Pole core rotatable type advanced oxidation electrolytic bath

Abstract

The invention provides an advanced oxidation electrolytic cell with rotatable pole cores, which comprises an exhaust sealing end plate, an electrolytic cell shell and a water inlet sealing end plate from top to bottom, the electrolytic cell shell is of a cylindrical structure, an anode pole core and a cathode pole core are arranged in the electrolytic cell shell, and the length of the electrolytic cell shell is greater than that of the anode pole core and that of the cathode pole core; the anode pole core comprises an anode plate with a multi-layer plate structure, the cathode pole core comprises a cathode plate with a multi-layer plate structure, and at least part of the anode plate and the cathode plate are assembled to form advanced oxidation reaction areas at equal intervals. The microporous screen holes are formed in the positive and negative plate supporting plates, so that inlet water is effectively and uniformly mixed, water drops in discharged gas are filtered by the screen, and the gas-water separation efficiency is improved. The unique design of the cathode and anode cores optimizes the gas-liquid flow state in the reactor, improves the dispersion speed of bubbles on the surface of the polar plate, improves the mixing efficiency of fluid in the electrolytic cell, improves the overall reaction efficiency of the system, and reduces the energy consumption and equipment cost of the system.

Description

Technical Field

[0001] This invention relates to the fields of electrochemical advanced oxidation and environmental remediation, and more specifically, to an advanced oxidation electrolyzer with a rotatable electrode core. Background Technology

[0002] Most existing advanced oxidation reactors (AEs) are flow-through plate electrolyzers with a predominantly laminar internal water flow. AEs primarily rely on the oxidation of pollutants by hydroxyl radicals, which have a very short lifespan (nanoseconds). This means that pollutant removal occurs mainly near the electrode reaction zone, and the laminar flow reactors currently struggle to achieve optimal mixing, resulting in low pollutant removal efficiency. Secondly, AEs generate large amounts of gas during the reaction, leaving significant gas on the electrode surfaces. The laminar flow hinders gas diffusion, drastically reducing the active reaction zone area and increasing mass transfer resistance. This further reduces pollutant removal efficiency and increases system energy consumption. Furthermore, current electrolyzers typically employ separate designs for the electrolyzer and gas-liquid separator. The gas-liquid mixture after the electrolyzer reaction requires further separation, increasing equipment costs and system footprint, and making the AE process more complex.

[0003] In summary, current advanced oxidation electrolyzers have the following disadvantages:

[0004] (1) The liquid flow in the electrolytic cell reactor is laminar, the pollutants and hydroxyl radicals do not mix well, the reaction effect is poor, and the pollutant removal efficiency is low.

[0005] (2) Advanced oxidation reactions will generate a large amount of gas in the reaction zone on the electrode surface. The laminar liquid flow is not conducive to the diffusion of a large amount of gas, which leads to a significant increase in the mass transfer resistance between the electrodes, greatly increasing the energy consumption of the electrolytic cell, increasing the operating cost of the system, and reducing the reaction efficiency.

[0006] (3) The advanced oxidation system currently adopts the form of separate construction of electrolytic cell and gas-water separator, which increases equipment cost and system footprint, making the overall system more complex and maintenance cost will also increase. Summary of the Invention

[0007] In view of this, the present invention aims to propose an advanced oxidation electrolyzer with a rotatable core to solve the problems of low pollutant removal efficiency and unfavorable gas diffusion in the prior art of advanced oxidation reactors.

[0008] To achieve the above objectives, the technical solution of the present invention is implemented as follows:

[0009] A rotatable electrode core advanced oxidation electrolyzer includes, from top to bottom, an exhaust sealing end plate, an electrolyzer shell, and a water inlet sealing end plate. The electrolyzer shell is cylindrical, and an anode core and a cathode core are installed inside. The length of the electrolyzer shell is greater than the lengths of the anode core and cathode core. The anode core includes a multi-layered anode plate, and the cathode core includes a multi-layered cathode plate. At least a portion of the anode plate is assembled with the cathode plate to form equally spaced advanced oxidation reaction zones. This optimizes the gas-liquid flow pattern within the reactor, increases the dispersion rate of bubbles on the electrode surface, and improves the mixing efficiency of the fluid within the electrolyzer. It integrates the advanced oxidation reaction and gas-liquid separation into a single reactor, improving the overall system reaction efficiency while reducing system energy consumption and equipment costs.

[0010] Furthermore, the anode plate includes an anode plate-shaped area and an anode sieve plate area. The anode plate-shaped area is configured as an arc-shaped plate structure with a complete plate surface, and the anode sieve plate area is configured as a sieve plate structure. The cathode plate includes a cathode plate-shaped area and a cathode sieve plate area. The cathode plate-shaped area is configured as an arc-shaped plate structure with a complete plate surface, and the cathode sieve plate area is configured as a sieve plate structure. The cathode sieve plate area and the anode sieve plate area are staggered.

