An array of forced hydrocyclones reactor

Abstract

This invention discloses a forced hydrocyclone array reactor, comprising: multiple standardized reactor shells; the multiple standardized reactor shells are vertically arranged and connected in series or parallel; each standardized reactor shell contains a coaxial contact catalytic interface component, and each standardized reactor shell has an upper fluid port and a lower fluid port on its outer side, the axes of which are parallel to the tangent of the inner concentric circle of the standardized reactor shell, so as to achieve a rotating flow state of the fluid inside the standardized reactor shell. This invention adopts an external forced hydrocyclone propulsion mechanism and an optimized reactor structure to significantly improve the reactor space utilization efficiency; the enhanced high-speed rotating flow improves the dynamic contact efficiency between the fluid and the contact catalytic interface component, simultaneously improves the uniformity of water flow distribution, and ensures that the velocity of the rotating flow is dynamically controllable.

Description

Technical Field

[0001] This invention relates to the field of gaseous or liquid pollutant treatment technology, and specifically to a forced hydrocyclone array reactor. Background Technology

[0002] The background technology of this invention will be described with a focus on the treatment and removal of pollutants in fluids.

[0003] In the field of water pollution control equipment, contact mass transfer reaction is an indispensable fundamental principle and cornerstone for core technologies such as biochemical treatment, surface chemical catalytic reaction treatment, surface adsorption treatment, and surface electrochemical oxidation-reduction treatment. Therefore, developing a highly efficient contact mass transfer reactor that is versatile, efficient, and easy to design, produce, and engineer has become one of the keys to upgrading the efficiency of environmental protection equipment.

[0004] For example, in a three-dimensional biofilm reaction system, the contact time and frequency between the water and the microorganisms on the surface of the biological carrier directly determine the biodegradation efficiency. The same applies to electrochemical catalytic oxidation-reduction systems on the anode and cathode surfaces, where the reaction rate is significantly influenced by factors such as mass transfer efficiency, catalytic contact frequency, and contact time. In high-intensity photocatalytic oxidation systems (such as high-ultraviolet photocatalytic oxidation systems), the light source has a specific effective excitation distance. Within this range, the higher the frequency of water circulation, the more complete the photocatalytic reaction, and the more ideal the pollutant oxidation and degradation effect. Therefore, high-performance contact oxidation or catalytic oxidation reactors require advanced design concepts, innovative structural optimization, high equipment integration, simplified equipment module design, and novel operating mechanisms to achieve upgrades in reactor application scenarios, mass transfer efficiency, and intelligent operation control. Summary of the Invention

[0005] To address the problems of low space utilization, low internal circulation contact frequency, and uneven flow pattern in existing internal recirculation reactors, especially small internal recirculation reactors, this invention provides a forced hydraulic vortex array reactor.

[0006] This invention discloses a forced hydrocyclone array reactor, comprising multiple standardized reactor shells;

[0007] Multiple standardized reactor shells are vertically arranged and connected in series or in parallel to enable fluid to flow between the standardized reactor shells in a series or parallel manner.

[0008] Each standardized reactor shell contains a coaxial contact catalytic interface assembly, and an annular cavity is formed between the standardized reactor shell and the contact catalytic interface assembly. Each standardized reactor shell has an upper fluid port and a lower fluid port on its outer side. The axes of the upper fluid port and the lower fluid port are parallel to the tangent of the inner concentric circle of the standardized reactor shell, so as to achieve a rotating flow state of fluid inside the standardized reactor shell. The axes of the upper fluid port and the lower fluid port represent the fluid flow direction, and the tangent of the inner concentric circle of the standardized reactor shell represents the internal fluid flow direction of the standardized reactor shell.

[0009] As a further improvement of the present invention, it also includes: a sealing top cover; the sealing top cover is located on the upper part of the standardized reactor shell and is used for pressure sealing of the standardized reactor shell, and the sealing top cover has a central circular hole; the contact catalytic interface assembly passes through the central circular hole of the sealing top cover and is vertically installed inside the shell along the axis of the standardized reactor shell, and the gap between the sealing top cover and the contact catalytic interface assembly is filled with a sealing plug.

[0010] As a further improvement of the present invention, multiple standardized reactor shells are arranged in a triangular matrix in batches.

