Method for electromagnetic synergistic oxidation of organic matter in wastewater

Abstract

This invention discloses a method for electromagnetic synergistic oxidation of organic matter in wastewater. The method involves placing an electrolyte, an auxiliary oxidant, and organic wastewater containing polycyclic aromatic hydrocarbons and antibiotics in an electrolytic cell, and operating at a voltage of 1–12V and a current density of 1–20 mA / cm². 2 This invention oxidizes polycyclic aromatic hydrocarbons (PAHs) and antibiotic pollutants under specific conditions, achieving their degradation and mineralization. Simultaneously, the invention provides an electrolytic cell. The method and apparatus of this invention can generate a large amount of active material through an ultra-large specific surface area cathode. A series of electromagnetic synergistic chain reactions achieve full contact between pollutants and active materials, while also recovering valuable ions from wastewater, thus achieving the purpose of purifying organic wastewater. This solves the technical problems of long reaction time, high energy consumption, and low mineralization rate in existing technologies.

Description

A method for electromagnetic synergistic oxidation of organic matter in wastewater Technical Field

[0001] This invention belongs to the field of organic wastewater treatment technology, specifically relating to a method for electromagnetic synergistic oxidation of organic matter in wastewater. Background Technology

[0002] The in-depth development of organic chemistry, while expanding production capacity, has also generated a large amount of wastewater, which naturally contains significant quantities of polycyclic aromatic hydrocarbons (PAHs) and antibiotic-like pollutants. Simple physicochemical methods are insufficient to completely degrade or transfer these pollutants. Furthermore, biological treatment technologies often fail to meet the expected requirements for highly stable and recalcitrant pollutants. Electrochemical oxidation technologies, such as electrochemical oxidation and electrochemical catalytic oxidation, generate a large number of electrons and protons through the intervention of an electric field, achieving electron transfer. This can decompose recalcitrant organic pollutants into biodegradable small-molecule organic compounds and even mineralize them, thus being considered an effective water treatment technology for recalcitrant organic wastewater. Adding a certain amount of oxidant to the treatment system can accelerate electron transfer and generate a large amount of oxidizing reactive oxygen species (ROS), further accelerating the degradation rate and increasing the mineralization rate. CN110872145A discloses an electrochemical method for removing organic matter by adding an oxidant. Using hydrogen peroxide as the oxidant, hydroxyl radicals are generated through stirring and the addition of transition metals, resulting in an electron transfer reaction that produces organic polymers, which are then removed through solid-liquid separation. CN110980894A discloses a method for electrochemically degrading volatile organic compounds. Using an ionic liquid as the electrolyte, the method employs constant potential electrolysis to generate active hydroxyl radicals that directly oxidize the organic compounds. At a voltage of 1.2-1.5V, a degradation rate of approximately 80% is achieved.

[0003] It is worth noting that the above-mentioned treatment technologies also have shortcomings: (1) the reaction process takes a long time, which increases the energy consumption for degrading pollutants; (2) the target pollutants will generate some intermediate products that inhibit the positive reaction during the oxidative degradation process, which will prolong the treatment time; (3) due to the ring-opening problem of polycyclic aromatic hydrocarbons and antibiotics and the problem of long degradation pathways, the difficulty of quickly achieving complete mineralization is increased. Summary of the Invention

[0004] To address the problems existing in the prior art, this invention provides a method for the electromagnetic synergistic oxidation of organic matter in wastewater. This method controls reaction parameters to oxidize most organic pollutants in an electrolytic cell under specific current density and magnetic field strength, achieving complete degradation and thorough mineralization of the pollutants. Specifically, electrolytes, auxiliary oxidants, and organic wastewater containing polycyclic aromatic hydrocarbons and antibiotics are placed in an electrolytic cell, with the voltage ranging from 1 to 12V and the current density from 1 to 20 mA / cm².2 Under certain conditions, polycyclic aromatic hydrocarbons (PAHs) and antibiotic pollutants are oxidized, achieving their degradation and mineralization. The electrolytic cell includes a shell, with a microporous aeration unit located in the lower part of the shell. The microporous aeration unit includes an aeration pipe and several aeration plates. An air pump is connected to one end of the aeration pipe via a control valve, and the other end of the aeration pipe is connected to several aeration plates. Micropores are formed on both the aeration pipe and the aeration plates. The anode is located at the center of the shell, with a non-contact solenoid coil wound around it. The motor's output shaft is connected to the solenoid coil via a conductive slider. Cathodes I and II are cylindrical electrodes, with cathode II located outside the anode and... Several aeration plates are installed between cathode II and the anode. Cathode I is located outside cathode II, and several aeration plates are installed between cathode II and cathode I. Several aeration plates are installed between cathode I and the inner wall of the shell. An exhaust hole is opened at the top of the shell. An annular negative pressure air intake unit is fixed at the top of the shell and forms an air chamber. The air chamber is connected to the exhaust hole at the top. A dosing pipe is installed at the top of the shell. A water inlet and a sludge storage hopper are installed at the bottom of the shell. One or more drain outlets are opened at the top of the shell. A perforated baffle is installed below the drain outlet to prevent incomplete reaction. The solenoid coil, motor, cathode I, cathode II, anode, and air pump are connected to the power supply.

