Electro-fenton and electro-catalytic enhanced synergistic unit and application thereof

Abstract

The application belongs to the technical field of water treatment, and provides an electro-Fenton and electro-catalysis reinforced type synergistic unit and application thereof. The electro-Fenton and electro-catalysis reinforced type synergistic unit is composed of a surface / network electrode and a comb / grid electrode, and the surface / network electrode and the comb / grid electrode are arranged in parallel in each synergistic unit. The arrangement mode of the synergistic unit is divided into three types: the first type is that the synergistic units form a closed loop along the wall of the reaction device; the second type is that a plurality of non-connected synergistic units are arranged along the wall of the reaction device; and the third type is a combination of the first type and the second type. The electro-Fenton and electro-catalysis reinforced type synergistic unit can obtain a closer electrode spacing and a lower voltage, and cooperate with the stirring device on the side of the comb / grid electrode to obtain a better mass transfer effect and a more efficient synergistic degradation effect compared with the traditional synergistic unit. Moreover, different types of configurations are selected through analysis of the polluted water quality.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of water treatment, and particularly relates to an electro-Fenton and electro-catalysis reinforced type synergistic unit and application thereof. BACKGROUND

[0002] Industrial wastewater has complex components, and contains not only a large amount of organic pollutants that can be oxidized and degraded, such as aromatic hydrocarbons, chain alkanes and the like, but also inorganic pollutants such as ammonia nitrogen that can be oxidized and degraded. The ability of electro-Fenton oxidation method and anode electro-catalytic oxidation method to degrade the above pollutants alone needs to be improved. Research has found that the two methods can be used in cooperation to improve the pollutant degradation efficiency and energy utilization efficiency.

[0003] At present, the electro-Fenton and electro-catalysis synergistic degradation mainly uses a "traditional type" synergistic system to degrade pollutants. The traditional type configuration includes a plate / net-shaped cathode cooperating with a plate / net-shaped anode synergistic system, a sleeve type synergistic system, a surface / net-shaped electrode cooperating with a brush-shaped electrode synergistic system and the like. When the plate / net-shaped cathode cooperating with the plate / net-shaped anode synergistic system and the sleeve type synergistic system are used for synergistic degradation, the pollutants are degraded at one side of the electrode, and then the degradation products move to the other side of the electrode for further degradation. The synergistic degradation process occurs in a cycle between the two electrodes. Research has found that when the above systems are used, the electrode spacing becomes smaller, which can shorten the mass transfer distance between the cathode and the anode, and can also reduce the operating voltage, which is beneficial to the degradation of the pollutants. However, as the spacing between the cathode and the anode becomes smaller, the mass transfer resistance of the external pollutants entering the space between the cathode and the anode increases, which is not conducive to the efficient mass transfer of the pollutants in the reaction device, and further not conducive to the efficient degradation of the pollutants.

[0004] In patent document CN116119781A, a "traditional" plate / mesh cathode and plate / mesh anode are used for synergistic degradation of pollutants, and certain degradation effect is achieved, but the following problems still exist: on the one hand, the synergistic degradation mainly occurs between the adjacent cathode and anode in the "traditional" synergistic degradation; on the other hand, as the electrode spacing decreases, the mass transfer resistance of the liquid entering the cathode and anode increases rapidly, which is not conducive to the synergistic degradation reaction between the cathode and anode, and further not conducive to the efficient degradation of pollutants in the reactor. In patent document CN109879381A, a sleeve type electro-Fenton reactor is used, that is, a cathode shell and an anode sleeve are used, but the system uses a sleeve structure, which is not conducive to the wastewater entering the cathode and anode from the direction perpendicular to the cylinder surface to occur synergistic degradation. Therefore, in addition to the horizontal water flow stirring, longitudinal water flow stirring needs to be provided, and additional energy is needed to make the liquid in the system flow fully, which increases the energy consumption of wastewater treatment. In patent document CN115124116B, a "traditional" face / mesh electrode is used to cooperate with a brush electrode synergistic system, that is, an anode pipe and a cathode carbon brush are used, which can reduce the current density, but too low current density is not conducive to the degradation of pollutants, and the brush structure can significantly increase the mass transfer resistance inside the reaction device, which is not conducive to the efficient mass transfer between the cathode and anode in the wastewater, and further not conducive to efficient degradation.

[0005] In order to solve the above problems, it is urgent to provide an electro-Fenton and electro-catalytic enhanced synergistic unit which can realize smaller electrode spacing and mass transfer resistance and lower operating voltage and efficient degradation. SUMMARY

[0006] The purpose of the present application is to provide an electro-Fenton and electro-catalytic enhanced synergistic unit and its application to overcome the shortcomings of the prior art.

[0007] In order to achieve the above-mentioned purpose of the application, the present application provides the following technical solutions:

[0008] The present application provides an electro-Fenton and electro-catalytic enhanced synergistic unit, which is composed of one face / mesh electrode and one comb / grid electrode, and the face / mesh electrode and the comb / grid electrode are arranged in parallel in each synergistic unit.

[0009] In the reaction device, from the outside to the inside, the reaction device wall, the face / mesh electrode and the comb / grid electrode are sequentially arranged;

[0010] The arrangement mode of the synergistic unit is divided into three types: the first type is that the synergistic units form a closed loop along the reaction device wall; the second type is that a plurality of non-connected synergistic units are arranged along the reaction device wall, and the number n of the synergistic units is greater than or equal to 1; the third type is a combination of the first type and the second type;

[0011] The electro-Fenton and electro-catalysis enhanced synergic unit comprises a plane / mesh cathode and a comb / grid anode or the electro-Fenton and electro-catalysis enhanced synergic unit comprises a plane / mesh anode and a comb / grid cathode.