[0011] As a further improvement of the present invention, based on the different angles between the axes of the upper and lower fluid ports of the standardized reactor shell and the radial line from the center of the standardized reactor shell to the center point of the port inlet, the standardized reactor shell is divided into T1 to T5 types of reactor shells.

[0012] As a further improvement of the present invention, the T1 type reactor shell is characterized in that: the angle between the axis of the lower fluid port and the radial line of the lower fluid port is 30° or 52°, the angle between the axis of the upper fluid port and the radial line of the upper fluid port is 30° or 52°, and the angle between the radial line of the lower fluid port and the radial line of the upper fluid port is 120° or 76°; the T2 and T5 type reactor shells are characterized in that: the angle between the axis of the lower fluid port and the radial line of the lower fluid port is... The angle between the axis of the upper fluid port and the radial line of the upper fluid port is 65°, the angle between the radial line of the lower fluid port and the radial line of the upper fluid port is 30°, and the angle between the radial line of the lower fluid port and the radial line of the upper fluid port is 150°; the T3 and T4 type reactor shells are characterized in that: the angle between the axis of the lower fluid port and the radial line of the lower fluid port is 65°, the angle between the axis of the upper fluid port and the radial line of the upper fluid port is 30°, and the angle between the radial line of the lower fluid port and the radial line of the upper fluid port is 30°.

[0013] As a further improvement of the present invention, the upper fluid ports of different standardized reactor shells are connected to each other, and the lower fluid ports are connected to each other, so as to realize the matrix-based series connection or parallel connection of the standardized reactor shells.

[0014] As a further improvement of the present invention, the standardized reactor shell connected in a matrix series is mounted on the base frame, and is fixed by an auxiliary fixing frame in the upper middle part.

[0015] As a further improvement of the present invention, the fluid includes a gas or liquid to be reacted, and the contact catalytic interface component includes an electrode catalytic component, a strong photocatalytic oxidation component, a specially made transition metal coating surface catalytic component, a biological filler carrier component, and a surface adsorption component.

[0016] As a further improvement of the present invention, a stabilizing head is also connected to the upper part of the contact catalytic interface component for connecting and fixing the contact catalytic interface component. The upper part of the stabilizing head is also provided with a lifting ring. According to the actual use scenario requirements of the reactor, a special functional module is also configured inside the stabilizing head. The special functional module includes a smart electronic control end component and an anode generator. The smart electronic control end component or the anode generator is connected to the power supply through a connecting cable. A grounding electrode or a negative electrode is installed on the standardized reactor shell.

[0017] As a further improvement of the present invention, an auxiliary additive port branch is also connected to the inflow pipes of the upper fluid port and the lower fluid port.

[0018] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0019] This invention employs an external forced swirling flow mechanism and an optimized reactor structure to significantly improve reactor space utilization efficiency; it enhances the dynamic contact efficiency between the fluid and the contact catalytic interface components through enhanced high-speed swirling flow, simultaneously improves the uniformity of water flow distribution, and ensures that the swirling flow velocity is dynamically controllable.

[0020] This invention achieves a triangular matrix-style batch connection arrangement of reactors through the design of standardized reactor shells of different models. The reactors can be connected in parallel or in series, and the number is adjustable, which improves the flexibility, versatility and space utilization efficiency of the overall reactor arrangement. At the same time, through the staggered laminar flow docking interface connection method, the staggered mixing and contact reaction of the laminar flow inside and outside the reactor is realized, which further improves the contact mass transfer efficiency of the reactor and ensures a more efficient treatment effect.

[0021] The contact catalytic interface components of this invention can be electrode catalytic components, high-intensity photocatalytic oxidation components, specially designed transition metal coated surface catalytic components, biological packing carrier components, surface adsorption components, etc., making them fully adaptable to different reactors and reaction processes, greatly expanding the application scenarios of the reactors. This achievement can provide practical reference for the standardization, mass production, universal application scenarios, and engineering design and manufacturing of compact mixed contact mass transfer reactors. Attached Figure Description

[0022] Figure 1 This is an sectional view of the assembly of the forced hydrocyclone array reactor disclosed in this invention.

[0023] Figure 2 This is a top view (middle height plane) of the array assembly of the forced hydrocyclone array reactor disclosed in this invention.

