A tornado type cyclone enhanced gas-liquid-solid three-phase reactor and a method for gas-liquid-solid three-phase reaction using the same

Abstract

This invention discloses a tornado-type swirling enhanced gas-liquid-solid three-phase reactor and a method for conducting gas-liquid-solid three-phase reactions using it, belonging to the field of chemical reactor technology. The reactor of this invention includes an annular jacket space formed by an outer cylinder and an inner cylinder; a gas ejector with multiple nozzles at the bottom, each nozzle having both horizontal tangential and vertical upward components; a flow port in the middle of the inner cylinder sidewall, forming a "discontinuous jacket" structure; a composite heat exchange system including an outer jacket and an inner heat exchanger; and a built-in filter at the bottom. This invention drives the fluid to form a rotating upward circulation through multi-angle gas injection, combined with the discontinuous jacket to achieve integrated reaction, gas-liquid separation, and solid sedimentation. With precise temperature control by the composite heat exchange system, it achieves efficient mass and heat transfer, internal circulation of solid particles, and online product filtration. This invention has a simple structure, is inherently safe, and has a high degree of functional integration, making it particularly suitable for strongly exothermic gas-liquid-solid catalytic reactions, and has significant economic and social benefits.

Description

Technical Field

[0001] This invention relates to the field of chemical reactor technology, and more specifically, to a tornado-type swirling enhanced gas-liquid-solid three-phase reactor and a method for conducting gas-liquid-solid three-phase reactions therein. This invention is particularly applicable to strongly exothermic gas-liquid-solid catalytic reactions, such as hydrogenation, oxidation, and halogenation reactions, as well as in fields such as bio-fermentation and wastewater treatment. Background Technology

[0002] Gas-liquid-solid three-phase reactors are widely used in chemical, biological, and environmental protection fields. Traditional reactors mainly include mechanically stirred tank reactors, bubble column reactors, and fixed-bed reactors. However, these traditional devices generally suffer from the following problems when processing gas-liquid-solid three-phase systems: First, traditional mechanically stirred tank reactors rely on the mechanical movement of the agitator to achieve mixing, resulting in significant mixing dead zones, uneven distribution of solid catalysts or biomass, and utilization rates typically below 70%. Simultaneously, the dynamic seal of the agitator shaft is prone to leakage under high pressure, posing a significant safety hazard when handling flammable and explosive gases such as hydrogen and oxygen.

[0003] Secondly, many gas-liquid-solid reactions (such as hydrogenation and oxidation) are strongly exothermic processes. Traditional reactors have limited heat removal capabilities, and single jacket cooling often cannot remove the heat of reaction in time, which can easily lead to local overheating. This, in turn, can cause problems such as increased side reactions, catalyst coking and deactivation, or biomass deactivation, affecting product quality and yield.

[0004] Furthermore, for fine-particle catalysts or solid substrates, separation is usually required after the reaction, which involves a long process, high equipment investment, and easy catalyst loss.

[0005] In addition, some improvements have emerged in the existing technology. For example, Chinese patent CN101396647B (publication date: April 1, 2009) discloses a gas-liquid-solid three-phase suspended bed reactor for Fischer-Tropsch synthesis, which integrates heat exchange components and a liquid-solid filtration and separation device. Another example is Chinese patent CN106334500B (publication date: January 18, 2017), which discloses an external circulation reactor that simultaneously performs reaction, heat exchange, and separation functions, achieving separation through a hydrocyclone.

