to prevent particulate or micro-particle catalyst from falling into the lower tray. The downcomer inlet is located at the bottom of the tray, extending below the liquid surface of the adjacent lower tray. This technical solution effectively solves the aforementioned problems and can be used in catalytic distillation. However, this existing technology only uses a stirring device in the liquid phase, and the stirring power comes from an external source, resulting in high energy consumption and increased investment and operating costs.

[0006] Therefore, there is an urgent need for a reactive distillation column that can effectively improve the gas-liquid-solid three-phase contact mass transfer efficiency. By applying a special configuration of the catalyst in the reactive distillation column, the adverse effects of the solid catalyst being submerged in the liquid phase are avoided. This not only effectively improves the gas-liquid mass transfer efficiency, but also effectively reduces equipment investment and operating costs.

[0007] The information disclosed in this background section is intended only to enhance the understanding of the overall background of the invention and should not be construed as an admission or in any way implying that the information constitutes prior art known to those skilled in the art. Summary of the Invention

[0008] The purpose of this invention is to provide a solid catalyst configuration that allows for gas-liquid-solid mass transfer reactions to be completed without being immersed in a liquid phase during catalyst use.

[0009] Another objective of this invention is to provide a reactive distillation column using this solid catalyst configuration, in which the catalyst particles undergo reciprocating fluidized motion in the gas-liquid mass transfer space due to the combined action of the lift of the gas phase and the gravity of the turbine-type solid catalyst particles and the drag force of the droplets. At the same time, the gas and liquid form a flow state with both countercurrent and cross-current, thereby completing a highly efficient gas-liquid mass transfer reaction.

[0010] To achieve the above objectives, according to a first aspect of the present invention, the present invention provides a solid catalyst configuration, the solid catalyst being particulate and generally turbine-shaped, comprising: a columnar portion having a columnar structure with catalyst active components disposed on both end faces of the column, and a catalyst support inside the column; and a finned portion having an integral structure with the columnar portion and extending tangentially along the outer wall of the column, with catalyst active components disposed on the surface of the fins, and a catalyst support inside the fins.

[0011] Furthermore, in the above technical solution, the fins can be evenly spaced along the circumference of the column to form an integral turbine structure, and the extension direction of the fins can be counterclockwise.

[0012] Furthermore, in the above technical solution, the catalyst particles undergo a reciprocating fluidized motion in the gas-liquid mass transfer space due to the combined effects of the lift force of the gas phase, the gravity of the catalyst particles themselves, and the downward drag force of the droplets. At the same time, the rising gas phase and the falling droplets form a flow state in which countercurrent and cross-flow coexist.

[0013] According to a second aspect of the present invention, a reactive distillation column is provided, which utilizes the solid catalyst configuration of any one of the foregoing claims to complete the gas-liquid-solid mass transfer reaction of each tray, comprising: a gas rising unit fixed on the lower tray and extending upward above the liquid layer for providing a jet-like rising gas phase; a liquid falling unit fixed on the upper tray for providing descending liquid droplets; and a gas-liquid mass transfer space disposed between the gas rising unit and the liquid falling unit and enclosed by a perforated double-layer catalyst filter plate for limiting the up-and-down reciprocating motion of the catalyst particles.

[0014] Furthermore, in the above technical solution, the double-layer catalyst filter plate includes an upper catalyst filter plate and a lower catalyst filter plate. The diameter of the perforated holes on the filter plate is smaller than the size of the catalyst particles, allowing the rising gas phase and the falling droplets to pass through.

[0015] Furthermore, in the above technical solution, when the distance between two adjacent layers of trays is H, the lower catalyst filter plate is arranged at a height of 0.25 to 0.45H above the tray; the upper catalyst filter plate is arranged at a height of 0.3 to 0.4H above the lower catalyst filter plate.