[0012] Preferably, the plane of the synergic unit is a flat plate and / or an arc surface; the distance between the plane where the plane / mesh electrode is located and the plane where the comb / grid electrode is located is 1-50 mm.

[0013] Preferably, the ratio of the length of the comb teeth / grid strips in the comb / grid electrode to the length of the corresponding plane / mesh electrode is 0.05-1:1, the gap between the comb teeth / grid strips is 1-50 mm, and the width of the comb teeth / grid strips is 1-50 mm.

[0014] Preferably, the transverse ribs of the grid electrode in the comb / grid electrode comprise conductive transverse ribs or non-conductive transverse ribs, and the distance between the transverse ribs is 1-500 mm.

[0015] The conductive transverse ribs comprise one or more of titanium ribs, titanium-based ruthenium iridium ribs, titanium-based lead dioxide ribs and titanium-based tin antimony ribs; the non-conductive transverse ribs comprise one or more of alumina ribs, zirconia ribs and silicon carbide ribs.

[0016] Preferably, the cross section of the comb teeth / grid strips in the comb / grid electrode is one or more of a circular cross section, a semi-circular cross section, an elliptical cross section, a square cross section, a rectangular cross section, a parallelogram cross section, an arch cross section, a rhombus cross section, a trapezoidal cross section, a triangular cross section, a pentagonal cross section, a hexagonal cross section, a wavy cross section, a V-shaped cross section, a semi-V-shaped cross section, a U-shaped cross section, a semi-U-shaped cross section and an X-shaped cross section.

[0017] The cross section of the reaction device is a circular cross section, a rectangular cross section, a square cross section, a triangular cross section, a pentagonal cross section or a hexagonal cross section.

[0018] Preferably, when the pollutants are benzene ring-containing compounds, the electro-Fenton and electro-catalysis enhanced synergic unit is a plane / mesh cathode combined with a comb / grid anode; when the pollutants are chain alkane-containing compounds, the electro-Fenton and electro-catalysis enhanced synergic unit is a plane / mesh anode combined with a comb / grid cathode.

[0019] Preferably, the cathode is a homogeneous electro-Fenton cathode or a heterogeneous electro-Fenton cathode; the homogeneous electro-Fenton cathode is a metal material electrode or a carbon material electrode; the heterogeneous electro-Fenton cathode is an electrode obtained by impregnating a transition metal into a homogeneous electro-Fenton material, the homogeneous electro-Fenton material is a metal material or a carbon material, and the transition metal is an oxide of iron, an oxychloride of iron or an oxychloride of iron and copper.

[0020] The anode is a noble metal anode, a DSA anode or a carbon anode.

[0021] The metal material comprises one or more of iron, nickel, copper, manganese, cobalt, silver, platinum, gold, zinc and cadmium; the carbon material comprises diamond, graphite, amorphous carbon or modified carbon;

[0022] The amorphous carbon comprises wood-based activated carbon, shell-based activated carbon, coal-based activated carbon, regenerated carbon, oxygen-based iron chloride modified activated carbon or petroleum-based activated carbon; the modified carbon is heteroatom modified carbon, and the heteroatom comprises one or more of fluorine, nitrogen, phosphorus and sulfur;

[0023] The iron oxide is Fe2O3, Fe3O4 or FeOOH; the iron oxychloride is FeOCl; the transition metal comprises one or more of iron, nickel, copper, manganese, cobalt, silver, platinum, gold, zinc and cadmium;

[0024] The noble metal comprises one or more of gold, silver, platinum, ruthenium, rhodium, palladium, osmium and iridium; the carbon anode comprises coke anode, graphite anode or diamond anode; the DSA anode comprises titanium-based ruthenium iridium electrode, titanium-based iridium tantalum electrode, titanium-based lead dioxide electrode or titanium-based tin antimony electrode.

[0025] As preferred, an aeration device is arranged below the positive side of the comb / grid-shaped anode or cathode, and air, oxygen or a mixture of air and oxygen is aeration-exposed to the electro-Fenton and electro-catalysis enhanced type synergistic unit through the aeration device, and the flow rate of the aeration is 50-800 mL / min;

[0026] The stirring device is arranged at the side of the comb / grid-shaped electrode, and the distance between the stirring device and the water surface and the ratio of the water depth are 0.01-0.99:1.

[0027] As preferred, the current density is 1-70 mA / cm 2 .

[0028] The application also provides the application of the electro-Fenton and electro-catalysis enhanced type synergistic unit in water treatment.

[0029] The beneficial effects of the application include:

[0030] 1) The synergistic unit of the application uses the face / net-shaped electrode and the comb / grid-shaped electrode parallel thereto, so that closer electrode spacing (i.e. shorter anode-cathode mass transfer spacing), lower operation voltage, smaller mass transfer resistance and excellent mass transfer effect can be simultaneously obtained, the enhanced type synergistic degradation is realized, and better treatment efficiency and lower treatment energy consumption are obtained.

[0031] 2) The present application can obtain closer electrode spacing and lower voltage by using comb / grid electrodes and surface / net electrodes in combination, and can obtain better mass transfer effect compared with traditional synergistic units by using stirring devices (mechanical stirring and aeration stirring) on the side of the comb / grid electrodes, to realize enhanced synergy and obtain more efficient synergistic degradation effect. Moreover, by analyzing the pollution water quality, different types of configurations are selected to obtain higher mass transfer efficiency, better degradation effect and lower energy consumption. BRIEF DESCRIPTION OF DRAWINGS

[0032] Figure 1 The electro-Fenton and electro-catalysis synergistic unit of Example 1;

[0033] Figure 2 The electro-Fenton and electro-catalysis synergistic unit of Comparative Example 1;

[0034] Figure 3 COD removal rates of different structures of Example 1 and Comparative Example 1 on coking wastewater;