[0024] Figure 3 This is a top view of the overall assembly bottom base frame of the forced hydrocyclone array reactor disclosed in this invention;

[0025] Figure 4 This is a top view of the upper auxiliary fixing frame of the forced hydrocyclone array reactor disclosed in this invention.

[0026] Figure 5 This is a top view schematic diagram of the flow state of the assembled components C to D disclosed in this invention;

[0027] Figure 6 This is a top view of the reactor shell of type T1 to T5 disclosed in this invention.

[0028] In the picture:

[0029] 1. Standardized reactor shell; 2. Contact catalytic interface assembly; 3. Sealed top cover; 4. Sealing stopcock; 5. Stabilizing head; 6. Connecting cable; 7. Lifting ring; 8. Upper fluid port; 9. Lower fluid port; 10. Base frame; 11. Auxiliary fixing frame; 12. Auxiliary additive port; 13. Grounding electrode or negative electrode; 14. Special function module; 15. Main inlet; 16. Main effluent. Detailed Implementation

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

[0031] The present invention will now be described in further detail with reference to the accompanying drawings:

[0032] like Figures 1-6 As shown, this invention provides a forced hydrocyclone array reactor, which is applicable to various contact mass transfer reaction processes such as biochemical treatment, surface chemical catalytic reaction treatment, surface adsorption treatment, and surface electrochemical oxidation-reduction treatment. It is also applicable to the treatment of gaseous and liquid fluid pollution. It includes: a standardized reactor shell 1, a contact catalytic interface component 2, a sealed top cover 3, a sealed plug 4, a stabilizing head 5, a connecting cable 6, a lifting ring 7, an upper fluid port 8, a lower fluid port 9, a base frame 10, an auxiliary fixing frame 11, an auxiliary additive port 12, a grounding electrode or negative electrode 13, a special functional module 14, a main inlet 15, and a main outlet 16.

[0033] Specifically:

[0034] In this invention, multiple standardized reactor shells 1 are vertically arranged and connected in series or parallel. Within each standardized reactor shell 1, a sealing top cover 3 is located at the top and serves as a pressure-bearing seal. The sealing top cover 3 has a central circular hole. A contact catalytic interface assembly 2 passes through the central circular hole of the sealing top cover 3 and is vertically installed inside the shell along the axis of the standardized reactor shell 1. The gap between the sealing top cover 3 and the contact catalytic interface assembly 2 is filled with a sealing plug 4 to achieve a sealing effect.

[0035] The standardized reactor shell 1 of the present invention is provided with an upper fluid port 8 and a lower fluid port 9 on its outer side. The axes (fluid flow direction) of the upper fluid port 8 and the lower fluid port 9 are parallel to the tangent of the concentric circle inside the standardized reactor shell 1 (internal fluid flow direction). This allows the fluid to be controlled to flow into the shell from the upper fluid port 8 in a tangential direction and then out of the shell from the lower fluid port 9 in a tangential direction. Alternatively, the fluid can be controlled to flow into the shell from the lower fluid port 9 in a tangential direction and then out of the shell from the upper fluid port 8 in a tangential direction. This ensures that the fluid is always in a high-speed rotating flow state inside the standardized reactor shell 1, enhancing the rotational agitation and mass transfer mixing of the fluid and improving the reaction efficiency.

[0036] Based on the different angles between the axes of the upper fluid port 8 and the lower fluid port 9 of the standardized reactor shell 1 and the radial line from the center of the standardized reactor shell 1 to the center point of the port inlet, this invention classifies the standardized reactor shell 1 into five installation models, T1 to T5, namely, T1-T5 type reactor shells. Specifically, the T1 type reactor shell is characterized by: the angle between the axis of the lower fluid port 9 and the radial line of the lower fluid port 9 being 30° (or 52°); the angle between the axis of the upper fluid port 8 and the radial line of the upper fluid port 8 being 30° (or 52°); and the angle between the radial line of the lower fluid port 9 and the radial line of the upper fluid port 8 being 120° (or 76°). The T2 and T5 type reactor shells are characterized by: the angle between the axis of the lower fluid port 9 and the radial line of the lower fluid port 9 being 65°; the angle between the axis of the upper fluid port 8 and the radial line of the upper fluid port 8 being 30°; and the angle between the radial line of the lower fluid port 9 and the radial line of the upper fluid port 8 being 150°. °; The characteristics of the T3 and T4 reactor shells are: the angle between the axis of the lower fluid port 9 and the radial line of the lower fluid port 9 is 65°, the angle between the axis of the upper fluid port 8 and the radial line of the upper fluid port 8 is 30°, and the angle between the radial line of the lower fluid port 9 and the radial line of the upper fluid port 8 is 30°; the T5 reactor shell can be regarded as a 180° rotated installation of the T2 reactor shell, and the fluid inlet and outlet can be interchanged, so it can be regarded as the same type of reactor shell; similarly, the T3 and T4 reactor shells can be regarded as the same type of reactor shell, and the actual processing and production can be carried out according to the three standardized reactor shells 1 of T1, T3 and T5, for details see Figure 6 .