[0016] Furthermore, in the above technical solution, the gas riser unit can adopt a T-shaped gas distributor, which may include: a riser pipe, the bottom of which is fixed to the lower tray and used to receive the rising gas phase from the lower layer, the upper part of which extends above the liquid accumulation layer; and a branch pipe, which is arranged on the upper part of the riser pipe and extends in the horizontal direction, with upward-facing nozzles evenly distributed on the branch pipe.

[0017] Furthermore, in the above technical solution, there can be multiple branch pipes arranged radially outward along the riser pipe; the nozzle can be one of a fan-shaped nozzle, a rectangular nozzle, or an elliptical nozzle, with a fan-shaped nozzle being preferred.

[0018] Furthermore, in the above technical solution, when the distance between two adjacent trays is H, the branch pipe can be located at a position of 0.1 to 0.2H below the lower catalyst filter plate.

[0019] Furthermore, in the above technical solution, a filter screen for blocking catalyst residue can be provided at the lower end of the riser pipe.

[0020] Furthermore, in the above technical solution, the liquid downcomer can be a liquid distributor fixed on the upper tray, with nozzles arranged on the liquid distributor to provide uniformly sprayed liquid droplets downwards.

[0021] Furthermore, in the above technical solution, in the gas-liquid mass transfer space, the catalyst particles, in a non-liquid phase immersion state, form a coexistence of gas-liquid countercurrent and crosscurrent through reciprocating rotational motion, thereby completing and enhancing the gas-liquid-solid three-phase mass transfer reaction process.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] 1) This invention applies a special turbine-type solid catalyst particle configuration to a reactive distillation column. The catalyst particles do not enter the liquid layer. The active components of the catalyst are on the surface of the finned part and the two end faces of the columnar part of the catalyst particles. The interior of the finned part and the columnar part is the carrier. Therefore, the turbine-type catalyst particles not only have the same catalytic efficiency as existing catalysts, but the design of the finned part can also increase the overall specific surface area of ​​the particles.

[0024] 2) By setting up an upper and lower catalyst filter plate structure, the present invention can effectively prevent the solid catalyst from being carried to the reaction mass transfer space of other trays by rising gas or falling liquid, which is conducive to stabilizing the reaction mass transfer process on each tray and reducing the operation fluctuation of the tower system.

[0025] 3) This invention utilizes a relatively independent gas-liquid mass transfer space, allowing rising gas and falling droplets to convect and collide within this space. During this process, the rising gas and falling droplets encounter turbine-shaped solid catalyst particles, and under the guiding effect of the fins, a vortex phenomenon is formed. The gas and droplets form a flow state where countercurrent and cross-current coexist. Simultaneously, the turbine-shaped catalyst particles undergo reciprocating fluidized motion in the gas-liquid mass transfer space. The rising gas and falling droplets react upon contact with the surface of the solid catalyst particles, achieving a distillation separation process. Compared with the prior art, this invention can further enhance the gas-liquid-solid three-phase reaction and mass transfer process.

[0026] 4) By setting up a gas distributor and a liquid distributor, the gas rises uniformly and the liquid droplets fall uniformly, which increases the mass transfer contact area between the gas and liquid phases, thereby reducing the overall pressure drop of the tower and facilitating the mass transfer process.

[0027] 5) The present invention provides a filter screen at the lower end of the riser pipe to block catalyst residue, which can effectively prevent catalyst residue from penetrating the upper catalyst filter plate and being carried into the upper tower plate by the rising gas.

[0028] 6) This invention does not require stirring to promote gas-liquid mass transfer reactions, nor does it require additional external energy, which can significantly reduce the operating cost of the reactive distillation column of this invention. Experiments have shown that by using the solid catalyst configuration and reactive distillation column of this invention, the number of trays and the overall pressure drop of the column can be significantly reduced while achieving the same product yield.