[0006] One of the closest prior art to this application is Chinese patent CN1962035A (publication date: May 16, 2007), which discloses a jet vortex bed gas-liquid-solid three-phase reactor. This scheme uses a circulating pump to extract the slurry and then inject it tangentially from the four corners to drive the slurry pool to rotate as a whole, replacing mechanical stirring. Oxidation air is introduced into the nozzle. However, this scheme has the following shortcomings: (1) Its injection medium is liquid phase, and the gas is passively entrained, which limits the gas dispersion effect and mass transfer efficiency, making it difficult to form a highly turbulent gas-liquid-solid three-phase contact interface; (2) No reaction-separation partition structure is set, which cannot realize online separation of gas, liquid and solid and internal circulation of solid particles. After the reaction, external equipment is still required for separation; (3) The heat exchange method is single, relying only on the heat exchange of the outer jacket. The heat transfer capacity is limited and cannot effectively cope with the local overheating and "runaway temperature" problems that may occur during strong exothermic reactions (such as hydrogenation and oxidation); (4) An external circulating pump is required to drive the liquid phase, which increases equipment investment and operating energy consumption, and the system complexity is high.

[0007] In summary, the existing technology lacks an integrated reactor design scheme that can simultaneously achieve efficient mixing and mass transfer, precise temperature control, internal circulation of solid particles, and online filtration of products within a single reactor. Summary of the Invention

[0008] The technical problem this invention aims to solve is to address the following shortcomings of existing gas-liquid-solid three-phase reactors: traditional mechanical stirring suffers from mixing dead zones and high-pressure dynamic seal leakage risks; single-jacket cooling and heat transfer capacity is insufficient, easily leading to local overheating; single function requires external equipment to separate solids after the reaction, resulting in long processes and high investment; existing improved solutions (such as jet cyclone reactors) have limited mass transfer efficiency and do not achieve integrated reaction-separation. This invention aims to provide an integrated reactor with a structurally integrated design, high efficiency in mass and heat transfer, intrinsic safety, and the ability to achieve internal circulation of solid particles and online filtration.

[0009] To solve the above-mentioned technical problems, the present invention adopts the following technical solution: This invention provides a tornado-type swirl-enhanced gas-liquid-solid three-phase reactor, comprising: The reactor shell includes an outer cylinder 1 and an inner cylinder 2. The inner cylinder 2 is coaxially disposed inside the outer cylinder 1, and an annular jacket space 3 is formed between the outer cylinder 1 and the inner cylinder 2. A gas injector 4 is disposed at the bottom of the reactor shell. The gas injector 4 has a plurality of nozzles 41, and the injection direction of the nozzles 41 has both a horizontal tangential component and a vertical upward component. The liquid inlet 5 is located on the upper part of the reactor shell and is used to introduce liquid reactants into the inner cylinder 2; Solid inlet 6 is located at the top of the reactor shell and is used to add solid particles; The composite heat exchange system includes an outer jacket 7 disposed on the outer wall of the outer cylinder 1 and at least one internal heat exchanger 8 disposed inside the reactor shell; The inner cylinder 2 has at least one flow port 21 in the middle region of the vertical direction on the side wall. The flow port 21 connects the annular jacket space 3 with the internal space of the inner cylinder 2. The fluid flow area at the flow port 21 is larger than the fluid flow area of ​​the annular jacket space 3, so that the fluid velocity is reduced when it enters the inner cylinder 2. An internal filter 9 is located in the bottom area of ​​the reactor shell; The gas phase outlet 10 is located at the top of the reactor shell.

[0010] As a further technical solution of the present invention, the projections of the plurality of nozzles 41 on the horizontal plane are evenly distributed along the circumference of the outer cylinder 1, and the angle between the center line of the nozzle 41 and the horizontal plane is 15° to 45°, and the angle between the center line of the nozzle 41 and the vertical plane is 5° to 30°.

[0011] As a further technical solution of the present invention, there are multiple flow ports 21, which are evenly distributed along the circumference of the inner cylinder 2.

[0012] As a further technical solution of the present invention, the internal heat exchanger 8 is a spiral coil, which is fixedly connected to the inner wall of the inner cylinder 2, and is located in the lower middle part of the annular jacket space 3, and below the flow port 21.

[0013] As a further technical solution of the present invention, the outer jacket 7 and the inner heat exchanger 8 are independently connected to the heat exchange medium supply system to control the flow rate and temperature of their heat exchange medium respectively.