[0035] Figure 4 The electro-Fenton and electro-catalysis synergistic unit of Example 2;

[0036] Figure 5 The electro-Fenton and electro-catalysis synergistic unit of Comparative Example 2;

[0037] Figure 6 COD removal rates of different structures of Example 2 and Comparative Example 2 on coking wastewater;

[0038] Figure 7 The electro-Fenton and electro-catalysis synergistic unit of Example 3;

[0039] Figure 8 The electro-Fenton and electro-catalysis synergistic unit of Example 4;

[0040] Figure 9 The electro-Fenton and electro-catalysis synergistic unit of Comparative Example 3;

[0041] Figure 10 COD removal rates of different structures of Example 4 and Comparative Example 3 on coking wastewater;

[0042] Figure 11 The electro-Fenton and electro-catalysis synergistic unit of Example 5;

[0043] Figure 12 The electro-Fenton and electro-catalysis synergistic unit of Comparative Example 4;

[0044] Figure 13 COD removal rates of different structures of Example 5 and Comparative Example 4 on coking wastewater;

[0045] Figure 14Electro-Fenton and electro-catalysis synergistic unit for example 6;

[0046] Figure 15 Electro-Fenton and electro-catalysis synergistic unit for example 7;

[0047] Figure 16 Degradation rate of 2,3-dichlorobutyric acid aqueous solution with concentration of 30 mg / L by different comb tooth length of electro-Fenton and electro-catalysis synergistic unit for example 8 and comparative example 5;

[0048] Figure 17 Electro-Fenton and electro-catalysis synergistic unit for example 9;

[0049] In the figure, 1 is a comb / grid electrode, 2 is a plane / net electrode, 3 is a reaction device, 4 is a power supply, 5 is an aeration device, 6 is a water inlet, 7 is a water outlet, and 8 is a stirring device. DETAILED DESCRIPTION

[0050] The present application provides an electro-Fenton and electro-catalysis reinforced synergistic unit, which is composed of a plane / net electrode and a comb / grid electrode, and the plane / net electrode and the comb / grid electrode are arranged in parallel in each synergistic unit.

[0051] In the reaction device, the reaction device wall, the plane / net electrode and the comb / grid electrode are sequentially arranged from outside to inside.

[0052] The arrangement mode of the synergistic unit is of three types: the first type is that the synergistic units form a closed loop along the reaction device wall; the second type is that a plurality of non-connected synergistic units are arranged along the reaction device wall, and the number n of the synergistic units is greater than or equal to 1; and the third type is a combination of the first type and the second type.

[0053] The electro-Fenton and electro-catalysis reinforced synergistic unit comprises a plane / net cathode and a comb / grid anode, or the electro-Fenton and electro-catalysis reinforced synergistic unit comprises a plane / net anode and a comb / grid cathode.

[0054] The electro-Fenton and electro-catalysis reinforced synergistic unit of the present application is fixed in the reaction device, the same electrodes are connected by metal wires, and the anode and the cathode are respectively connected to the positive and negative poles of the power supply through wires; the wastewater is pumped into the reaction device from the water inlet and discharged from the water outlet.

[0055] In the present application, the closed loop formed by the plane / net electrode and the comb / grid electrode along the reaction device wall is a head-to-tail structure.

[0056] In the present application, the number of non-connected plane / net electrodes and non-connected comb / grid electrodes is independently preferably 2-10, and further preferably 3-5.

[0057] In the present application, the surface of the synergic unit is preferably flat and / or arc-shaped; the distance between the surface of the surface / mesh electrode and the surface of the comb / grid electrode is preferably 1-50 mm, more preferably 3-40 mm, and even more preferably 10-25 mm.

[0058] In the present application, the distance between the surface of the surface / mesh electrode and the surface of the comb / grid electrode is the distance between the cathode and the anode; the surface includes various surface bodies, such as plate-shaped (straight shape) and non-plate-shaped (e.g., arc-shaped).

[0059] In the present application, the ratio of the length of the comb teeth / grid bars in the comb / grid electrode to the length of the corresponding surface / mesh electrode is preferably 0.05-1:1, more preferably 0.2-0.9:1, and even more preferably 0.3-0.8:1; the gap of the comb teeth / grid bars is preferably 1-50 mm, more preferably 3-40 mm, and even more preferably 10-25 mm; the width of the comb teeth / grid bars is preferably 1-50 mm, more preferably 3-40 mm, and even more preferably 10-25 mm.

[0060] In the present application, the transverse ribs of the grid electrode in the comb / grid electrode preferably include conductive transverse ribs or non-conductive transverse ribs, and the distance between the transverse ribs is preferably 1-500 mm, more preferably 15-400 mm, and even more preferably 35-90 mm.

[0061] The conductive transverse ribs preferably include one or more of titanium ribs, titanium-based ruthenium iridium ribs, titanium-based lead dioxide ribs, and titanium-based tin antimony ribs; the non-conductive transverse ribs preferably include one or more of alumina ribs, zirconia ribs, and silicon carbide ribs.

[0062] In the present application, both the conductive material and the non-conductive material can serve as a support to prevent the deformation of the grid electrode, and the non-conductive material can prevent the short circuiting of the cathode and the anode.

[0063] In the present application, the cross section of the comb teeth / grid bars in the comb / grid electrode is preferably one or more of circular, semi-circular, elliptical, square, rectangular, parallelogram, arched, rhombic, trapezoidal, triangular, pentagonal, hexagonal, wavy, V-shaped, semi-V-shaped, U-shaped, semi-U-shaped, and X-shaped cross section.

[0064] The cross section of the reaction device is preferably circular, rectangular, square, triangular, pentagonal, or hexagonal.

[0065] In the present application, the comb / grid electrode is a comb electrode or a grid electrode, and the surface / mesh electrode is a surface electrode or a mesh electrode.