[0005] The electrolyte is, but is not limited to, carbonic acid, acetic acid, hypochlorous acid, phosphoric acid, aluminum hydroxide, zinc hydroxide, sodium salt, phosphate salt, chloride salt, and iron salt, and the amount of electrolyte added is 2 to 8 mmol / L.

[0006] The auxiliary oxidant is selected from hydrogen peroxide, sodium peroxide, sodium persulfate, and chlorine water, and the amount of auxiliary oxidant added is 80~160 mmol / L.

[0007] Metal ions, selected from nickel ions, molybdenum ions, zirconium ions, and niobium ions, are added to the electrolytic cell at a concentration of 1–4 mmol / L.

[0008] The perforated baffle is a hollow frustum shape, and the aeration plate is an arc plate.

[0009] The annular negative pressure suction unit consists of a circular plate and a cylinder fixed at the center of the circular plate. The circular plate has two or more exhaust fans, and the cylinder has several air holes. The cylinder passes through the motor output shaft and is fixed to the top of the housing. The disc fits tightly with the inner wall of the housing and forms an annular air chamber with the top of the housing.

[0010] The cathode I is a mesh or porous electrode, and the electrode material is selected from Ti, iron, carbon materials, and stainless steel; the cathode II is an iron-carbon microelectrode, which is a cylindrical electrode made by wrapping iron-carbon microelectrolysis material with an iron mesh.

[0011] The anode is composed of a substrate and an active layer; the anode is composed of a substrate and an active layer attached to the substrate; the substrate material is selected from porous carbon materials, metal oxides, conductive glass, and conductive ceramics; the active layer material is selected from metals and metal oxides; wherein the metal is selected from titanium, iron, cobalt, nickel, ruthenium, tungsten, antimony, rhodium, lanthanum, cerium, praseodymium, lutetium, scandium, and yttrium.

[0012] The anode was prepared according to the literature "Research on Electrocatalytic Oxidation of Pyridine and Naphthalene by Rare Earth Doped Lead-Tin DSA Electrode". Acid-base pretreatment was used to change the surface morphology of the substrate. Electroplating or hot calcination was used to achieve a tight bond between the active layer and the substrate. Electrodeposition was used to complete the adhesion of the active layer.

[0013] This invention utilizes an electromagnetic synergistic oxidation device composed of an anode, a solenoid coil, cathode I, and cathode II. The anode and the energized solenoid coil achieve electromagnetic synergy, with each powered independently to control the electric and magnetic fields. The rotational disturbance of the solenoid coil and the intervention of the magnetic field not only assist in the electric field oxidation of organic wastewater but also achieve the adsorption and desorption of valence ions, thus addressing side reaction inhibition and equipment scaling issues. The desorbed valence ions undergo electrocoagulation with particulate matter and salts in the wastewater and precipitate in a sludge storage hopper. After equipment operation, the sludge is removed to recover the valence ions. Cathode I and cathode II form a dual cathode structure to increase the reaction surface area and the amount of active substances produced. Cathode II can also generate active substances through the micro-electrolysis of iron and carbon. Microcurrents enable synergistic effects of electromagnetic and micro-electrolysis for better degradation; perforated baffles prevent direct discharge of large amounts of wastewater, causing back-mixing and turbulence to increase reaction time and optimize the wastewater purification process; oxygen-containing gases are introduced through micropores in aeration plates and pipes to increase dissolved oxygen content and enhance active components, thereby accelerating the reaction process through multi-pathway and multi-series oxidation; various gases (oxygen, hydrogen, carbon dioxide, chlorine, dichloromethane, and other VOCs) float to the surface through the holes in the perforated baffles and are collected in the gas chamber by the annular negative pressure suction unit under the action of the exhaust fan, recovering oxygen and hydrogen for resource utilization while avoiding the inhibitory effect of harmful gases on the reaction.