[0037] In this invention, the upper fluid ports 8 and lower fluid ports 9 of different standardized reactor shells 1 are connected to each other. That is, along the wastewater treatment direction, if the lower fluid port 9 of the first upstream standardized reactor shell 1 is used as an inlet, then the upper fluid port 8 of the first standardized reactor shell 1 is connected to the upper fluid port 8 of the second standardized reactor shell 1, and the lower fluid port 9 of the second standardized reactor shell 1 is connected to the lower fluid port 9 of the third standardized reactor shell 1, and so on. If the upper fluid port 8 of the first upstream standardized reactor shell 1 is used as an inlet, then the lower fluid port 9 of the first standardized reactor shell 1 is connected to the lower fluid port 9 of the second standardized reactor shell 1, and the upper fluid port 8 of the second standardized reactor shell 1 is connected to the upper fluid port 8 of the third standardized reactor shell 1, and so on. This achieves a matrix-like series connection of the standardized reactor shells 1, such as... Figure 1 , Figure 2Meanwhile, depending on the actual water quality or usage scenario, the standardized reactor shell 1 can also be used in parallel or as a single independent unit, making the installation and application scenarios flexible.

[0038] Furthermore, the standardized reactor shell 1 of the present invention, which is connected in a matrix-like series, is mounted on the base frame 10 (e.g., Figure 3 ), and the upper middle part is fixed by an auxiliary fixing frame 11 (such as Figure 4 ).

[0039] Furthermore, the fluid in this invention can be a gas or liquid to be reacted, or it can be a pollutant removal process or a product manufacturing process.

[0040] Furthermore, the contact catalytic interface component 2 of the present invention can be an electrode catalytic component, a strong photocatalytic oxidation component, a specially made transition metal coating surface catalytic component, a biological filler carrier component, a surface adsorption component, etc.

[0041] Furthermore, the upper part of the contact catalytic interface component 2 of the present invention is also connected to a stabilizing head 5 for connecting and fixing the contact catalytic interface component 2. The upper part of the stabilizing head 5 is also a lifting ring 7, which can lift the contact catalytic interface component 2 as a whole out, making it convenient for installation and maintenance.

[0042] Furthermore, depending on the actual usage scenario of the reactor, the stabilizing head 5 of the present invention can also be configured with a special functional module 14, which can be a smart electronic control end component, an anode generator, etc., and can be connected to a power supply via a connecting cable 6; the standardized reactor shell 1 can be equipped with a grounding electrode or a negative electrode 13.

[0043] For example:

[0044] When the contact catalytic interface component 2 is a biological packing carrier component, there is no need to select a special functional module 14, connecting cable 6, and grounding electrode or negative electrode 13. At this time, the standardized reactor is a high-efficiency bioreactor.

[0045] When the contact catalytic interface component 2 is a strong photocatalytic oxidation component, the matching special function module 14 is a smart electronic control terminal component, and the matching connecting cable 6 is provided. There is no need to select the grounding electrode or negative electrode 13. At this time, the standardized reactor is a high-efficiency photocatalytic oxidation reactor.

[0046] When the contact catalytic interface component 2 is an electrode catalytic component, the special functional module 14 is an anode generator, and is equipped with connecting cable 6 and grounding electrode or negative electrode 13. At this time, the standardized reactor is an electrocatalytic oxidation-reduction reactor.