[0014] Furthermore, the built-in filter 9 is a sintered metal filter element or a metal wire mesh filter element, and is equipped with a backwashing structure.

[0015] Furthermore, it also includes a sampling tube 11, which is disposed in the middle of the reactor shell, for sampling and analyzing the reaction mixture.

[0016] The present invention also provides a method for carrying out a gas-liquid-solid three-phase reaction in a gas-liquid-solid three-phase reactor as described in any one of the above claims, comprising the following steps: Step 1: Add solid particles through the solid inlet 6 and allow them to settle to the bottom of the reactor; Step 2: The liquid phase reactant is introduced into the inner cylinder 2 through the liquid phase inlet 5, and the gas phase reactant is injected tangentially and upwardly into the annular jacket space 3 through multiple nozzles 41 of the gas injector 4. Step 3: In the annular jacket space 3, the high-speed injected gas forms a jet pump effect, entraining liquid phase reactants and settled solid particles, forming a rotating and rising circulation. The gas-liquid-solid three phases react in this region. At the same time, the outer jacket 7 and the inner heat exchanger 8 work together to exchange heat on the reaction system. Step 4: When the reaction mixture rises to the flow port 21 of the inner cylinder 2, the flow area expands and the flow rate decreases, achieving preliminary gas-liquid separation. The separated gas is discharged from the gas phase outlet 10, while the liquid, carrying solid particles, settles downwards along the inside of the inner cylinder 2 under the action of gravity and returns to the bottom of the reactor, thereby forming an internal circulation of solid particles between the reaction zone of the annular jacket space 3 and the settling zone of the inner cylinder 2. Step 5: The qualified products generated by the reaction are continuously collected after being filtered by the built-in filter 9.

[0017] Preferably, in step three, the radial temperature difference in the reaction zone is controlled within ±2℃ by independently adjusting the flow rate and temperature of the heat exchange medium in the outer jacket 7 and the inner heat exchanger 8.

[0018] Preferably, in step three, the rotating and rising circulation causes the solid particles to form a reciprocating cycle of "jet lifting - sedimentation return" within the reactor, and the residence time of the solid particles in the reaction zone is 1 to 3 hours.

[0019] The core technical solution of this invention is as follows: (1) Power innovation: The traditional mechanical agitator is replaced by a gas ejector with multiple upward tilting angles 4. Multiple nozzles 41 simultaneously generate horizontal tangential and vertical upward jets, driving the gas-liquid-solid three phases in the annular jacket space 3 to form a "tornado" rotating upward flow, eliminating the risk of leakage of the agitator shaft dynamic seal from the source and greatly improving the mass transfer efficiency.

[0020] (2) Structural Integration: The "discontinuous jacket structure" is used—that is, a flow port 21 is set in the middle of the side wall of the inner cylinder 2, which causes a sudden change in the flow area, naturally dividing the same vertical container into three functional areas: the annular jacket space 3 below the flow port 21 is the circulating reaction zone, the flow port 21 is the gas-liquid separation zone, and the inside of the inner cylinder 2 is the solid settling zone. This structure does not require external circulation pipelines or additional separation equipment, realizing the integration of reaction, separation and settling.

[0021] (3) Synergistic thermal management: The "combined cooling of external sleeve 7 and internal heat exchanger 8" method is adopted, and the internal heat exchanger 8 is set in the middle and lower part of the circulating reaction zone - that is, the core area with the strongest turbulence. The functions of the two are clearly defined: the external sleeve 7 is responsible for basic heat exchange, and the internal heat exchanger 8 is responsible for local strong heat release and heat transfer. They can be controlled independently, realizing precise control of reaction temperature.