[0011] Furthermore, the outer shell of the electrolytic cell includes a sealing structure, an electrolytic cell cylinder, and an inlet and an outlet disposed on the electrolytic cell cylinder. The electrolytic cell cylinder is configured as a cylindrical structure, and sealing structures are provided at both the upper and lower parts of the electrolytic cell cylinder. The inlet and outlet are disposed on the side wall of the electrolytic cell cylinder, with the inlet located near the lower part and the outlet located near the upper part.

[0012] Furthermore, the eccentricity directions of the inlet and outlet should be opposite.

[0013] Furthermore, the anode core includes an anode sealing conductive pad, a conductive anode bearing, an anode plate support plate, and an anode plate. The anode plate support plate is disposed on the top of the anode plate and rotates integrally with the anode plate. The conductive anode bearing is disposed radially around the anode plate, and an annular anode sealing conductive pad is disposed on the outside of the conductive anode bearing, the anode sealing conductive pad enclosing the conductive anode bearing.

[0014] Furthermore, an anode contact plate is also connected to the radial side of the anode sealing conductive pad for electrically connecting the anode plate.

[0015] Furthermore, an anode blade is provided around the outermost anode plate, and the anode blade protrudes and extends away from the axis.

[0016] Furthermore, the cathode core includes a cathode sealing conductive pad, a conductive cathode bearing, a cathode plate support plate, and a cathode plate. The cathode plate support plate is disposed on the top of the cathode plate and rotates integrally with the cathode plate. The conductive cathode bearing is disposed radially around the cathode plate, and an annular cathode sealing conductive pad is disposed on the outside of the conductive cathode bearing, the cathode sealing conductive pad enclosing the conductive cathode bearing.

[0017] Furthermore, a cathode contact plate is also connected to the radial side of the cathode sealing conductive pad for electrically connecting the cathode plate.

[0018] Furthermore, cathode blades are provided around the outermost cathode plate, and the cathode blades extend in a direction away from the axis.

[0019] Compared with existing technologies, the rotatable electrode core advanced oxidation electrolyzer of the present invention has the following advantages:

[0020] The liquid flow in the electrolytic cell reactor is turbulent, resulting in excellent mixing of pollutants and hydroxyl radicals, high reaction efficiency, and high pollutant removal efficiency.

[0021] The rotating design of the electrode core inside the reactor creates a highly turbulent liquid flow state, which is very conducive to the diffusion of a large amount of gas. This greatly reduces the mass transfer resistance between the electrode plates, significantly reduces the energy consumption of the electrolytic cell, greatly reduces the operating cost of the system, and at the same time greatly improves the reaction efficiency.

[0022] This advanced oxidation process combines an electrolytic cell with a gas-liquid separator, which greatly reduces equipment costs and system footprint, making the overall system process more streamlined and maintenance costs significantly reduced. Attached Figure Description

[0023] Figure 1 This is an axial view of the electrolytic cell assembly according to the present invention;

[0024] Figure 1a This is a front view of the electrolytic cell assembly according to the present invention;

[0025] Figure 2 This is an exploded axial view of the electrolytic cell described in this invention;

[0026] Figure 2a This is an exploded front view of the electrolytic cell described in this invention;

[0027] Figure 2b This is an exploded view of the electrolytic cell described in this invention.

[0028] Figure 3 This is a schematic diagram of the electrode plate assembly design according to the present invention;

[0029] Figure 3afor Figure 3 Sectional view of AA;

[0030] Figure 3b for Figure 3a A magnified view of the selected area;

[0031] Figure 4 This is a schematic diagram of the operation of the advanced oxidation electrolyzer according to Embodiment 1 of the present invention;

[0032] Figure 5 This is a schematic diagram of the operation of the advanced oxidation electrolytic cell in Embodiment 2 of the present invention;

[0033] Figure 6 This is a schematic diagram of the operation of the advanced oxidation electrolytic cell in Embodiment 3 of the present invention.

[0034] Explanation of reference numerals in the attached figures:

[0035] 1-Electrolytic cell outer shell, 101-Sealing structure, 102-Electrolytic cell cylinder, 103-Water inlet, 104-Water outlet, 2-Anode core, 201-Anode sealing conductive pad, 202-Conductive anode bearing, 203-Anode plate support plate, 204-Anode plate, 204a-Anode plate area, 204b-Anode sieve plate area, 205-Anode contact plate, 206-Anode blade, 21-Raw water inlet main pipe, 22-Raw water side inlet pipe, 23 - Bottom water inlet pipe, 24- Drainage pipe, 25- Exhaust pipe, 3- Cathode core, 301- Cathode sealing conductive pad, 302- Conductive cathode bearing, 303- Cathode plate support plate, 304- Cathode plate, 304a- Cathode plate area, 304b- Cathode sieve plate area, 305- Cathode contact plate, 306- Cathode blade, 4- Water inlet sealing end plate, 41- Lower water inlet, 5- Exhaust sealing end plate, 51- Exhaust port, 6- Return water booster device. Detailed Implementation

[0036] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings.