[0047] Furthermore, auxiliary additive ports 12 can be connected to the inflow pipes of the upper fluid port 8 and the lower fluid port 9 to enhance the efficiency of the contact mass transfer reaction. For example, when the standardized reactor is used as a high-efficiency bioreactor, microbial nutrient solution can be added to the auxiliary additive port 12 to improve microbial activity; when the standardized reactor is used as a high-efficiency photocatalytic oxidation reactor, hydrogen peroxide can be added to the auxiliary additive port 12 to improve the synergistic effect of advanced oxidation.

[0048] Additional instructions on the use of this invention:

[0049] Note 1: For example Figure 1 The fluid flows in from the main inlet 15, then enters the first standardized reactor through the lower fluid port 9. It flows through the cavity between the standardized reactor shell 1 and the contact catalytic interface component 2 from the bottom of the first standardized reactor, undergoes the corresponding reaction, and then flows upward to the upper fluid port 8 of the first standardized reactor and out. The upper fluid port 8 of the first standardized reactor is connected to the upper fluid port 8 of the second standardized reactor, and the fluid enters the second standardized reactor from the upper fluid port 8. It flows through the cavity between the standardized reactor shell 1 and the contact catalytic interface component 2 from the top of the second standardized reactor, undergoes the corresponding reaction, and then flows downward to the lower fluid port 9 of the second standardized reactor and out. The lower fluid port 9 of the second standardized reactor is connected to the lower fluid port 9 of the third standardized reactor, and the fluid enters the third standardized reactor from the lower fluid port 9. This process continues, with the fluid moving up and down, following the longest path through the cavities between the shells of all standardized reactors 1 and the contact catalytic interface components 2, undergoing sufficient reaction, until it reaches the main outlet 16 for qualified discharge.

[0050] Note 2: For example Figure 2 , Figure 5 As shown: Assembly component C represents a standardized reactor in installation state C (the same applies to other assembly components with different numbers):

[0051] ① The fluid enters the assembly component C tangentially from the lower fluid port 9, causing the fluid to form a clockwise tangential rotating circulation in the lower part of the assembly component C. Under the continuous inflow of the total inflow 15, the fluid gradually rises in a clockwise rotating circulation until it flows to the upper part of the assembly component C.

[0052] ②During the entire clockwise rotational circulation process, flow layer A is always the flow layer that is close to the outer shell of the standardized reactor 1, and flow layer B is always the flow layer that is close to the contact catalytic interface component 2. During the process, the fluid reaction in flow layer B is more complete.

[0053] ③ The fluid further flows to the upper fluid port 8 of the assembly component D and enters the assembly component D tangentially, so that the incoming fluid forms a counterclockwise tangential rotating circulation in the upper part of the assembly component D. Under the continuous impetus of the incoming flow, it gradually descends in a counterclockwise rotating circulation until it flows to the lower part of the assembly component D, flows out from the lower fluid port 9 and enters the next assembly component standard reactor, and so on, in the form of rotating circulation, flowing through all the standard reactors to fully react;

[0054] ④ As shown in ①, ②, and ③, and in conjunction with the diagram, the fluid flows to the upper fluid port 8 of assembly component C in a clockwise rotating circulation pattern. Flow layer A is the outer fluid layer and the reaction is not sufficient, while flow layer B is the inner fluid layer and the reaction is more complete. When the fluid flows from assembly component C to assembly component D, its flow pattern changes from a clockwise rotating circulation pattern to a counterclockwise rotating circulation pattern. In assembly component D, flow layer A becomes the inner flow layer close to the contact catalytic interface component 2 and the reaction is more complete, while flow layer B becomes the outer flow layer close to the shell 1 of the standardized reactor and the reaction is not sufficient. And so on. When the fluid flows through different standardized reactors, the properties of the inner and outer flow layers of flow layers A and B continuously alternate, and the two alternately achieve close contact with the contact catalytic interface component 2, achieving a stronger alternating mixing effect and contact mass transfer reaction efficiency.

[0055] ⑤ By gradually rising / falling through the rotating circulation, the path of the fluid flowing through the cavity between the standardized reactor shell 1 and the contact catalytic interface component 2 is further lengthened, the contact time and frequency between the fluid and the contact catalytic interface component 2 are further increased, and the circulation stirring mass transfer effect is enhanced, making the reaction more complete and efficient.