[0014] The distance between cathode I and cathode II is 5-10 cm, the distance between anode and cathode II is 8-12 cm, and the air velocity is 0.5~2 m / s. 3 / min, the magnetic field strength of the solenoid is 50~200mT, and the reaction time is 0.5~6h.

[0015] The advantages and technical effects of this invention are as follows:

[0016] The reduction reaction of oxygen on a cathode with an ultra-large specific surface area increases the amount of active material produced. Simultaneously, the back-mixing turbulence generated by the perforated baffle and the disturbance of the spiral coil facilitate good diffusion of the active material. The number and conduction rate of electrons are crucial factors determining the electrochemical reaction rate; the addition of electrolytes promotes electron conduction, achieving ionization equilibrium and thus improving the reaction rate. In the electrolytic cell of this invention, the good diffusion of active material ensures sufficient contact between organic pollutants and active components, improving the degradation efficiency of organic matter and shortening the reaction time. The intervention of a magnetic field achieves electromagnetic synergy, accelerating the reaction process and recovering valent ions. Rapid degradation occurs at lower voltage and current densities, thereby reducing energy consumption. The synergistic effect of multiple active materials attacks different active sites in organic matter, shortening the chain reaction length and facilitating the generation of low-molecular-weight intermediates, thereby improving the final mineralization degree of organic matter. Attached Figure Description

[0017] Figure 1 is a schematic diagram of the electrolytic cell structure of the present invention;

[0018] Figure 2 is a schematic cross-sectional view of the microporous aeration unit and electrode structure of the present invention.

[0019] Figure 3 is a schematic diagram of the annular negative pressure intake unit structure of the present invention;

[0020] Figure 4 is a schematic diagram of the perforated baffle structure of the present invention;

[0021] In the diagram: 1. Shell; 2. Air pump; 3. Control valve; 4. Motor; 5. Aeration plate; 6. Cathode I; 7. Cathode II; 8. Anode; 9. Solenoid coil; 10. Dosing pipe; 11. Inlet; 12. Outlet; 13. Sludge hopper; 14. Air chamber; 15. Perforated baffle; 16. Cylinder; 17. Exhaust fan; 18. Aeration pipe; 19. Annular negative pressure suction unit. Detailed Implementation

[0022] To make the present invention more specific and clear, the present invention will be further described in detail below with reference to the accompanying drawings and embodiments. Unless otherwise specified, the reagents and methods in the embodiments are all commercially available reagents or performed according to conventional methods.

[0023] As shown in Figures 1-4, the electrolytic cell used in this embodiment includes a shell 1. A microporous aeration unit is installed in the lower part of the shell. The microporous aeration unit includes an aeration pipe 18 and several aeration plates 5. An air pump 2 is connected to one end of the aeration pipe via a control valve 3, and the other end of the aeration pipe is connected to several aeration plates 5. Micropores are opened on both the aeration pipe and the aeration plates. The anode 8 is located at the center of the shell. A motor is fixed at the center of the top of the shell, and its output shaft passes through the shell and enters the shell, connecting to a solenoid coil 9 via a conductive slider. The solenoid coil 9 is wound non-contactly on the anode 8. Cathodes I 6 and II 7 are cylindrical electrodes. Cathode II 7 is located outside the anode, and four aeration plates are arranged between cathode II and the anode. Cathode I 6 is located outside the cathode II, and four aeration plates are arranged between cathode II and cathode I. The aeration plates are arranged between the cathode I6 and the inner wall of the shell. The aeration plates are arc-shaped. The top of the shell has an exhaust hole. The annular negative pressure suction unit consists of a circular plate and a cylinder 16 fixed at the center of the circular plate. The circular plate has four exhaust fans 17. The cylinder has several air holes. The cylinder passes through the motor output shaft and is fixed to the top of the shell. The disc fits tightly with the inner wall of the shell and forms an annular air chamber 14 with the top of the shell. The air chamber is connected to the exhaust hole at the top. The top of the shell is equipped with a dosing pipe 10. The bottom of the shell is equipped with a water inlet 11 and a sludge storage hopper 13. The upper part of the shell has one or more drain outlets 12. A perforated baffle 15 is set below the drain outlet 12. The perforated baffle is a hollow frustum shape. The solenoid coil, motor, cathode I, cathode II, anode, and air pump are respectively connected to the power supply.