[0022] Compared with the prior art, the present invention has the following beneficial effects: (1) Significantly improved mass and heat transfer efficiency: The traditional mechanical stirring is replaced by "multi-angle tangential injection". The jet pump effect is formed by gas phase injection, which drives the fluid to generate a "tornado" swirling flow. The gas-liquid-solid three-phase contact area and mass transfer efficiency are much higher than those of the traditional stirred tank. The gas-liquid mass transfer coefficient is increased by 45% in the pilot test. The composite heat exchange system (external jacket + internal heat exchanger) increases the overall heat transfer coefficient by more than 28% compared with single jacket cooling. The measured radial temperature difference of the bed is less than 1.5℃, which is particularly suitable for strong exothermic reactions. At the same time, the flow port set on the inner cylinder side wall forms a variable diameter structure, which naturally divides the circulating reaction zone, gas-liquid separation zone and solid sedimentation zone in the same container, realizing the integrated integration of reaction, separation and sedimentation.

[0023] (2) Simplified structure and inherent safety: The traditional mechanical stirring and high-pressure dynamic seal are eliminated, eliminating the main leakage risk points. The equipment structure is simpler, the manufacturing and maintenance costs are lower, and the inherent safety is higher.

[0024] (3) Highly integrated functions: The reactor integrates four major functions: reaction, gas-liquid separation, solid sedimentation and product filtration. It does not require external circulation pipelines or hydrocyclones or other additional equipment, which greatly shortens the process flow and reduces investment and operating costs. With the sampling pipe in the middle of the reactor and the built-in filter at the bottom, a quality control closed loop of "reaction monitoring - qualified sampling" is formed to realize continuous production.

[0025] (4) Improved solid particle utilization and reaction continuity: Solid particles in the reactor rely on gravity settling and gas jet entrainment to achieve the reciprocating motion of "floating reaction - sinking cycle", which prolongs the residence time of particles in the reaction zone. The built-in filter ensures that particles are not lost, enabling truly continuous production.

[0026] (5) Flexible operation and precise control: The outer jacket and the inner heat exchanger can be controlled independently and can be precisely adjusted according to the thermal effect of different reaction stages, effectively preventing "overheating" and side reactions. Attached Figure Description

[0027] Figure 1 This is a schematic diagram of the structure of a gas-liquid-solid three-phase reactor provided in an embodiment of the present invention.

[0028] Figure 2 for Figure 1 The cross-sectional view along the AA direction shows the nozzle distribution and injection direction of the gas injector.

[0029] Explanation of markings in the diagram: 1-Outer cylinder; 2-Inner cylinder; 21-Flow port; 3-Annular jacket space; 4-Gas ejector; 41-Nozzle; 5-Liquid inlet; 6-Solid inlet; 7-Outer jacket; 8-Inner heat exchanger; 9-Built-in filter; 10-Gas outlet; 11-Sampling tube. Detailed Implementation

[0030] To make the objectives, technical solutions, and advantages of this invention clearer, the technical solutions in the embodiments of this invention will be clearly and completely described below with reference to specific embodiments and the accompanying drawings. Obviously, the described embodiments are only some embodiments of this invention, and not all embodiments. Based on the embodiments of this invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this invention.

[0031] Example 1: Reactor Structure

[0032] like Figure 1 As shown, this embodiment provides a tornado-type swirl-enhanced gas-liquid-solid three-phase reactor. The reactor includes a vertical cylindrical reactor shell, which is composed of an outer cylinder 1 and an inner cylinder 2 coaxially disposed inside it. An annular jacket space 3 is formed between the outer cylinder 1 and the inner cylinder 2.

[0033] A gas ejector 4 is installed at the bottom of the reactor. The gas ejector 4 has multiple nozzles 41. Figure 2 As shown, the projections of multiple nozzles 41 on the horizontal plane are uniformly distributed along the circumference of the outer cylinder 1. The injection direction of each nozzle 41 simultaneously has a horizontal tangential component and a vertical upward component. Specifically, the angle α between the centerline of the nozzle 41 and the horizontal plane is 30°, and the angle β between the centerline and the vertical plane is 15°. This angle range (horizontal inclination 15-45°, vertical inclination 5-30°) was determined through computational fluid dynamics (CFD) simulation optimization: if the horizontal inclination angle is less than 15° or greater than 45°, a stable rotating upward flow cannot be formed; if the vertical inclination angle is less than 5°, the lifting force of solid particles is insufficient, and they are prone to deposition; if it is greater than 30°, the residence time of solid particles in the reaction zone is too short, affecting the reaction efficiency. Within this optimized range, a stable 'tornado' swirling flow can be formed, achieving the best mass transfer and solid circulation effect. This "multi-angle" design enables the injected gas to drive the fluid within the annular jacket space 3 to form a strong rotating upward flow.