[0037] like Figures 1-4 As shown, an advanced oxidation electrolytic cell structure includes, from top to bottom, an exhaust sealing end plate 5, an electrolytic cell shell 1, and a water inlet sealing end plate 4. The electrolytic cell shell 1 is configured as a cylindrical structure. An anode core 2 and a cathode core 3 are installed inside the electrolytic cell shell 1. The length of the electrolytic cell shell 1 is greater than the length of the anode core 2 and the cathode core 3, so that the anode reaction and the cathode reaction take place inside the electrolytic cell shell 1.

[0038] The material of the outer shell 1 of the electrolytic cell can be set to various metal and non-metal materials, as long as it can meet the strength requirements of the reactor operation; the anode core 2 includes, but is not limited to, anodes suitable for various advanced oxidation reactors; the cathode core 3 includes, but is not limited to, cathodes suitable for various advanced oxidation reactors; the water inlet sealing end plate 4 and the exhaust sealing end plate 5 can be various surface sealing structures such as flanges, and this application illustrates the flange sealing form.

[0039] The outer shell 1 of the electrolytic cell includes a sealing structure 101, an electrolytic cell cylinder 102, and an inlet 103 and an outlet 104 disposed on the electrolytic cell cylinder 102. The electrolytic cell cylinder 102 is a cylindrical structure, and sealing structures 101 are provided at both the upper and lower parts of the electrolytic cell cylinder 102. The sealing structures 101 can be flanges or other various surface sealing structures. The inlet 103 and the outlet 104 are disposed on the side wall of the electrolytic cell cylinder 102, with the inlet 103 located near the lower part, allowing water to enter the electrolytic cell cylinder 102 from an eccentric side, and the outlet 104 located near the upper part, allowing water to exit the electrolytic cell cylinder 102 from an eccentric side. Preferably, the eccentric directions of the inlet 103 and the outlet 104 should be opposite. In this embodiment, the material of the electrolytic cell cylinder 102 can be various metals or non-metals, as long as the strength is sufficient to meet the operating requirements of the reactor.

[0040] The length of the anode core 2 is less than the length of the electrolytic cell outer shell 1. Specifically, the anode core 2 includes an anode sealing conductive pad 201, a conductive anode bearing 202, an anode plate support plate 203, and an anode plate 204. The anode plate 204 is configured as a multi-layer plate structure, with the multi-layer plates forming a concentric cylindrical structure. At least a portion of the anode plate 204 can be assembled with the cathode plate 304 to form equally spaced advanced oxidation reaction zones. Furthermore, the surface of the anode plate 204 can be of two forms: a complete plate surface or a mesh-like structure with uniformly arranged micropores. The anode plate support plate 203 is located on top of the anode plate 204 and rotates integrally with the anode plate 204. A conductive anode bearing 202 is disposed radially around the anode plate 204. An annular anode sealing conductive pad 201 is disposed on the outer side of the conductive anode bearing 202, enclosing the conductive anode bearing 202 and sealing the top of the anode plate 204. The conductive anode bearing 202 connects the rotating anode support plate 203 to the fixed anode sealing conductive pad 201. Furthermore, an anode contact piece 205 is connected to the radial side of the anode sealing conductive pad 201 for electrical connection to the anode plate 204. An anode blade 206 is disposed around the outermost anode plate 204, protruding away from the axis to facilitate rotation of the anode plate 204 under the action of water flow.

[0041] Furthermore, the anode plate 204 includes an anode plate-shaped region 204a and an anode sieve plate region 204b. The anode plate-shaped region 204a is configured as an arc-shaped plate structure with a complete plate surface. The anode sieve plate region 204b is provided with uniformly distributed micropores, forming a sieve plate structure. The anode plate-shaped region 204a is located near the front side, and the anode sieve plate region 204b is located near the rear side.

[0042] In this embodiment, the anode sealing conductive pad 201 is made of metal and can be any conductive gasket that meets the sealing performance requirements, as long as its thickness and size meet the design requirements. Preferably, the anode contact plate 205 and the metal anode sealing conductive pad 201 are designed as a single unit, including but not limited to casting, welding, and other connection methods. The conductive anode bearing 202 includes but is not limited to various bearings with excellent rotational performance, corrosion resistance, and excellent conductivity. The anode plate support plate 203 is configured with a microporous structure to discharge the gas inside the electrolytic cell to the outside through the exhaust sealing end plate. The micropores on the anode plate support plate 203 are basically uniformly distributed and have good conductivity. The anode plate 204 contains a catalyst coating suitable for advanced oxidation reactions.