[0024] Example 1: Treatment of naphthalene-containing wastewater in this example

[0025] First, following the method described in the article "Research on Electrocatalytic Oxidation of Pyridine and Naphthalene by Rare Earth Doped Lead-Tin DSA Electrode", the RuO2 substrate was pretreated with acid and alkali. Metallic Ti was then electroplated onto the substrate surface to prepare a Ti / RuO2 electrode as the anode, with a Ti mass ratio of 5wt%. A Ti cylinder was selected as cathode I, and iron filings and charcoal (mass ratio 4:1) were placed in an iron mesh box as cathode II. In the electrolytic cell, a microporous aeration unit composed of aeration pipes and aeration plates is responsible for supporting the electrodes. The anode is located at the center of the shell and aeration pipes. Cathode II is located outside the anode, with four aeration plates between cathode II and the anode, and the distance between cathode II and the anode is 12 cm. Cathode I is located outside cathode II, with four aeration plates between cathode II and cathode I, and the distance between cathode I and cathode II is 8 cm. Four aeration plates are located between cathode I and the inner wall of the shell. The rotational disturbance of the solenoid coil and the intervention of the magnetic field can assist the electric field oxidation of organic wastewater and also realize the adsorption and desorption of valence ions. By opening micropores on the aeration pipes and aeration plates, oxygen undergoes a reduction reaction on the ultra-large specific surface area cathode, increasing the amount of active substances produced. At room temperature, 2 L of naphthalene wastewater with a concentration of 8 mmol / L was added to the electrolytic cell through the inlet. After the wastewater wetted the electrodes, 5 mmol / L sodium chloride, 100 mmol / L sodium persulfate, and 1 mmol / L nickel sulfate were added through the dosing tube. Then, a 6V voltage was applied using a single-pulse power supply, the solenoid magnetic field strength was set to 130 mT, and the air intake was adjusted to 0.5 m³ / h using an air pump and control valve. 3 The aeration rate is [ / min], with air blown into the cathode surface by a microporous aeration unit. During the continuous reaction, to avoid direct discharge of large amounts of wastewater, a hollow frustum-shaped perforated baffle effectively causes backmixing and turbulence in the wastewater, increasing reaction time and optimizing the wastewater purification process. Simultaneously, the backmixing turbulence allows for good diffusion of active substances. Various gases during the reaction rise through the holes in the perforated baffle and are collected in the gas chamber by the exhaust fan or through holes on the cylinder (the four exhaust fans on the circular plate and several air holes on the cylinder work together to form a negative pressure annular gas chamber for automatic gas collection). After the reaction, the gases can be further treated through the exhaust port connected to the top of the gas chamber. During the reaction, valence ions, under the influence of the spiral coil and magnetic field, undergo electrocoagulation with particulate matter and salts in the wastewater and precipitate in the sludge storage hopper. After operation, the sludge can be removed to recover the valence ions. During the reaction, the purified water flows out through the drain. After the device has been running for 5 hours, the naphthalene removal rate is 72% and the mineralization degree is 48%.

[0026] A control group without sodium persulfate was also tested, showing a naphthalene removal rate of 44% and a mineralization degree of 30%. This indicates that the addition of persulfate promoted the electrochemical oxidation removal of polycyclic aromatic hydrocarbons. There is a synergistic effect between ·OH and ·OH, and at the same time The combined effect of ·OH contributes more to the degree of mineralization than that of ·OH.

[0027] A control group without nickel sulfate was also tested, and the naphthalene removal rate was 68%, indicating that the addition of transition metals can also promote the electrochemical oxidation removal of polycyclic aromatic hydrocarbons and is beneficial to the activation of persulfate.