[0034] A liquid inlet 5 is provided at the top of the reactor shell to introduce liquid reactants into the inner cylinder 2. A solid inlet 6 is provided at the top of the reactor shell for adding solid particles (such as catalyst). A gas outlet 10 is also provided at the top of the reactor shell.

[0035] Multiple flow ports 21 are provided on the sidewall of the inner cylinder 2 in the central region of the vertical direction. These flow ports 21 are evenly distributed along the circumference of the inner cylinder 2. The flow ports 21 connect the annular jacket space 3 with the internal space of the inner cylinder 2. The total opening area of ​​the flow ports 21 is larger than the fluid flow cross-sectional area of ​​the annular jacket space 3, forming a variable diameter structure. This causes the flow area to suddenly expand and the flow velocity to decrease significantly when the fluid enters the inner cylinder 2 from the annular jacket space 3, thereby achieving preliminary gas-liquid separation. This variable diameter structure functionally divides the reactor into three regions: the annular jacket space 3 below the flow ports 21 is the circulating reaction zone, the flow ports 21 are the gas-liquid separation zone, and the interior of the inner cylinder 2 is the solid settling zone.

[0036] An internal filter 9 is installed at the bottom of the reactor shell. In this embodiment, a sintered metal filter element is used, and a backwashing structure is configured to filter and extract clear reaction products.

[0037] The composite heat exchange system includes an outer jacket 7 disposed on the outer wall of the outer cylinder 1 and an inner heat exchanger 8 disposed inside the reactor shell. In this embodiment, the inner heat exchanger 8 adopts a spiral coil structure, is fixedly connected to the inner wall of the inner cylinder 2, is located inside the inner cylinder 2, and is located below the flow port 21, i.e., the core region where the turbulence is most intense in the circulation zone. The outer jacket 7 and the inner heat exchanger 8 are independently connected to an external heat exchange medium supply system, and their flow rate, temperature, and type of heat exchange medium can be controlled separately.

[0038] A sampling tube 11 is also installed in the middle of the reactor shell for sampling and analyzing the reaction mixture.

[0039] Example 2: Hydrogenation reaction using this reactor

[0040] This embodiment uses a typical hydrogenation reaction as an example to illustrate the method of conducting a gas-liquid-solid three-phase reaction using the reactor of the present invention. The pilot-scale experiment was completed in March 2025, with a processing capacity of 50 kg / h.

[0041] Step 1: Add solid catalyst with an average particle size of 50 μm into the reactor through solid inlet 6. The catalyst settles to the bottom of the reactor under gravity, and the initial solid content is controlled at 10 wt%.

[0042] Step 2: Introduce the liquid reactant into the inner cylinder 2 through the liquid inlet 5, controlling the flow rate to a liquid space velocity of 0.5 h⁻¹. -1 Simultaneously, hydrogen gas is injected tangentially and upwardly into the annular jacket space 3 through multiple nozzles 41 of the gas injector 4, controlling the hydrogen partial pressure to be 1.8 MPa.