[0043] The length of the cathode core 3 is less than the length of the electrolytic cell outer shell 1. Specifically, the cathode core 3 includes a cathode sealing conductive pad 301, a conductive cathode bearing 302, a cathode plate support plate 303, and a cathode plate 304. The cathode plate 304 is configured as a multi-layer plate structure, with the multi-layer plates forming a concentric cylindrical structure. The cathode plate 304 is adapted for advanced oxidation reactions, and at least a portion of the cathode plate 304 can be assembled with the anode plate 204 to form equally spaced advanced oxidation reaction zones. Furthermore, the surface of the cathode plate 304 can be of two forms: a complete plate surface or a mesh-like structure with uniformly arranged micropores. The cathode plate support plate 303 is located on top of the cathode plate 304 and rotates integrally with the cathode plate 304. A conductive cathode bearing 302 is disposed radially around the cathode plate 304. An annular cathode sealing conductive pad 301 is disposed on the outer side of the conductive cathode bearing 302, enclosing the conductive cathode bearing 302 and sealing the top of the cathode plate 304. The conductive cathode bearing 302 connects the rotating cathode plate support plate 303 to the fixed cathode sealing conductive pad 301. Furthermore, a cathode contact plate 305 is connected to the radial side of the cathode sealing conductive pad 301 for electrical connection to the cathode plate 304. A cathode blade 306 is disposed around the outermost cathode plate 304, protruding away from the axis to facilitate rotation of the cathode plate 304 under the action of water flow. The cathode plate with the cathode blade 306 has a different outer diameter than the anode plate with the anode blade 206, allowing the cathode and anode plates to generate different linear velocities, thus causing relative rotation between them.

[0044] Furthermore, the cathode plate 304 includes a cathode plate-shaped region 304a and a cathode sieve plate region 304b. The cathode plate-shaped region 304a is configured as an arc-shaped plate structure with a complete plate surface. The cathode sieve plate region 304b is provided with uniformly distributed micropores, forming a sieve plate structure. The cathode plate-shaped region 304a is located near the rear side, and the cathode sieve plate region 304b is located near the front side. The cathode sieve plate region 304b is staggered from the anode sieve plate region 204b to increase the turbulence effect within the reaction zone.

[0045] In this embodiment, the cathode sealing conductive pad 301 is made of metal and can be any conductive gasket that meets the sealing performance requirements, as long as its thickness and size meet the design requirements. Preferably, the cathode contact plate 305 and the metal cathode sealing conductive pad 301 are designed as a single unit, including but not limited to integral molding by casting, welding, or other connection methods. The conductive cathode bearing 302 includes, but is not limited to, various bearings with excellent rotational performance, corrosion resistance, and excellent conductivity. The cathode plate support plate 303 is configured with a microporous structure, allowing water entering through the inlet to pass through the cathode plate support plate 303 into the electrolytic cell. The micropores on the cathode plate support plate 303 are basically uniformly arranged, providing good conductivity.

[0046] As one embodiment of the present invention, an advanced oxidation electrolyzer operation process is also provided, as follows:

[0047] (1) Water inlet: Wastewater enters the advanced oxidation electrolytic cell through the water inlet on the water inlet sealing end plate 4 and the water inlet 103 on the electrolytic cell shell 1.

[0048] ① Water enters through the lower inlet 41 on the water inlet sealing end plate 4, serving as the raw water that mainly participates in the electrolysis reaction. The water enters the electrolytic cell electrode reaction zone through the micropores on the cathode plate support plate 303 on the cathode core 3. The electrode micropores serve two purposes: first, they enhance flow resistance, reduce the raw water inlet flow rate, prolong the reaction residence time of the raw water in the reactor, and improve reaction efficiency; second, they enhance mixing, ensuring uniform mixing of the raw water inlet and improving the reaction and removal effect of pollutants.

[0049] ② The water inlet 103 on the outer shell 1 of the electrolytic cell mainly provides the rotational power for the electrolytic cell cores, causing the anode plate 204 and cathode plate 304 to rotate under the tangential force of the eccentric water flow. Specifically, the outer diameters of the anode and cathode plates with rotating blades on the anode and cathode cores are different, resulting in different linear velocities under the same tangential force of the water flow. Consequently, the anode core 2 and cathode core 3 will rotate relative to each other, increasing the turbulence between the anode and cathode plates. Simultaneously, the tangentially fed water can also enter the reaction zone of the anode and cathode plates through the sieve holes on the anode and cathode cores to participate in the electrolysis reaction.