[0029] The above description is merely an overview of the technical solution of the present invention. In order to better understand the technical means of the present invention and to implement it according to the contents of the specification, and to make the above and other objects, technical features and advantages of the present invention easier to understand, one or more preferred embodiments are listed below and described in detail with reference to the accompanying drawings. Attached Figure Description

[0030] Figure 1 This is a schematic diagram of the solid catalyst structure used in the reactive distillation column of this invention.

[0031] Figure 2 This is a schematic diagram of the internal structure of the reactive distillation column of the present invention.

[0032] Figure 3 This is a top view of the gas distributor inside the reactive distillation column of the present invention.

[0033] Explanation of key figure labels:

[0034] 1-Solid catalyst particles, 11-Columnar part, 12-Finned part, 2-Gas distributor, 21-Rising pipe, 22-Branch pipe, 23-Gas phase nozzle, 24-Filter screen, 3-Liquid phase nozzle, 4-Gas-liquid mass transfer space, 41-Upper catalyst filter plate, 42-Lower catalyst filter plate;

[0035] 100 - Reactive distillation column; 101 - Tray;

[0036] A - Liquid layer, A1 - Droplet. Detailed Implementation

[0037] The specific embodiments of the present invention will now be described in detail with reference to the accompanying drawings, but it should be understood that the scope of protection of the present invention is not limited to the specific embodiments.

[0038] Unless otherwise expressly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "comprises" shall be understood to include the stated elements or components without excluding other elements or other components.

[0039] In this document, for ease of description, spatial relative terms such as “below,” “under,” “down,” “above,” “above,” “upper,” etc., are used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that spatial relative terms are intended to encompass different orientations of an object in use or operation, in addition to those depicted in the figures. For example, if an object in the figure is flipped, an element described as “below” or “under” another element or feature would be oriented “above” that element or feature. Thus, the exemplary term “below” can encompass both the downward and upward orientations. An object may also have other orientations (rotated 90 degrees or other orientations), and the spatial relative terms used herein should be interpreted accordingly.

[0040] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.

[0041] Compared to existing technologies where solid catalyst particles are immersed in the liquid phase and gas bubbles into the liquid phase to complete the gas-liquid-solid mass transfer reaction, this invention applies a special solid catalyst particle configuration to a reactive distillation column. The catalyst particles do not enter the liquid layer. By setting up a relatively independent gas-liquid mass transfer space, the rising gas and the falling droplets can convect and collide in this space. At the same time, the rising gas drives the turbine-shaped catalyst particles to have an upward trend, while the gravity of the catalyst particles themselves and the drag force of the falling droplets cause the catalyst particles to have a downward trend. During this process, the turbine-shaped catalyst particles undergo reciprocating fluidized motion in the gas-liquid mass transfer space. The rising gas and the falling droplets react on the surface of the solid catalyst particles and realize the distillation separation process. Compared with existing technologies, this invention can further enhance the gas-liquid-solid three-phase reaction and mass transfer process.

[0042] Example 1

[0043] like Figure 1 As shown, this embodiment provides a solid catalyst configuration. The solid catalyst is granular and has an overall turbine shape. The solid catalyst particle 1 includes a columnar portion 11 and a finned portion 12. The columnar portion 11 has a columnar structure with catalyst active components distributed on both end faces, and the interior of the column is a catalyst support. The finned portion 12 is an integral structure with the columnar portion 11 and extends tangentially along the outer wall of the column. The surface of the fins is distributed with catalyst active components, and the interior of the fins is a catalyst support. Specifically, the fins can be evenly spaced along the circumference of the column to form an integral turbine structure, and the extension direction of the fins can be counterclockwise.

[0044] Further as Figure 1As shown, with this special catalyst configuration, after the rising gas and falling droplets encounter the solid catalyst particles 1, a vortex phenomenon can be formed under the guiding effect of the fin portions 12, so that the gas and droplets form a flow state where counter-current flow and cross-current flow coexist. The turbine-type solid catalyst particles 1 continuously rotate and move up and down under the combined action of rising airflow, self-gravity and falling droplets (that is, up-and-down reciprocating fluidization motion), which further strengthens the contact and mass transfer process of the gas-liquid-solid three phases.