[0066] In the present application, when the pollutants are benzene ring-containing compounds, the electro-Fenton and electro-catalysis enhanced type synergistic unit preferably comprises a surface / mesh cathode matched with a comb / grid anode; when the pollutants are chain alkane-containing compounds, the electro-Fenton and electro-catalysis enhanced type synergistic unit preferably comprises a surface / mesh anode matched with a comb / grid cathode.

[0067] In the present application, the benzene ring-containing compounds preferably comprise chlorophenol, fluorophenol, bromophenol, iodophenol, nitrobenzene or phenol, and the chain alkane-containing compounds preferably comprise chloroacetic acid, chlorobutyric acid, bromoacetic acid or bromobutyric acid.

[0068] In the present application, the cathode preferably comprises a homogeneous electro-Fenton cathode or a heterogeneous electro-Fenton cathode; the homogeneous electro-Fenton cathode preferably comprises a metal material electrode or a carbon material electrode; the heterogeneous electro-Fenton cathode preferably comprises an electrode obtained by impregnating a transition metal into a homogeneous electro-Fenton material, the transition metal preferably comprises iron, nickel, copper, manganese, cobalt, silver, platinum, gold, zinc and cadmium, and the homogeneous electro-Fenton material preferably comprises a metal material or a carbon material.

[0069] The anode preferably comprises a noble metal anode, a DSA anode or a carbon anode.

[0070] The metal material preferably comprises one or more of iron, nickel, copper, manganese, cobalt, silver, platinum, gold, zinc and cadmium; the carbon material preferably comprises diamond, graphite, amorphous carbon or modified carbon.

[0071] The amorphous carbon preferably comprises wood-based activated carbon, shell-based activated carbon, coal-based activated carbon, regenerated carbon, iron oxychloride-modified activated carbon or petroleum-based activated carbon; the modified carbon preferably comprises heteroatom-modified carbon, and the heteroatom preferably comprises one or more of fluorine, nitrogen, phosphorus and sulfur.

[0072] The iron oxide preferably comprises Fe2O3, Fe3O4 or FeOOH; the iron oxychloride preferably comprises FeOCl; and the transition metal preferably comprises one or more of iron, nickel, copper, manganese, cobalt, silver, platinum, gold, zinc and cadmium.

[0073] The noble metal preferably comprises one or more of gold, silver, platinum, ruthenium, rhodium, palladium, osmium and iridium; the carbon anode preferably comprises a coke anode, a graphite anode or a diamond anode; and the DSA anode preferably comprises a titanium-based ruthenium-iridium electrode, a titanium-based iridium-tantalum electrode, a titanium-based lead dioxide electrode or a titanium-based tin-antimony electrode.

[0074] In the present application, the electro-Fenton and electro-catalysis enhanced type synergistic unit is provided with an aeration device on the side, preferably an aeration device provided below the positive side of the comb / grid anode or the comb / grid cathode, air, oxygen or a mixture of air and oxygen is introduced into the electro-Fenton and electro-catalysis enhanced type synergistic unit through the aeration device, and the flow rate of the aeration is preferably 50-800 mL / min, further preferably 100-700 mL / min, and more preferably 200-600 mL / min.

[0075] The stirring device is arranged at the side of the comb / grid electrode, and the height of the stirring device can be adjusted; the distance between the stirring device and the water surface and the ratio of the water depth are preferably 0.01-0.99:1, further preferably 0.1-0.8:1, and more preferably 0.3-0.7:1.

[0076] In the application, the aeration device supplies oxygen for the system while improving the mass transfer effect of the wastewater in the reaction system; the aeration device arranged below the side of the comb / grid electrode supplies air while cooperating with the stirring device arranged at the side of the comb / grid electrode to strengthen the mass transfer effect of the wastewater between the cathode and the anode, thereby improving the efficiency of the synergistic degradation.

[0077] In the application, the current density is preferably 1-70 mA / cm 2 , further preferably 10-60 mA / cm 2 , and more preferably 20-40 mA / cm 2 .

[0078] The application further provides the application of the electro-Fenton and electro-catalysis intensified synergistic unit in water treatment.

[0079] The reaction device comprising the electro-Fenton and electro-catalysis intensified synergistic unit comprises a comb / grid electrode 1, a surface / net-shaped electrode 2, a reaction device 3, a power supply 4, an aeration device 5, a water inlet 6, a water outlet 7, and a stirring device 8.

[0080] The electro-Fenton and electro-catalysis intensified synergistic unit comprises the surface / net-shaped electrode 2 and the comb / grid electrode 1 parallel to the surface / net-shaped electrode 2, and a plurality of (n≥1) synergistic units are fixed in the reaction device 3. The electro-Fenton and electro-catalysis intensified synergistic unit can comprise two types: the first type is the surface / net-shaped cathode cooperating with the comb / grid-shaped anode parallel to the surface / net-shaped cathode, and the second type is the surface / net-shaped anode cooperating with the comb / grid-shaped cathode parallel to the surface / net-shaped anode. In the reaction device 3, the synergistic unit can be arranged in three types: the first type is that the synergistic units form a closed loop along the wall of the reaction device; the second type is that a plurality of non-connected synergistic units are arranged along the wall of the reaction device, and the number of the synergistic units is n≥1; when n=1, the synergistic unit is arranged alone, and when n≥2, the surface / net-shaped electrode and the comb / grid-shaped electrode are arranged in parallel in each synergistic unit; and the third type is a combination of the first type and the second type.