[0050] (2) During the electrolysis reaction, the anode and cathode cores rotate under the tangential water inlet. Due to their different rotation speeds, they rotate relative to each other. During this rotation, the cylindrical electrode generates centrifugal force, causing a large number of bubbles generated on the surface to dissipate and separate rapidly. Furthermore, the relative rotation of the anode and cathode plates further increases the turbulence of the wastewater in the reaction zone, enhancing the bubble dissipation and separation effect. Moreover, the same anode and cathode plate is divided into two regions: a plate region and a sieve plate region. Under the rotation, the sieve holes in the sieve plate region also generate turbulence around the sieve holes, which greatly enhances the bubble dissipation and separation effect. The enhanced bubble dissipation and separation effect effectively reduces the mass transfer resistance between the anode and cathode plates, effectively reducing reaction energy consumption and operating costs. With the enhanced turbulence in the plate region, the mixing state and contact opportunities of hydroxyl radicals generated by advanced oxidation with pollutants are greatly enhanced, significantly improving the pollutant removal effect. Furthermore, with the enhanced bubble dissipation and separation effect on the plate surface, the reactive area on the plate surface is effectively guaranteed, thus ensuring that the amount of hydroxyl radicals generated is not affected.

[0051] (3) Drainage and exhaust: The wastewater after the reaction is discharged through the outlet 104 on the outer shell 1 of the electrolytic cell. The outlet is located below the exhaust sealing end plate 5, so the area between the outlet and the exhaust sealing end plate 5 is the gas discharge zone. Moreover, under the action of the rotating blades of the top electrode core, the gas will rotate, and the centrifugal force generated by the rotation will make the gas and liquid droplets more thoroughly separated, improving the gas-liquid separation effect. In addition, the gas is discharged through the micropores on the electrode support plate of the top electrode core. The micropores can also filter water droplets, enhancing the gas-liquid separation effect. Furthermore, the micropores will increase the flow resistance of gas discharge, ensuring that the gas flow rate is maintained within a safe range during gas discharge, ensuring the safety of the exhaust process. The electrolytic cell design of this invention combines the functions of an advanced oxidation reactor and a gas-liquid separator, saving equipment investment and system footprint, simplifying the system process, and effectively reducing system costs.

[0052] Example 1

[0053] In this embodiment, the operation process of the advanced oxidation electrolyzer is as follows:

[0054] (1) Water inlet: In this embodiment, the raw water inlet main pipeline 21 is divided into two water inlet branches: the raw water side water inlet pipeline 22 and the raw water bottom water inlet pipeline 23. A portion of the raw water in the raw water bottom water inlet pipeline 23 enters the advanced oxidation electrolysis cell through the water inlet on the water inlet sealing end plate 4, and a portion of the raw water in the raw water side water inlet pipeline 22 enters the advanced oxidation electrolysis cell through the water inlet 103 on the electrolysis cell shell 1.

[0055] ① The water inlet on the inlet sealing end plate 4 serves as the raw water that mainly participates in the electrolysis reaction. The water enters the electrolytic cell electrode reaction zone through the micropores on the electrode support plate on the electrode core. The micropores on the electrode plate play two roles: first, they enhance flow resistance, reduce the flow rate of the raw water, prolong the reaction residence time of the raw water in the reactor, and improve the reaction efficiency; second, they enhance mixing, ensure that the raw water is mixed evenly, and improve the reaction and removal effect of pollutants.

[0056] ② The water inlet 103 on the outer shell 1 of the electrolytic cell mainly provides the rotational power for the electrolytic cell cores, causing the anode and cathode to rotate under the tangential force of the eccentric water flow. Specifically, the outer diameters of the plates with rotating blades on the anode and cathode cores are different, resulting in different linear velocities under the same tangential force of the water flow. This causes relative rotation between the anode and cathode cores, increasing the turbulence between the plates. Simultaneously, the tangentially fed water can also enter the reaction zone of the anode and cathode plates through the sieve holes on the anode and cathode cores to participate in the electrolysis reaction.

[0057] (2) During the electrolysis reaction, the anode and cathode cores rotate under the tangential water inlet. Due to their different rotation speeds, they rotate relative to each other. During this rotation, the cylindrical electrode generates centrifugal force, causing a large number of bubbles generated on the surface to dissipate and separate rapidly. Furthermore, the relative rotation of the anode and cathode plates further increases the turbulence of the wastewater in the reaction zone, enhancing the bubble dissipation and separation effect. Moreover, the same anode and cathode plate is divided into two regions: a plate region and a sieve plate region. Under the rotation, the sieve holes in the sieve plate region also generate turbulence around the sieve holes, which greatly enhances the bubble dissipation and separation effect. The enhanced bubble dissipation and separation effect effectively reduces the mass transfer resistance between the anode and cathode plates, effectively reducing reaction energy consumption and operating costs. With the enhanced turbulence in the plate region, the mixing state and contact opportunities of hydroxyl radicals generated by advanced oxidation with pollutants are greatly enhanced, significantly improving the pollutant removal effect. Furthermore, with the enhanced bubble dissipation and separation effect on the plate surface, the reactive area on the plate surface is effectively guaranteed, thus ensuring that the amount of hydroxyl radicals generated is not affected.