[0056] ⑥ The front end of the main inlet 15 is connected to a high-pressure conveying device. By adjusting the outflow of the high-pressure conveying device, the flow rate of the main inlet 15 can be effectively controlled, thereby controlling the flow rate of the rotating circulation inside the standardized reactor. The higher the flow rate, the more times the rotating circulation passes through, the longer the flow path, and the higher the mixing mass transfer effect, resulting in a better reaction effect. However, in order to balance the reaction effect and energy consumption, the forced conveying flow rate is generally controlled at 2~5m / s.

[0057] Note 3: For example Figure 2 , Figure 6In the transition connection at the corner, reactor shells of types T2 to T5 are required, while all other intermediate shells use type T1. Specifically, the flow from assembly component E to assembly component F requires the use of type T2 and type T3 reactor shells to achieve fluid flow pattern and path conversion, and the flow from assembly component G to assembly component H requires the use of type T4 and type T5 reactor shells to achieve fluid flow pattern and path conversion. After all connections are completed and assembled, an equilateral triangular assembly matrix is ​​formed. The matrix can be large or small, and the number of rows / columns can be increased or decreased. It can be flexibly connected in series, or a standardized reactor can be used separately according to the actual application scenario, or different assembly matrices can be used in parallel. The assembly space utilization rate is high, and the adjustment flexibility is high.

[0058] The advantages of this invention are:

[0059] 1. Forced rotating circulation reaction has high contact mass transfer efficiency, good reaction effect, improves the space utilization of the reactor body, and realizes the compact and simple design of the reactor.

[0060] 2. The rotating circulation between different reactors achieves alternating forms of internal and external laminar flow and upper and lower baffle flow, further extending the reaction flow path, improving the mixing and contact mass transfer effect, making the reaction more complete, thorough and uniform, and further improving the overall reaction effect while saving reactor volume.

[0061] 3. By using a relatively small number (3-5 types) of standardized reactor shell designs, a triangular matrix-style batch connection arrangement of reactors can be successfully achieved. The reactors can be connected in parallel or in series, and the number is adjustable, which improves the flexibility, versatility, and space utilization efficiency of the overall reactor assembly. At the same time, it also enhances the convenience of batch, process-oriented, and intelligent design and manufacturing of standardized reactors, making it easier for them to be applied in large-scale engineering projects.

[0062] 4. The contact catalytic interface components can be electrode catalytic components, strong photocatalytic oxidation components, specially made transition metal coated surface catalytic components, biological packing carrier components, surface adsorption components, etc.; correspondingly, special functional modules can be integrated and selected according to the actual use scenario requirements of the reactor. The reactor shell can also be made of insulating engineering plastics or conductive metal materials, and can be selectively equipped with grounding electrodes or negative electrodes, so that it can be fully adapted to different reactors and reaction processes, greatly improving the application scenarios of the reactor.

[0063] 5. The power for the forced rotating circulation comes from a powerful conveying mechanical device. The pressure and flow rate of the rotating circulation are adjustable, making the reaction process more controllable.

[0064] 6. The vertical matrix reactor layout features a standardized integrated design for the core contact catalytic interface components, with a lifting ring at the top. The overall design is simple and easy to use, facilitating manufacturing, installation, and maintenance during operation.

[0065] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A forced hydrocyclone array reactor, characterized in that, include: Multiple standardized reactor shells; Multiple standardized reactor shells are vertically arranged and connected in series or in parallel to enable fluid to flow between the standardized reactor shells in a series or parallel manner. Each standardized reactor shell contains a coaxial contact catalytic interface assembly, and an annular cavity is formed between the standardized reactor shell and the contact catalytic interface assembly. Each standardized reactor shell has an upper fluid port and a lower fluid port on its outer side. The axes of the upper and lower fluid ports are parallel to the tangent of the inner concentric circle of the standardized reactor shell, so as to achieve a rotating flow state of the fluid inside the standardized reactor shell. The axes of the upper and lower fluid ports represent the fluid flow direction, and the tangent of the inner concentric circle of the standardized reactor shell represents the internal fluid flow direction of the standardized reactor shell. The fluid enters the first standardized reactor through its lower fluid port. It flows from the bottom of the reactor through the cavity between the reactor shell and the contact catalytic interface component, gradually rising in a clockwise rotational circulation within the cavity. After reacting, it flows upward to the upper fluid port of the first standardized reactor and exits. The upper fluid port of the first standardized reactor connects to the upper fluid port of the second standardized reactor, from which the fluid enters. It then flows from the top of the second standardized reactor through the cavity between the reactor shell and the contact catalytic interface component, gradually descending in a counter-clockwise rotational circulation within the cavity. After reacting, it flows downward to the lower fluid port of the second standardized reactor and exits. The lower fluid port of the second standardized reactor connects to the lower fluid port of the third standardized reactor, from which the fluid enters. This process continues, with the fluid moving up and down, following the longest path through the cavities between the reactor shells and the contact catalytic interface component of all standardized reactors, ensuring complete reaction, until it reaches the final discharge port and is discharged in compliance with regulations.