[0081] In the application, when the first type of electro-Fenton and electro-catalysis intensified synergistic unit is used, the comb / grid-shaped anode is connected to the positive electrode of the power supply 4, and the surface / net-shaped cathode is connected to the negative electrode of the power supply 4; when the second type of electro-Fenton and electro-catalysis intensified synergistic unit is used, the comb / grid-shaped cathode is connected to the negative electrode of the power supply 4, and the surface / net-shaped anode is connected to the positive electrode of the power supply 4.

[0082] In the application, the electro-Fenton and electro-catalysis reinforced synergistic unit is provided with an aeration device 5 on the side, preferably provided with the aeration device 5 below the positive side of the comb / grid-shaped anode or below the positive side of the comb / grid-shaped cathode, air, oxygen or mixed gas of oxygen and air is exposed to the electro-Fenton and electro-catalysis synergistic system through the aeration device, and the gas flow is adjusted, so that the mass transfer effect of the wastewater in the reaction system is promoted while oxygen is supplied to the system; the stirring device 8 is provided on the side of the comb / grid-shaped electrode 1, and the height of the stirring device 8 can be adjusted; the reaction device 3 is provided with a water inlet 6 connected with an external water inlet pipeline and a water outlet 7 connected with an external water outlet pipeline; after the device is successfully installed, the power supply 4 is turned on, so that the electro-Fenton and electro-catalysis synergistic degradation reaction is carried out.

[0083] The fine regulation method of the electro-Fenton and electro-catalysis reinforced synergistic unit of the application can select different kinds of electro-Fenton and electro-catalysis reinforced synergistic units according to the specific shape and size of the reaction device, and regulate the shape, size, group number and arrangement position of the reinforced synergistic unit; on this basis, the cross-sectional shape, width and gap of the comb teeth / grid strips of the comb / grid-shaped electrode, the distance between the positive and negative electrode surfaces, the electrode material and the property of the electrode are regulated, so that the system is suitable for efficient synergistic degradation of different wastewaters. The specific operation method is as follows:

[0084] 1) According to the different (size, shape) of the reaction device, the shape, size, group number and arrangement position of the electro-Fenton and electro-catalysis reinforced synergistic unit are determined.

[0085] 2) When the pollutants in the wastewater are benzene ring-containing compounds, for example: chlorophenol, fluorophenol, bromophenol, iodophenol, nitrobenzene and phenol, the main active substance for degradation is hydroxyl radical (·OH), and the efficiency of the system for synergistically degrading pollutants mainly depends on the yield of hydroxyl radical (·OH), and a larger cathode area is beneficial to the generation of hydroxyl radical (·OH), so a surface / net-shaped cathode is needed to cooperate with a comb / grid-shaped anode as a synergistic unit to carry out electro-Fenton and electro-catalysis synergistic degradation reaction; when the pollutants are chain alkane-containing compounds, for example: chloroacetic acid, chlorobutyric acid, bromoacetic acid and bromobutyric acid, anodic oxidation is the main degradation pathway, and a larger anode area is beneficial to the degradation of pollutants, so a surface / net-shaped anode is needed to cooperate with a comb / grid-shaped cathode as a synergistic unit to carry out electro-Fenton and electro-catalysis synergistic degradation reaction.

[0086] 3) By regulating the number of comb teeth / barriers, cross-sectional shape, cross-sectional width and comb teeth / barrier gap, on the one hand, the electric field distribution between the anode and the cathode can be regulated, so that the electric field distribution of the comb / barrier electrode matching surface / mesh electrode in the system is close to the electric field distribution when the traditional surface / mesh electrode matching surface / mesh electrode is used; on the other hand, under the condition of the same electrode spacing, the system obtains more optimal flow field conditions, and thus the mass transfer resistance of the system is significantly lower than that when the traditional surface / mesh electrode matching surface / mesh electrode is used, which is beneficial to the wastewater entering the anode and the cathode to occur the synergistic degradation reaction.

[0087] 4) When the electro-Fenton and electro-catalysis enhanced synergistic unit is used, on the one hand, in the synergistic unit, the structure of the surface / mesh electrode and the parallel comb / barrier electrode is used, according to the structural characteristics of the comb / barrier electrode, the wastewater is easily introduced from the side of the comb / barrier electrode, and the stirring device and the aeration device are used to strengthen the mass transfer of the wastewater from the comb / barrier electrode side into the anode and the cathode; on the other hand, by means of the comb / barrier electrode structure, the electric field law is used, so that the distance between the anode and the cathode can be smaller, and thus the operating voltage and the processing energy consumption are lower, and by means of the above two aspects, the "enhanced" synergistic degradation is realized.

[0088] The technical solutions provided by the present application will be described in detail below in combination with the embodiments, but they should not be understood as limiting the scope of protection of the present application.

[0089] Example 1

[0090] The electro-Fenton and electro-catalysis enhanced synergistic unit uses one synergistic unit, the cathode uses a cylindrical iron oxychloride modified activated carbon electrode with a size of 400 mm x 100 mm, the anode uses a titanium-based ruthenium-iridium comb electrode, the comb teeth are parallel to the cathode in the axial direction, the cross section of the comb teeth is circular, the ratio of the length of the comb teeth to the length of the corresponding surface cathode is 1:1, the comb teeth gap is 5 mm, the comb teeth width is 2 mm, the distance between the cathode and the anode is 4 mm, the same electrodes are connected by copper wires, the anode and the cathode are connected with the positive and negative poles of the external power source through wires, respectively, air is introduced into the electro-Fenton and electro-catalysis system through the aeration device, the aeration flow rate is 500 mL / min, the stirring device is arranged on the side of the comb electrode, the ratio of the distance between the stirring device and the water surface to the water depth in the container is 0.5:1, the external power source is turned on, and the coking wastewater with a chemical oxygen demand (COD) of 1200 mg / L (mainly containing phenolic compounds and heterocyclic compounds) is subjected to electro-Fenton and electro-catalysis synergistic degradation. Under the condition of the current density of 10 mA / cm 2 , the coking wastewater is degraded for 2 h under the condition of continuously introducing air.