[0058] (3) Drainage and exhaust: The wastewater after the reaction is discharged through the outlet 104 on the outer shell 1 of the electrolytic cell and then discharged to the subsequent treatment process through the drainage pipe 24. The drain outlet is located below the exhaust sealing end plate 5, so the area between the drain outlet and the exhaust sealing end plate 5 is the gas emission area. Moreover, under the action of the rotating blades of the top electrode core, the gas will be driven to rotate, and the centrifugal force generated by the rotation will make the gas and liquid droplets more thoroughly separated, improving the gas-liquid separation effect. In addition, the gas is discharged through the micropores on the electrode plate support plate on the top electrode core, and then discharged to the subsequent process through the exhaust pipe 25. The micropores on the electrode plate support plate can also filter water droplets, enhance the gas-liquid separation effect, and the micropores will increase the flow resistance of gas discharge, ensuring that the gas flow rate is maintained within a safe range during gas discharge, and ensuring the safety of the exhaust process. The electrolytic cell design of this invention combines the functions of an advanced oxidation reactor and a gas-liquid separator, saving equipment investment and system footprint, simplifying the system process, and effectively reducing system costs.

[0059] Example 2

[0060] In this embodiment, the operation process of the advanced oxidation electrolyzer is as follows:

[0061] (1) Water inlet and return: In this embodiment, the raw water enters the advanced oxidation electrolysis cell through the water inlet main pipe 31 and the water inlet on the water inlet sealing end plate 4. A portion of the treated water after reaction enters the advanced oxidation electrolysis cell through the water return pipe 34 and the water inlet 103 on the electrolysis cell shell 1.

[0062] ① The water inlet on the inlet sealing end plate 4 serves as the raw water that mainly participates in the electrolysis reaction. The water enters the electrolytic cell electrode reaction zone through the micropores on the electrode support plate on the electrode core. The micropores on the electrode plate play two roles: first, they enhance flow resistance, reduce the flow rate of the raw water, prolong the reaction residence time of the raw water in the reactor, and improve the reaction efficiency; second, they enhance mixing, ensure that the raw water is mixed evenly, and improve the reaction and removal effect of pollutants.

[0063] ② The water inlet 103 on the outer shell 1 of the electrolytic cell mainly provides the rotational power for the electrolytic cell cores, causing the anode and cathode to rotate under the tangential force of the eccentric water flow. Specifically, the outer diameters of the plates with rotating blades on the anode and cathode cores are different, resulting in different linear velocities under the same tangential force of the water flow. This causes relative rotation between the anode and cathode cores, increasing the turbulence between the plates. Simultaneously, the tangentially fed water can also enter the reaction zone of the anode and cathode plates through the sieve holes on the anode and cathode cores to participate in the electrolysis reaction.

[0064] During the electrolysis reaction, the anode and cathode cores rotate under the tangential inflow of water. Due to their different rotational speeds, they rotate relative to each other. This rotation generates centrifugal force in the cylindrical electrodes, causing numerous bubbles on the surface to dissipate rapidly. Furthermore, the relative rotation of the anode and cathode plates increases the turbulence in the wastewater within the reaction zone, enhancing bubble dissipation and separation. Moreover, each anode and cathode plate is divided into two regions: a plate region and a sieve plate region. The rotation of the sieve plate region also generates turbulence around the sieve openings, significantly enhancing bubble dissipation and separation. This enhanced bubble dissipation and separation effectively reduces the mass transfer resistance between the anode and cathode plates, thus reducing reaction energy consumption and operating costs. The increased turbulence within the plate region significantly enhances the mixing and contact opportunities between hydroxyl radicals generated by advanced oxidation and contaminants, noticeably improving the removal of pollutants. Furthermore, the enhanced bubble dissipation and separation on the plate surface effectively preserves the reactive zone on the plate surface, ensuring that the amount of hydroxyl radicals generated remains unaffected.