2. The forced hydrocyclone array reactor as described in claim 1, characterized in that, Also includes: A sealing top cover; the sealing top cover is located on the upper part of the standardized reactor shell and is used for pressure sealing of the standardized reactor shell. The sealing top cover has a central circular hole. The contact catalytic interface assembly passes through the central circular hole of the sealing top cover and is vertically installed inside the shell along the axis of the standardized reactor shell. The gap between the sealing top cover and the contact catalytic interface assembly is filled with a sealing plug.

3. The forced hydrocyclone array reactor as described in claim 1, characterized in that, Multiple standardized reactor shells are arranged in a triangular matrix in a batch.

4. The forced hydrocyclone array reactor as described in claim 1 or 3, characterized in that, Based on the different angles between the axes of the upper and lower fluid ports of the standardized reactor shell and the radial line from the center of the standardized reactor shell to the center point of the port inlet, the standardized reactor shell is divided into T1 to T5 types of reactor shells.

5. The forced hydrocyclone array reactor as described in claim 4, characterized in that, The T1 type reactor shell is characterized by the following: the angle between the axis of the lower fluid port and the radial line of the lower fluid port is 30° or 52°, the angle between the axis of the upper fluid port and the radial line of the upper fluid port is 30° or 52°, and the angle between the radial line of the lower fluid port and the radial line of the upper fluid port is 120° or 76°; the T2 and T5 type reactor shells are characterized by the following: the angle between the axis of the lower fluid port and the radial line of the lower fluid port is 65°, the angle between the axis of the upper fluid port and the radial line of the upper fluid port is 30°, and the angle between the radial line of the lower fluid port and the radial line of the upper fluid port is 150°; the T3 and T4 type reactor shells are characterized by the following: the angle between the axis of the lower fluid port and the radial line of the lower fluid port is 65°, the angle between the axis of the upper fluid port and the radial line of the upper fluid port is 30°, and the angle between the radial line of the lower fluid port and the radial line of the upper fluid port is 30°.

6. The forced hydrocyclone array reactor as described in claim 1 or 3, characterized in that, The upper fluid ports of the different standardized reactor shells are connected to each other, and the lower fluid ports are connected to each other, so as to realize the matrix-style series connection or parallel connection of the standardized reactor shells.

7. The forced hydrocyclone array reactor as described in claim 6, characterized in that, The standardized reactor shell, which is connected in a matrix and series, is mounted on the base frame and is fixed by an auxiliary fixing frame in the middle and upper part.

8. The forced hydrocyclone array reactor as described in claim 1, characterized in that, The fluid includes the gas or liquid to be reacted, and the contact catalytic interface components include an electrode catalytic component, a strong photocatalytic oxidation component, a specially made transition metal coating surface catalytic component, a biological filler carrier component, and a surface adsorption component.

9. The forced hydrocyclone array reactor as described in claim 1, characterized in that, The upper part of the contact catalytic interface component is also connected to a stabilizing head for connecting and fixing the contact catalytic interface component. The upper part of the stabilizing head is also provided with a lifting ring. According to the actual use scenario requirements of the reactor, the stabilizing head is also configured with a special function module, which includes a smart electronic control end component and an anode generator. The smart electronic control end component or the anode generator is connected to the power supply through a connecting cable. A grounding electrode or a negative electrode is installed on the standardized reactor shell.

10. The forced hydrocyclone array reactor as described in claim 1, characterized in that, The upper fluid port and the lower fluid port are also connected to auxiliary additive port branches on their inlet pipes.

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