[0045] Example 2

[0046] As Figure 2 shown, this embodiment provides a reactive distillation column 100 applying the solid catalyst configuration in Embodiment 1. By confining the solid catalyst particles 1 of Embodiment 1 in the gas-liquid mass transfer space 4, the gas-liquid-solid mass transfer reaction on each tray is completed under the condition that the solid catalyst is not immersed in the liquid accumulation layer A. The reactive distillation column 100 of this embodiment comprises a gas rising unit, a liquid descending unit and a gas-liquid mass transfer space 4. Wherein, the gas rising unit is fixed on the lower tray 101 and extends upward to above the liquid accumulation layer A, for providing the rising gas phase in a jet form. Specifically, without limitation, the gas rising unit can adopt a T-shaped gas distributor 2, with reference to Figure 2 , the gas distributor 2 comprises: a gas rising pipe 21 and branch pipes 22, wherein the bottom of the gas rising pipe 21 is fixed on the lower tray 101 and is used for receiving the rising gas phase from the lower layer, and the upper part of the gas rising pipe 21 extends to above the liquid accumulation layer A. The branch pipes 22 are arranged at the upper part of the gas rising pipe 21 and extend in the horizontal direction, and a plurality of branch pipes 22 can be provided and arranged radially outward along the gas rising pipe 21, for example, the arrangement method shown in Figure 3 (a "rice-shaped" arrangement) can be adopted. Upward nozzles 23 are uniformly arranged on the branch pipes 22. The nozzles are one of fan-shaped nozzles, rectangular nozzles or elliptical nozzles, and fan-shaped nozzles are preferably used. The rising gas from the lower layer enters the branch pipes 22 through the gas rising pipe 21, and is jetted upward through the nozzles 23 on the branch pipes.

[0047] Further as Figure 2 shown, the liquid descending unit is fixed on the upper tray and is used for providing falling droplets. Specifically, the liquid descending unit in this embodiment can adopt a liquid distributor, the liquid distributor is provided with liquid-phase nozzles 3 uniformly arranged below the tray, and the liquid-phase nozzles 3 can also adopt one of rectangular nozzles, elliptical nozzles or fan-shaped nozzles, with fan-shaped nozzles being preferred. The liquid phase from the liquid accumulation layer A on the upper tray is uniformly sprayed downward through the liquid-phase nozzles 3 on the tray. The downward-sprayed liquid contacts the rising gas from the lower tray (refer to the arrow direction in Figure 2 ) in the form of droplets A1. After contacting, the droplets A1 fall on the lower tray to form liquid accumulation, and then continue to be sprayed downward through the liquid-phase nozzles 3 on the lower tray.

[0048] Further as Figure 2 As shown, the gas-liquid mass transfer space 4 is located between the gas-rising unit and the liquid-falling unit and is enclosed by a perforated double-layer catalyst filter plate, used to limit the up-and-down reciprocating motion of the catalyst particles 1. Specifically, the double-layer catalyst filter plate includes an upper catalyst filter plate 41 and a lower catalyst filter plate 42. The diameter of the perforations on the filter plates is smaller than the diameter of the catalyst particles 1. Complete solid catalyst particles can be confined in the gas-liquid mass transfer space 4 between the double-layer catalyst filter plates. The perforations on the filter plates allow the rising gas phase and the falling liquid droplets to pass through. Preferably, but not limitingly, considering that the solid catalyst particles 1 need a certain vertical movement space, and in order to achieve a better gas-liquid mass transfer effect, experiments have verified that when the distance between two adjacent trays is H, placing the lower catalyst filter plate 42 at a height of 0.25 to 0.45H above the tray, and placing the upper catalyst filter plate 41 at a height of 0.3 to 0.4H above the lower catalyst filter plate 42, can achieve a better gas-liquid mass transfer effect.