[0065] (3) Drainage and exhaust: The wastewater after the reaction is discharged through the outlet 104 on the outer shell 1 of the electrolytic cell. The main drainage pipe 32 is divided into two branches: a drainage branch pipe 33 and a return water pipe 34. Among them, part of the treated water after the reaction is discharged to the subsequent treatment process through the drainage branch pipe 33, and the other part of the treated water is returned through the return water pipe 34 to provide rotational power for the rotation of the electrolytic cell electrode core. The drain outlet is located below the exhaust sealing end plate 5, so the area between the drain outlet and the exhaust sealing end plate 5 is the gas emission area. Moreover, under the action of the rotating blades of the top electrode core, the gas will be driven to rotate, and the centrifugal force generated by the rotation will make the gas and liquid droplets more thoroughly separated, improving the gas-liquid separation effect. In addition, the gas is discharged through the micropores on the electrode plate support plate on the top electrode core, and then discharged to the subsequent process through the exhaust pipe 35. The micropores on the electrode plate support plate can also filter water droplets, enhance the gas-liquid separation effect, and the micropores will increase the flow resistance of gas emission, ensuring that the gas flow rate is maintained within a safe range during gas emission, and ensuring the safety of the exhaust process. The electrolytic cell design of this invention combines the functions of an advanced oxidation reactor and a gas-liquid separator, saving equipment investment and system footprint, simplifying the system process, and effectively reducing system costs.

[0066] Example 3

[0067] In this embodiment, the operation process of the advanced oxidation electrolyzer is as follows:

[0068] (1) Water inlet and return: In this embodiment, raw water enters the advanced oxidation electrolytic cell through the water inlet main pipe 41 and the water inlet on the water inlet sealing end plate 4. A portion of the treated water after reaction enters the advanced oxidation electrolytic cell through the water return pipe 42 and the water inlet 103 on the electrolytic cell shell 1. The water return pipe 42 is equipped with a water return booster device 6 (including but not limited to a centrifugal pump or other mechanical device that can increase the water flow pressure and power), which increases the water return pressure and power, making the rotation speed of the cathode and anode cores of the electrolytic cell faster, the centrifugal force stronger, the bubbles generated by the reaction on the electrode plates dissipate faster, and the reaction efficiency of the electrolytic cell is higher.

[0069] ① The water inlet on the inlet sealing end plate 4 serves as the raw water that mainly participates in the electrolysis reaction. The water enters the electrolytic cell electrode reaction zone through the micropores on the electrode support plate on the electrode core. The micropores on the electrode plate play two roles: first, they enhance flow resistance, reduce the flow rate of the raw water, prolong the reaction residence time of the raw water in the reactor, and improve the reaction efficiency; second, they enhance mixing, ensure that the raw water is mixed evenly, and improve the reaction and removal effect of pollutants.

[0070] ② The water inlet 103 on the outer shell 1 of the electrolytic cell mainly provides the rotational power for the electrolytic cell cores, causing the anode and cathode to rotate under the tangential force of the eccentric water flow. Specifically, the outer diameters of the plates with rotating blades on the anode and cathode cores are different, resulting in different linear velocities under the same tangential force of the water flow. This causes relative rotation between the anode and cathode cores, increasing the turbulence between the plates. Simultaneously, the tangentially fed water can also enter the reaction zone of the anode and cathode plates through the sieve holes on the anode and cathode cores to participate in the electrolysis reaction.

[0071] During the electrolysis reaction, the anode and cathode cores rotate under the tangential inflow of water. Due to their different rotational speeds, they rotate relative to each other. This rotation generates centrifugal force on the cylindrical electrode, causing numerous bubbles generated on the surface to dissipate rapidly. Furthermore, the relative rotation of the anode and cathode plates increases the turbulence in the reaction zone, enhancing bubble dissipation and separation. Additionally, each anode and cathode plate is divided into two regions: a plate region and a sieve plate region. The rotation of the sieve plate region also generates turbulence around the sieve openings, significantly enhancing bubble dissipation and separation. This enhanced bubble dissipation and separation effectively reduces the mass transfer resistance between the anode and cathode plates, reducing reaction energy consumption and operating costs. The increased turbulence within the plate region significantly enhances the mixing and contact opportunities between hydroxyl radicals generated by advanced oxidation and pollutants, noticeably improving pollutant removal. Moreover, the enhanced bubble dissipation and separation on the plate surface effectively preserves the reactive zone, ensuring that the amount of hydroxyl radicals generated remains unaffected.

[0072] (3) Drainage and exhaust: The wastewater after the reaction is discharged through the outlet 104 on the outer shell 1 of the electrolytic cell. The main drainage pipe 43 is divided into two branches: a drainage branch pipe 44 and a return water pipe 42. Among them, part of the treated water after the reaction is discharged to the subsequent treatment process through the drainage branch pipe 44, and the other part of the treated water is returned through the return water pipe 42 to provide rotational power for the rotation of the electrolytic cell electrode core. The drain outlet is located below the exhaust sealing end plate 5, so the area between the drain outlet and the exhaust sealing end plate 5 is the gas emission area. Moreover, under the action of the rotating blades of the top electrode core, the gas will be driven to rotate, and the centrifugal force generated by the rotation will make the gas and liquid droplets more thoroughly separated, improving the gas-liquid separation effect. In addition, the gas is discharged through the micropores on the electrode plate support plate on the top electrode core, and then discharged to the subsequent process through the exhaust pipe 45. The micropores on the electrode plate support plate can also filter water droplets, enhance the gas-liquid separation effect, and the micropores will increase the flow resistance of gas emission, ensuring that the gas flow rate is maintained within a safe range during gas emission, and ensuring the safety of the exhaust process. The electrolytic cell design of this invention combines the functions of an advanced oxidation reactor and a gas-liquid separator, saving equipment investment and system footprint, simplifying the system process, and effectively reducing system costs.