[0091] The electro-Fenton and electro-catalysis synergistic unit of the present example is shown in Figure 1 .

[0092] Comparative Example 1

[0093] The titanium-based ruthenium iridium comb-shaped anode in Example 1 was replaced by a titanium-based ruthenium iridium cylindrical anode, which was placed in parallel inside the cylindrical cathode, and other conditions were the same as in Example 1. The chemical oxygen demand of the coking wastewater was 1200 mg / L. The electro-Fenton and electro-catalysis synergistic degradation was carried out for 2 h.

[0094] The electro-Fenton and electro-catalysis synergistic unit of the present comparative example is shown in Figure 2 .

[0095] The removal rates of the coking wastewater COD of the different structures of Example 1 and Comparative Example 1 are shown in Figure 3 . Figure 3 It can be known that the removal rate of the coking wastewater COD of Example 1 is 100%, and the removal rate of the coking wastewater COD of Comparative Example 1 is 61%. Therefore, it is concluded that the mass transfer effect of the structure system of Example 1 is better than that of the structure system of Comparative Example 1, and the former removal effect is obviously better than that of the latter.

[0096] Example 2

[0097] The electro-Fenton and electro-catalysis enhanced synergistic unit adopts two identical synergistic units. In the synergistic unit, the cathode adopts an arc-shaped oxygen-based iron chloride modified activated carbon electrode with a size of 100 mm x 100 mm, and the anode adopts a titanium-based ruthenium iridium grid-shaped electrode. The grid strip axis is parallel to the cathode, and is arranged on both sides of the reaction device. The cross section of the grid strip is semicircular. The ratio of the length of the grid strip to the length of the corresponding planar cathode is 1:1. The transverse rib is made of titanium-based ruthenium iridium material. The spacing of the transverse rib is 50 mm. The gap between the grid strips is 6 mm. The width of the grid strip is 2 mm. The spacing between the cathode and the anode is 3 mm. The same electrodes are connected by copper wires. The anode and the cathode are connected to the positive and negative poles of the external power source through wires, respectively. The electro-Fenton and electro-catalysis system is exposed to air through the aeration device, and the aeration flow rate is 500 mL / min. A stirring device is arranged on the side of the grid-shaped electrode. The ratio of the distance between the stirring device and the water surface to the water depth in the container is 0.5:1. The external power source is turned on. The electro-Fenton and electro-catalysis synergistic degradation of the coking wastewater (mainly containing phenolic compounds and heterocyclic compounds) with a chemical oxygen demand of 600 mg / L is carried out. The coking wastewater is degraded for 70 min under the condition of a current density of 10 mA / cm 2 .

[0098] The electro-Fenton and electro-catalysis synergistic unit of the present example is shown in Figure 4 .

[0099] Comparative Example 2

[0100] The titanium-based ruthenium iridium grid-shaped anode in Example 2 was replaced by a titanium-based ruthenium iridium arc surface anode, which was parallel to the cathode. Other conditions were the same as in Example 2. The electro-Fenton and electro-catalysis synergistic degradation of the coking wastewater with a chemical oxygen demand of 600 mg / L was carried out for 70 min.

[0101] The electro-Fenton and electrocatalytic synergistic unit in this comparative example is as follows: Figure 5 As shown.

[0102] The COD removal rates of different structures in Example 2 and Comparative Example 2 on coking wastewater are as follows: Figure 6 As shown, by Figure 6 It can be seen that Example 2 achieved a 100% COD removal rate from coking wastewater, while Comparative Example 2 achieved a 64% COD removal rate. Therefore, the structural system of Example 2 exhibits better mass transfer performance than that of Comparative Example 2, with the former showing significantly superior removal efficiency.

[0103] Example 3

[0104] The electro-Fenton and electrocatalytic enhancement synergistic unit employs two synergistic units. In one synergistic unit, the cathode is a 100mm × 100mm arc-shaped ferric chloride-modified activated carbon electrode, and the anode is a titanium-based ruthenium-iridium grid electrode with the grid bars axially parallel to the cathode. In the other synergistic unit, the cathode is a 100mm × 100mm plate-shaped ferric chloride-modified activated carbon electrode, and the anode is a titanium-based ruthenium-iridium grid electrode with the grid bars parallel to the cathode. The two synergistic units are respectively located on both sides of the reaction device. The grid bars have a semi-circular cross-section, and the ratio of the grid bar length to the corresponding planar cathode length is 0.9:1. The transverse ribs are titanium-based ruthenium-iridium. The materials used have a horizontal rib spacing of 50 mm, a grid bar spacing of 6 mm, a grid bar width of 2 mm, and a cathode and anode spacing of 3 mm. The electrodes of the same polarity are connected by copper wire. The anode and cathode are connected to the positive and negative terminals of an external power supply via wires, respectively. An aeration device is used to introduce air into the electro-Fenton and electrocatalytic system at a flow rate of 500 mL / min. A stirring device is installed on the side of the grid electrodes, with the distance between the stirring device and the water surface being 0.5:1 relative to the water depth in the container. The external power supply is turned on to perform electro-Fenton and electrocatalytic synergistic degradation on coking wastewater (mainly containing phenols and heterocyclic compounds) with a chemical oxygen demand of 600 mg / L. The current density is 10 mA / cm². 2 Under continuous air exposure, the coking wastewater was degraded for 70 minutes.

[0105] The electro-Fenton and electrocatalytic synergistic unit in this embodiment is as follows: Figure 7 As shown in the figure. The results indicate that the COD removal rate of the coking wastewater was 99%, which is similar to the effect in Example 2.