[0043] Step 3: Within the annular jacket space 3, high-speed injected hydrogen gas creates a jet pump effect, entraining liquid-phase reactants and settled catalyst, forming a rotating and rising circulation. The gas-liquid-solid three phases efficiently contact and undergo hydrogenation in this region. The heat released by the reaction is removed through a composite heat exchange system: cooling water is introduced into the outer jacket 7 for basic heat exchange, while low-temperature cooling water is introduced into the inner heat exchanger 8 (spiral coil), directly contacting the highly turbulent reaction fluid and rapidly removing the heat generated by the locally exothermic reaction. By independently adjusting the flow rates of the two heat exchange media, the reaction temperature is precisely controlled at 125±2℃, and the measured radial temperature difference of the bed is less than 1.5℃.

[0044] Step 4: When the reaction mixture rises to the flow port 21 of the inner cylinder 2, the flow rate decreases due to the sudden expansion of the flow area, and the gas and liquid achieve preliminary separation. The separated gas is discharged from the gas phase outlet 10, pressurized by the external circulating compressor, mixed with fresh hydrogen, and returned to the gas ejector 4 for recycling. The liquid, carrying catalyst particles, settles downwards under gravity and returns to the bottom of the reactor, waiting to be entrained and circulated by the gas ejector 4 again, forming an internal circulation of solid particles of "jet lifting-settling return".

[0045] Step 5: During the reaction, samples are taken periodically for analysis using sampling tube 11. Once the product is qualified, the built-in filter 9 is turned on to continuously collect clear reaction products, with a solid content of less than 50 ppm in the collected liquid.

[0046] Comparative Example 1: Comparative Experiment of Traditional Stirred Tank Reactor

[0047] To verify the technical effect of this invention, a comparative experiment was conducted under the same operating conditions using a traditional mechanically stirred tank reactor (equipped with a three-layer, six-bladed turbine impeller, a mechanical seal at the shaft end, external jacket cooling, and no internal heat exchanger). The reaction system, catalyst, and process conditions (reaction temperature 125℃, hydrogen partial pressure 1.8 MPa, liquid hourly space velocity 0.5 h⁻¹) were also tested. -1 The catalyst (average particle size 50 μm, solid content 10 wt%) was consistent with that in Example 2.

[0048] The results of the comparative experiment are as follows: index This invention (Example 2) Traditional stirred tank (Comparative Example 1) Comparison results reaction conversion rate 98.7% 95.2% Increased by 3.5 percentage points Target product selectivity 96.5% 93.7% Increased by 2.8 percentage points Bed radial temperature difference <1.5℃ 4.5-6.0℃ Significant improvement Gas-liquid mass transfer coefficient (KLa) Increase by 45% benchmark value Significantly improved Power consumption (including circulating pump / stirring motor) Reduced by more than 60% benchmark value Significantly reduced Continuous operation stability 500 hours without abnormalities After 200 hours, a slight leak was sealed. Superior safety and stability Note: This reactor does not have mechanical stirring. The power consumption comparison refers to the motor power consumption of a traditional stirred tank and the circulation pump power consumption of this solution.

[0049] The above comparison results fully demonstrate that the present invention is significantly superior to the traditional stirred tank reactor in terms of mass transfer efficiency, temperature control, operational stability and energy consumption, achieving unexpected technical effects and realizing the core innovations of "multi-angle gas injection" to replace mechanical stirring, "interrupted jacket" to achieve functional zoning, and "composite heat exchange" for precise temperature control.

[0050] Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A tornado-type cyclone-enhanced gas-liquid-solid three-phase reactor, characterized in that: include, The reactor shell includes an outer cylinder (1) and an inner cylinder (2), the inner cylinder (2) being coaxially disposed inside the outer cylinder (1), and an annular jacket space (3) being formed between the outer cylinder (1) and the inner cylinder (2). A gas injector (4) is disposed at the bottom of the reactor shell. The gas injector (4) has multiple nozzles (41). The injection direction of the nozzles (41) has both a horizontal tangential component and a vertical upward component. A liquid inlet (5) is provided on the upper part of the reactor shell to introduce liquid reactants into the inner cylinder (2); A solid inlet (6) is located at the top of the reactor shell and is used to add solid particles; The composite heat exchange system includes an outer jacket (7) disposed on the outer wall of the outer cylinder (1) and at least one internal heat exchanger (8) disposed inside the reactor shell. The inner cylinder (2) has at least one flow port (21) in the middle area of ​​the vertical direction on the side wall. The flow port (21) connects the annular jacket space (3) with the internal space of the inner cylinder (2). The fluid flow area at the flow port (21) is larger than the fluid flow area of ​​the annular jacket space (3) so that the fluid velocity is reduced when it enters the inner cylinder (2). An internal filter (9) is provided in the bottom region of the reactor shell; A gas phase outlet (10) is located at the top of the reactor shell.