[0073] While the present invention has been disclosed above, it is not limited thereto. Any person skilled in the art can make various modifications and alterations without departing from the spirit and scope of the invention; therefore, the scope of protection of the present invention should be determined by the scope defined in the claims.

Claims

1. A high-efficiency oxidation electrolytic cell with a rotatable electrode core, characterized in that, The electrolytic cell comprises, from top to bottom, an exhaust sealing end plate (5), an electrolytic cell shell (1), and a water inlet sealing end plate (4). The electrolytic cell shell (1) is configured as a cylindrical structure. An anode core (2) and a cathode core (3) are installed inside the electrolytic cell shell (1). The length of the electrolytic cell shell (1) is greater than the length of the anode core (2) and the cathode core (3). The anode core (2) includes an anode plate (204) with a multi-layer plate structure. The cathode core (3) includes a cathode plate (304) with a multi-layer plate structure. At least a portion of the anode plate (204) is assembled with the cathode plate (304) to form an equally spaced advanced oxidation reaction zone.

2. The electrolytic cell according to claim 1, characterized in that, The anode plate (204) has an anode plate-shaped area (204a) and an anode sieve plate area (204b). The anode plate-shaped area (204a) is configured as an arc-shaped plate structure with a complete plate surface, and the anode sieve plate area (204b) is configured as a sieve plate structure. The cathode plate (304) has a cathode plate-shaped area (304a) and a cathode sieve plate area (304b). The cathode plate-shaped area (304a) is configured as an arc-shaped plate structure with a complete plate surface, and the cathode sieve plate area (304b) is configured as a sieve plate structure. The cathode sieve plate area (304b) and the anode sieve plate area (204b) are staggered.

3. The electrolytic cell according to claim 1, characterized in that, The outer shell (1) of the electrolytic cell includes a sealing structure (101), an electrolytic cell cylinder (102), and an inlet (103) and an outlet (104) provided on the electrolytic cell cylinder (102). The electrolytic cell cylinder (102) is configured as a cylindrical structure. The sealing structure (101) is provided at both the upper and lower parts of the electrolytic cell cylinder (102). The inlet (103) and the outlet (104) are provided on the side wall of the electrolytic cell cylinder (102), with the inlet (103) located near the lower part and the outlet (104) located near the upper part.

4. The electrolytic cell according to claim 3, characterized in that, The eccentricity of the inlet (103) and outlet (104) should be opposite.

5. The electrolytic cell according to claim 1, characterized in that, The anode core (2) includes an anode sealing conductive pad (201), a conductive anode bearing (202), an anode plate support plate (203), and an anode plate (204). The anode plate support plate (203) is disposed on the top of the anode plate (204) and rotates integrally with the anode plate (204). The conductive anode bearing (202) is disposed radially around the anode plate (204). An annular anode sealing conductive pad (201) is disposed on the outside of the conductive anode bearing (202), and the anode sealing conductive pad (201) wraps around the conductive anode bearing (202).

6. The electrolytic cell according to claim 5, characterized in that, An anode contact piece (205) is also connected to the radial side of the anode sealing conductive pad (201) for electrically connecting the anode plate (204).

7. The electrolytic cell according to claim 5, characterized in that, The outermost anode plate (204) is provided with an anode blade (206) around its periphery, and the anode blade (206) protrudes and extends away from the axis.

8. The electrolytic cell according to claim 1, characterized in that, The cathode core (3) includes a cathode sealing conductive pad (301), a conductive cathode bearing (302), a cathode plate support plate (303), and a cathode plate (304). The cathode plate support plate (303) is disposed on the top of the cathode plate (304) and rotates integrally with the cathode plate (304). The conductive cathode bearing (302) is disposed radially around the cathode plate (304). An annular cathode sealing conductive pad (301) is disposed on the outside of the conductive cathode bearing (302), and the cathode sealing conductive pad (301) wraps around the conductive cathode bearing (302).

9. The electrolytic cell according to claim 8, characterized in that, A cathode contact plate (305) is also connected to the radial side of the cathode sealing conductive pad (301) for connecting the cathode plate (304) to the electrical system.

10. The electrolytic cell according to claim 8, characterized in that, A cathode blade (306) is provided around the outermost cathode plate (304), and the cathode blade (306) protrudes and extends away from the axis.

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