[0106] Example 4

[0107] The electro-Fenton and electro-catalysis enhanced synergistic unit adopts one synergistic unit, the cathode adopts a four-face-shaped oxygen-based ferric chloride modified activated carbon electrode with a size of 400 mm x 100 mm, the anode adopts a titanium-based lead dioxide comb-shaped electrode, the comb teeth are parallel to the cathode, the cross section of the comb teeth is circular, the ratio of the length of the comb teeth to the length of the corresponding face-shaped cathode is 1:1, the gap between the comb teeth is 5 mm, the width of the comb teeth is 3 mm, the distance between the cathode and the anode is 3 mm, the same electrodes are connected by copper wires, the anode and the cathode are connected with the positive and negative poles of the external power source through wires, air is blown into the electro-Fenton and electro-catalysis system through the aeration device, the aeration flow rate is 500 mL / min, a stirring device is arranged on the side of the comb-shaped electrode, the ratio of the distance between the stirring device and the water surface to the water depth in the container is 0.5:1, the external power source is turned on, and the electro-Fenton and electro-catalysis synergistic degradation of coking wastewater (mainly containing phenolic compounds and heterocyclic compounds) with a chemical oxygen demand of 1200 mg / L is carried out. Under the condition of continuous aeration, the coking wastewater is degraded for 120 min at a current density of 15 mA / cm 2 .

[0108] The electro-Fenton and electro-catalysis synergistic unit of the present embodiment is shown in Figure 8 .

[0109] Comparative Example 3

[0110] The titanium-based lead dioxide comb-shaped anode in Example 4 is replaced with a titanium-based lead dioxide four-face-shaped anode, which is placed parallel inside the cathode, and other conditions are the same as in Example 4. The electro-Fenton and electro-catalysis synergistic degradation of coking wastewater with a chemical oxygen demand of 1200 mg / L is carried out for 120 min.

[0111] The electro-Fenton and electro-catalysis synergistic unit of the present embodiment is shown in Figure 9 .

[0112] The COD removal rates of the coking wastewater in Example 4 and Comparative Example 3 are shown in Figure 10 . As can be seen from Figure 10 , the COD removal rate of wastewater in Example 4 is 100%, and the COD removal rate of wastewater in Comparative Example 3 is 59%, thus it is concluded that the mass transfer effect of the structural system in Example 4 is better than that in Comparative Example 3, and the former removal effect is obviously better than the latter.

[0113] Example 5

[0114] The electro-Fenton and electro-catalysis enhanced synergistic unit adopts two identical synergistic units. The cathode adopts a plate-shaped oxygen-based ferric chloride modified activated carbon electrode with a size of 100 mm x 100 mm. The anode adopts a titanium-based ruthenium-iridium comb-shaped electrode. The comb teeth are parallel to the cathode and are arranged on both sides of the reaction device. The cross section of the comb teeth is elliptical. The ratio of the length of the comb teeth to the length of the corresponding planar cathode is 1:1. The gap between the comb teeth is 5 mm. The width of the comb teeth is 3 mm. The distance between the cathode and the anode is 2 mm. The same electrodes are connected by copper wires. The anode and the cathode are connected to the positive and negative poles of the external power source through wires, respectively. Air is introduced into the electro-Fenton and electro-catalysis system through the aeration device at a flow rate of 500 mL / min. A stirring device is arranged on the side of the comb-shaped electrode. The ratio of the distance between the stirring device and the water surface to the water depth in the container is 0.5:1. The external power source is turned on. The electro-Fenton and electro-catalysis synergistic degradation of coking wastewater (mainly containing phenolic compounds and heterocyclic compounds) with a chemical oxygen demand of 600 mg / L is carried out. The current density is 15 mA / cm 2 , and the coking wastewater is degraded for 60 min under the condition of continuous air exposure.

[0115] The electro-Fenton and electro-catalysis synergistic unit of the present embodiment is as shown in Figure 11 .

[0116] Comparative Example 4

[0117] The titanium-based ruthenium-iridium comb-shaped anode in Example 5 is replaced with a titanium-based ruthenium-iridium plate-shaped anode, which is parallel to the cathode. The other conditions and Example 5 are the same. The electro-Fenton and electro-catalysis synergistic degradation of coking wastewater with a chemical oxygen demand of 600 mg / L is carried out for 60 min.

[0118] The electro-Fenton and electro-catalysis synergistic unit of the present comparative example is as shown in Figure 12 .

[0119] The COD removal rates of the coking wastewater in Example 5 and Comparative Example 4 with different structures are as shown in Figure 13 . As can be seen from Figure 13 , the COD removal rate of wastewater in Example 5 is 100%, and the COD removal rate of wastewater in Comparative Example 4 is 70%. Therefore, the mass transfer effect of the structural system in Example 5 is better than that in Comparative Example 4. The removal effect of the former is obviously better than that of the latter.

[0120] Example 6

[0121] The electro-Fenton and electro-catalysis enhanced synergistic unit adopts one synergistic unit, the cathode adopts a plate-shaped oxygen-based ferric chloride modified activated carbon electrode with a size of 100 mm x 100 mm, the anode adopts a titanium-based ruthenium-iridium comb-shaped electrode, the comb teeth are parallel to the cathode along the horizontal direction, the cross section of the comb teeth is circular, the ratio of the length of the comb teeth to the length of the corresponding planar cathode is 0.9:1, the gap between the comb teeth is 5 mm, the width of the comb teeth is 3 mm, the distance between the cathode and the anode is 2 mm, the same electrodes are connected by copper wires, the anode and the cathode are connected to the positive and negative poles of the external power source through wires, air is introduced into the electro-Fenton and electro-catalysis system through an aeration device, the aeration flow rate is 500 mL / min, a stirring device is arranged on the side of the comb-shaped electrode, the ratio of the distance between the stirring device and the water surface to the water depth in the container is 0.5:1, the external power source is turned on, and the electro-Fenton and electro-catalysis synergistic degradation of a rhodamine B aqueous solution with a chemical oxygen demand of 30 mg / L is carried out. Under the condition of continuously introducing air, rhodamine B is degraded for 30 min at a current density of 15 mA / cm 2 .