[0028] Example 2: Treatment of ciprofloxacin-containing wastewater in this example

[0029] First, referring to the literature "Study on Electrocatalytic Oxidation of Pyridine and Naphthalene by Rare Earth Doped Lead-Tin DSA Electrode", an acid-base pretreatment was performed on a g-C3N4 substrate. Co3O4 was then loaded onto the substrate using a calcination method to prepare a Co3O4 / g-C3N4 electrode as the anode, with a Co3O4 mass ratio of 8wt%. A graphite cylinder was selected as cathode I, and iron filings and coke (4:1) were placed in an iron mesh box as cathode II. The distance between cathode II and anode was 10 cm; the distance between cathode I and cathode II was 8 cm. At 35℃, 2 L of 10 mmol / L ciprofloxacin wastewater was added to the electrolytic cell through the inlet. After the wastewater wetted the electrodes, 5 mmol / L phosphoric acid and 100 mmol / L sodium peroxide were added through the dosing tube. Then, a 6V voltage was applied using a single-pulse power supply, a magnetic field strength of 100 mT, and an air volume of 0.6 m³ / s was introduced. 3 The aeration rate is [ / min], where oxygen is blown into the cathode surface through a microporous aeration unit to complete the aeration. During the continuous reaction, to avoid the direct discharge of large amounts of wastewater, a hollow frustum-shaped perforated baffle is installed to effectively cause backmixing of the wastewater, forming turbulence to increase the reaction time and optimize the wastewater purification process; at the same time, the backmixing turbulence also allows for good diffusion of active substances. Various gases during the reaction float to the surface through the holes in the perforated baffle, and are automatically collected by the combined action of four exhaust fans on the circular plate of the annular negative pressure suction unit and several air holes on the cylinder, forming an annular air chamber with negative pressure conditions. After the reaction, the gases can be further treated through the exhaust port connected to the top of the air chamber. During the reaction, valence ions undergo electrocoagulation with particulate matter and salts in the wastewater under the influence of the spiral coil and magnetic field, and precipitate in the sludge hopper. After the operation is completed, the sludge can be removed to recover the valence ions. During the reaction, the purified water flows out through the drain outlet, and after the equipment operation is completed, the purified water can be discharged through the inlet. After the device operated for 4 hours, the ciprofloxacin removal rate was 86% and the mineralization degree was 60%.

[0030] Meanwhile, a control group without sodium peroxide was used. The ciprofloxacin removal rate was 70%, and the mineralization degree was 52%. This indicates that the addition of sodium peroxide promoted the electrochemical oxidation removal of antibiotics. Sodium peroxide increased the amount of ·OH generated, thereby improving the removal rate and mineralization degree.

[0031] Example 3: This example describes the treatment of wastewater containing naphthalene and ciprofloxacin.

[0032] This embodiment is the same as Embodiment 1, except that, firstly, referring to the literature "Research on Electrocatalytic Oxidation of Pyridine and Naphthalene by Rare Earth Doped Lead-Tin DSA Electrode", an acid-base pretreatment of the conductive glass substrate was performed. A combination of electroplating and calcination was used to load cerium dioxide metal oxide onto the substrate surface to prepare a CeO2 / conductive glass electrode as the anode, with a CeO2 mass ratio of 6wt%. A stainless steel cylinder was selected as cathode I, and iron filings and charcoal (4:1) were placed in an iron mesh box as cathode II. The distance between cathode II and the anode was 8 cm; the distance between cathode I and cathode II was 6 cm. Under room temperature conditions, 2 L of wastewater containing 8 mmol / L naphthalene and 10 mmol / L ciprofloxacin was added to the electrolytic cell through the inlet. After the wastewater wetted the electrode, 5 mmol / L hypochlorous acid and 100 mmol / L hydrogen peroxide were added through the dosing tube 10. Then, a 10V voltage was applied using a single-pulse power supply, the magnetic field strength of the solenoid coil was set to 100 mT, and the air intake was adjusted to 1.0 m using an air pump and control valve. 3 The oxygen is blown into the cathode surface through a microporous aeration unit at a rate of / min to complete aeration. After the device has been running for 3 hours, the naphthalene removal rate is 88% and the mineralization degree is 70%; the ciprofloxacin removal rate is 86% and the mineralization degree is 62%.

[0033] A control group without hydrogen peroxide was also tested. The naphthalene removal rate was 48% and the mineralization degree was 28%. The ciprofloxacin removal rate was 50% and the mineralization degree was 30%. This indicates that the addition of hydrogen peroxide significantly promoted the electrochemical oxidation removal of polycyclic aromatic hydrocarbons and antibiotics. Hydrogen peroxide significantly increased the amount of ·OH generated, which significantly improved the removal rate and mineralization degree.