[0049] Furthermore, to provide a more suitable lift force for the catalyst particles to rise, when the distance between two adjacent trays is H, the branch pipe is preferably located at a position of 0.1 to 0.2H below the lower catalyst filter plate 42. During the gas-liquid mass transfer reaction, the solid catalyst particles continuously move up and down between the upper catalyst filter plate 41 and the lower catalyst filter plate 42. Due to wear caused by mutual collisions, catalyst residue may penetrate the upper catalyst filter plate 41 and be carried into the upper tray by the rising gas. Therefore, in this embodiment, a filter screen 24 for blocking catalyst residue is provided at the lower end of the riser pipe 21.

[0050] In this embodiment, within the gas-liquid mass transfer space 4 between the upper catalyst filter plate 41 and the lower catalyst filter plate 42, the solid catalyst particles 1, in a non-liquid-immersed state, generate both countercurrent and crosscurrent gas-liquid flows through reciprocating rotational motion, thus completing and enhancing the gas-liquid-solid three-phase mass transfer reaction process. The specific process is as follows: the gas rising from the lower tray passes through the filter screen 24 and enters the riser pipe 21 of the gas distributor; the gas continuing to rise passes through... Figure 3The nozzles 23 on the "m"-shaped structural branch pipes 22 spray upward, and the upward-spraying gas drives the turbine-shaped solid catalyst particles 1 accumulated on the lower catalyst filter plate 42 to move upward. The catalyst particles continuously rotate during the rising process, and at the same time, the liquid on the upper tray is sprayed downward in the form of droplets through the liquid-phase nozzles 3. When the droplets encounter the rising and continuously rotating solid catalyst particles 1, the solid catalyst falls back under the action of drag force and the self-gravity of the particles. The falling back solid catalyst particles 1 are driven to rise by the rising gas, or fall onto the lower catalyst filter plate 42. Under the action of the rising gas and the falling droplets, the solid catalyst particles 1 perform up-and-down reciprocating motion between the upper catalyst filter plate 41 and the lower catalyst filter plate 42. Since the solid catalyst particle 1 is composed of a columnar part 11 and fin parts 12, the active components of the catalyst are arranged on the surfaces of the fin parts 12 and the two end faces of the columnar part 11, and the interior of the fin parts 12 and the columnar part 11 is a carrier, the turbine-shaped catalyst particle 1 has substantially the same catalytic efficiency as the existing catalysts. After the rising gas and falling droplets encounter the turbine-shaped solid catalyst particles 1, a vortex phenomenon is formed under the guiding action of the fin parts 12, so that the gas and droplets form a flow state where countercurrent and crossflow coexist. The solid catalyst particles 1 also continuously rotate and reciprocate up and down under the action of the gas flow, which further enhances the contact and mass transfer of gas-liquid-solid three phases.

[0051] The following is a specific example to illustrate the process method of the present invention and the effects that can be achieved:

[0052] Using the reactive distillation column of this embodiment, with acidic resin as the catalyst and adopting the solid catalyst configuration of the present invention, when the molar ratio of acetic acid to ethanol is 1:1 for feeding, the feeding pressure is 0.2 Mpa, the feeding temperature is 30°C, the number of trays is 42, acetic acid is fed from the 3rd tray, and ethanol is fed from the 39th tray, a product with a mass fraction of 95% ethyl acetate can be obtained, and the pressure drop of the whole column is 11 kpa.

[0053] Under the same feeding conditions, when using conventional distillation facilities equipped with conventional acidic resin solid catalysts and reaching the same yield of ethyl acetate, 67 trays are required, and the pressure drop of the whole column is 20 kpa.

[0054] The foregoing description of specific exemplary embodiments of the present invention is for illustrative and explanatory purposes. These descriptions are not intended to limit the invention to the precise forms disclosed, and it will be apparent that many changes and variations can be made in accordance with the foregoing teachings. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application, thereby enabling those skilled in the art to implement and utilize various different exemplary embodiments of the invention, as well as various different choices and variations. Any simple modifications, equivalent changes, and alterations made to the foregoing exemplary embodiments should fall within the scope of protection of the present invention.