2. The gas-liquid-solid three-phase reactor according to claim 1, characterized in that: The projections of the plurality of nozzles (41) on the horizontal plane are evenly distributed along the circumference of the outer cylinder (1), and the angle between the center line of the nozzle (41) and the horizontal plane is 15° to 45°, and the angle between the center line of the nozzle (41) and the vertical plane is 5° to 30°.

3. The gas-liquid-solid three-phase reactor according to claim 1, characterized in that: There are multiple flow ports (21), which are evenly distributed along the circumference of the inner cylinder (2).

4. The gas-liquid-solid three-phase reactor according to claim 1, characterized in that: The internal heat exchanger (8) is a spiral coil, which is fixedly connected to the inner wall of the inner cylinder (2), located in the lower middle part of the annular jacket space (3), and below the flow port (21).

5. The gas-liquid-solid three-phase reactor according to claim 1, characterized in that: The outer jacket (7) and the inner heat exchanger (8) are independently connected to the heat exchange medium supply system to control the flow rate and temperature of their respective heat exchange mediums.

6. The gas-liquid-solid three-phase reactor according to claim 1, characterized in that: The built-in filter (9) is a sintered metal filter element or a metal wire mesh filter element, and is equipped with a backwashing structure.

7. The gas-liquid-solid three-phase reactor according to claim 1, characterized in that: It also includes a sampling tube (11), which is located in the middle of the reactor shell and is used to sample and analyze the reaction mixture.

8. A method for carrying out a gas-liquid-solid three-phase reaction using the gas-liquid-solid three-phase reactor according to any one of claims 1-7, characterized in that: Includes the following steps: Step 1: Add solid particles through the solid inlet (6) and allow them to settle to the bottom of the reactor; Step 2: The liquid phase reactant is introduced into the inner cylinder (2) from the liquid phase inlet (5), and the gas phase reactant is injected tangentially and upwardly into the annular jacket space (3) through multiple nozzles (41) of the gas injector (4). Step 3: In the annular jacket space (3), the high-speed injected gas forms a jet pump effect, entraining liquid phase reactants and settled solid particles, forming a rotating and rising circulation. The gas-liquid-solid three phases react in this region. At the same time, the outer jacket (7) and the inner heat exchanger (8) work together to exchange heat on the reaction system. Step 4: When the reaction mixture rises to the flow port (21) of the inner cylinder (2), the flow area expands and the flow rate decreases, achieving preliminary gas-liquid separation. The separated gas is discharged from the gas phase outlet (10), while the liquid, carrying solid particles, settles downward along the inside of the inner cylinder (2) under the action of gravity and returns to the bottom of the reactor, thereby forming an internal circulation of solid particles between the reaction zone of the annular jacket space (3) and the settling zone of the inner cylinder (2). Step 5: The qualified products generated by the reaction are continuously collected after being filtered by the built-in filter (9).

9. The method according to claim 8, characterized in that: In step three, the radial temperature difference in the reaction zone is controlled within ±2℃ by independently adjusting the flow rate and temperature of the heat exchange medium in the outer jacket (7) and the inner heat exchanger (8).

10. The method according to claim 8, characterized in that: In step three, the rotating and rising circulation causes the solid particles to form a reciprocating cycle of "jet lifting - sedimentation return" within the reactor, and the residence time of the solid particles in the reaction zone is 1 to 3 hours.

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