Claims

1. A method for electromagnetic synergistic oxidation of organic matter in wastewater, characterized in that: Electrolytes, auxiliary oxidants, and organic wastewater containing polycyclic aromatic hydrocarbons and antibiotics are placed in an electrolytic cell, and the electrolysis is carried out at a voltage of 1–12V and a current density of 1–20mA / cm³. 2 Under certain conditions, polycyclic aromatic hydrocarbons (PAHs) and antibiotic pollutants are oxidized to achieve the degradation and mineralization of PAHs and antibiotic pollutants; the electrolytic cell includes a shell (1), and a microporous aeration unit is set in the lower part of the shell. The microporous aeration unit includes an aeration pipe (18) and several aeration plates (5). The air pump (2) is connected to one end of the aeration pipe through a control valve (3), and the other end of the aeration pipe is connected to several aeration plates (5). Micropores are opened on the aeration pipe and the aeration plates; the anode (8) is set in the center of the shell, and a non-contact coil (9) is wound on the anode (8). The output shaft of the motor is connected to the coil through a conductive slider. The cathode I (6) and cathode II (7) are cylindrical electrodes. Cathode II (7) is set outside the anode and several aeration plates are set between cathode II and the anode. Cathode I (6) is set outside the cathode II and several aeration plates are set between cathode II and cathode I. A number of aeration plates are provided between the cathode I (6) and the inner side wall of the shell; an exhaust hole is opened at the top of the shell, and the annular negative pressure suction unit is fixed at the top of the shell and forms an air chamber (14). The air chamber is connected to the exhaust hole at the top. A dosing pipe (10) is provided at the top of the shell, and a water inlet (11) and a sludge storage hopper (13) are provided at the bottom of the shell. One or more drain outlets (12) are opened at the top of the shell, and a perforated baffle (15) is set below the drain outlet (12). The solenoid coil, motor, cathode I, cathode II, anode, and air pump are respectively connected to the power supply. The annular negative pressure suction unit consists of a circular plate and a cylinder (16) fixed at the center of the circular plate. The circular plate has two or more exhaust fans (17). Several air holes are opened on the cylinder. The cylinder passes through the motor output shaft and is fixed at the top of the shell. The disc fits tightly with the inner wall of the shell and forms an annular air chamber (14) with the top of the shell.

2. The method for electromagnetic synergistic oxidation of organic matter in wastewater according to claim 1, characterized in that: Electrolytes include, but are not limited to, carbonic acid, acetic acid, hypochlorous acid, phosphoric acid, aluminum hydroxide, zinc hydroxide, sodium salts, phosphate salts, chloride salts, and iron salts. The amount of electrolyte added is 2 to 8 mmol / L.

3. The method for electromagnetic synergistic oxidation of organic matter in wastewater according to claim 1, characterized in that: The auxiliary oxidant is selected from hydrogen peroxide, sodium peroxide, sodium persulfate, and chlorine water, and the amount of auxiliary oxidant added is 80~160 mmol / L.

4. The method for electromagnetic synergistic oxidation of organic matter in wastewater according to claim 1, characterized in that: Metal ions, selected from nickel ions, molybdenum ions, zirconium ions, and niobium ions, are added to the electrolytic cell at a concentration of 1–4 mmol / L.

5. The method for electromagnetic synergistic oxidation of organic matter in wastewater according to claim 1, characterized in that: The perforated baffle is a hollow frustum shape, and the aeration plate is an arc-shaped plate.

6. The method for electromagnetic synergistic oxidation of organic matter in wastewater according to claim 1, characterized in that: Cathode I is a mesh or porous electrode, and the electrode material is selected from Ti, iron, carbon, and stainless steel; Cathode II is an iron-carbon microelectrode, which is a cylindrical electrode made by wrapping iron-carbon microelectrolysis material with an iron mesh.

7. The method for electromagnetic synergistic oxidation of organic matter in wastewater according to claim 1, characterized in that: The anode consists of a substrate and an active layer attached to the substrate; the substrate material is selected from porous carbon materials, metal oxides, conductive glass, and conductive ceramics; the active layer material is selected from metals and metal oxides; among which the metals are selected from titanium, iron, cobalt, nickel, ruthenium, tungsten, antimony, rhodium, lanthanum, cerium, praseodymium, lutetium, scandium, and yttrium.

8. The method for electromagnetic synergistic oxidation of organic matter in wastewater according to claim 1, characterized in that: The magnetic field strength of the solenoid coil is 50~200mT, and the air velocity is 0.5~2m. 3 / min.

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