Claims

1. A reactive distillation column, characterized in that, A solid catalyst configuration is applied, which is granular and turbine-shaped, comprising: a columnar part, which is a columnar structure with catalyst active components arranged on both end faces of the column, and the interior of the column is a catalyst support; and a finned part, which is an integral structure with the columnar part and extends tangentially along the outer wall of the column, with the catalyst active components arranged on the surface of the fin, and the interior of the fin is the catalyst support. The reactive distillation column utilizes the solid catalyst configuration to complete the gas-liquid-solid mass transfer reaction on each tray. The reactive distillation column includes: a gas rising unit, which is fixed on the lower tray and extends upward above the liquid layer to provide jet-like rising gas phase; a liquid falling unit, which is fixed on the upper tray to provide descending liquid droplets; and a gas-liquid mass transfer space, which is located between the gas rising unit and the liquid falling unit and is enclosed by a perforated double-layer catalyst filter plate to limit the up-and-down reciprocating motion of the catalyst particles.

2. The reactive distillation column according to claim 1, characterized in that, The fins are evenly spaced along the circumference of the column to form an integral turbine structure, and the extension direction of the fins is counterclockwise.

3. The reactive distillation column according to claim 2, characterized in that, The catalyst particles undergo a reciprocating fluidized motion in the gas-liquid mass transfer space due to the combined effects of the lift force of the gas phase, the gravity of the catalyst particles themselves, and the downward drag force of the droplets. At the same time, the rising gas phase and the falling droplets form a flow state in which countercurrent and cross-flow coexist.

4. The reactive distillation column according to claim 1, characterized in that, The double-layer catalyst filter plate includes an upper catalyst filter plate and a lower catalyst filter plate. The diameter of the perforated holes on the filter plate is smaller than the size of the catalyst particles, allowing rising gas phase and falling droplets to pass through.

5. The reactive distillation column according to claim 4, characterized in that, When the distance between two adjacent layers of trays is H, the lower catalyst filter plate is arranged at a height of 0.25 to 0.45H above the tray; the upper catalyst filter plate is arranged at a height of 0.3 to 0.4H above the lower catalyst filter plate.

6. The reactive distillation column according to claim 1, characterized in that, The gas lifting unit is a T-shaped gas distributor, which includes: The riser pipe is fixed at its bottom to the lower tray and is used to receive the rising gas phase from the lower layer. The upper part of the riser pipe extends above the liquid layer. A branch pipe is located above the riser pipe and extends horizontally, with upward-facing nozzles evenly distributed on the branch pipe.

7. The reactive distillation column according to claim 6, characterized in that, The number of branch pipes is multiple and they are arranged radially outward along the riser pipe; the nozzle is a fan-shaped nozzle, a rectangular nozzle, or an elliptical nozzle.

8. The reactive distillation column according to claim 6, characterized in that, When the distance between two adjacent trays is H, the branch pipe is located at a position of 0.1 to 0.2H below the lower catalyst filter plate.

9. The reactive distillation column according to claim 6, characterized in that, The lower end of the riser pipe is equipped with a filter screen to block catalyst residue.

10. The reactive distillation column according to claim 1, characterized in that, The liquid distribution unit is a liquid distributor fixed on the upper tray, and the liquid distributor is equipped with nozzles to provide uniformly sprayed liquid droplets downwards.

11. The reactive distillation column according to claim 1, characterized in that, In the gas-liquid mass transfer space, the catalyst particles, in a non-liquid-immersed state, form a coexistence of countercurrent and crosscurrent of gas and liquid through reciprocating rotational motion, thereby completing and enhancing the three-phase mass transfer reaction process of gas, liquid, and solid.

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