[0122] The electro-Fenton and electro-catalysis synergistic unit of the present embodiment is shown in Figure 14 . The results show that the degradation rate of rhodamine B reaches 100%.

[0123] Example 7

[0124] The electro-Fenton and electro-catalysis enhanced synergistic unit adopts five synergistic units, the cathode adopts a plate-shaped oxygen-based ferric chloride modified activated carbon electrode with a size of 100 mm x 100 mm, the anode adopts a titanium-based ruthenium-iridium comb-shaped electrode, the cross section of the comb teeth is circular, the ratio of the length of the comb teeth to the length of the corresponding planar cathode is 0.8:1, the gap between the comb teeth is 5 mm, the width of the comb teeth is 3 mm, the distance between the cathode and the anode is 2 mm, the same electrodes are connected by copper wires, the anode and the cathode are connected to the positive and negative poles of the external power source through wires, air is introduced into the electro-Fenton and electro-catalysis system through an aeration device, the aeration flow rate is 500 mL / min, a stirring device is arranged on the side of the comb-shaped electrode, the ratio of the distance between the stirring device and the water surface to the water depth in the container is 0.5:1, the external power source is turned on, and the electro-Fenton and electro-catalysis synergistic degradation of coking wastewater (mainly containing phenolic compounds and heterocyclic compounds) with a chemical oxygen demand of 720 mg / L is carried out. Under the condition of continuously introducing air, the coking wastewater is degraded for 50 min at a current density of 10 mA / cm 2 .

[0125] The electro-Fenton and electro-catalysis synergistic unit of the present embodiment is shown in Figure 15 . The results show that the removal rate of the COD of the coking wastewater is 100%.

[0126] Example 8

[0127] The electro-Fenton and electrocatalytic enhanced synergistic unit employs two identical synergistic units. The anode is a 100mm × 100mm plate-shaped titanium-based ruthenium-iridium electrode, and the cathode is a comb-shaped electrode made of ferric chloride-modified activated carbon. The comb teeth are parallel to the anode and are positioned on both sides of the reaction device. The cross-section of the comb teeth is rectangular, with a tooth length to corresponding anode length ratio of 0.9:1, a tooth gap of 5mm, and a tooth width of 3mm. The distance between the cathode and anode is 3mm. Electrodes of the same polarity are connected by copper wire. The anode and cathode are connected to the positive and negative terminals of an external power supply via wires, respectively. Air is introduced into the electro-Fenton and electrocatalytic system through an aeration device at a flow rate of 500mL / min. A stirring device is placed beside the comb-shaped electrode, with the distance between the stirring device and the water surface in a ratio of 0.5:1 to the water depth in the container. The external power supply is turned on, and electro-Fenton and electrocatalytic synergistic degradation of a 30mg / L 2,3-dichlorobutyric acid aqueous solution is performed at a current density of 10mA / cm². 2 2,3-Dichlorobutyric acid was degraded for 30 minutes under continuous air exposure.

[0128] Comparative Example 5

[0129] The ratio of comb tooth length to corresponding planar anode length in Example 8 was changed to 1:1, and other conditions were the same as in Example 8. Electro-Fenton and electrocatalytic synergistic degradation of 30 mg / L 2,3-dichlorobutyric acid aqueous solution was carried out for 30 min.

[0130] The degradation rates of 2,3-dichlorobutyric acid aqueous solution with a concentration of 30 mg / L for different comb tooth lengths in Examples 8 and Comparative Example 5 are as follows: Figure 16 As shown, by Figure 16 It can be seen that the degradation rate of 2,3-dichlorobutyric acid aqueous solution in Example 8 was 99.7%, and the degradation rate of 2,3-dichlorobutyric acid aqueous solution in Comparative Example 5 was 90.2%.

[0131] Example 9

[0132] The electro-Fenton and electrocatalytic enhancement synergistic unit employs two synergistic units. In one synergistic unit, the cathode is a 400mm × 100mm cylindrical oxy-ferric chloride modified activated carbon electrode, and the anode is a titanium-based ruthenium-iridium comb-shaped electrode with the comb teeth axially parallel to the cathode. This synergistic unit is arranged along the reaction tank. In the other synergistic unit, the cathode is an 80mm × 100mm plate-shaped oxy-ferric chloride modified activated carbon electrode, and the anode is a titanium-based ruthenium-iridium comb-shaped electrode with the comb teeth parallel to the cathode. This synergistic unit is arranged inside the cylindrical synergistic unit. The comb teeth have a circular cross-section, and the ratio of the comb tooth length to the corresponding planar cathode length is... The ratio of the electrodes was 1:1, the gap between the comb teeth was 5mm, the width of the comb teeth was 2mm, the distance between the cathode and anode was 4mm, and the electrodes of the same polarity were connected by copper wire. The anode and cathode were connected to the positive and negative terminals of an external power supply by wires, respectively. Air was introduced into the electro-Fenton and electrocatalytic system through an aeration device at a flow rate of 500mL / min. A stirring device was installed on the side of the comb-shaped electrodes, and the ratio of the distance between the stirring device and the water surface to the water depth in the container was 0.5:1. The external power supply was turned on to perform electro-Fenton and electrocatalytic synergistic degradation on coking wastewater (mainly containing phenols and heterocyclic compounds) with a chemical oxygen demand (COD) of 1200mg / L. The current density was 10mA / cm². 2 Under continuous air exposure, the coking wastewater was degraded for 1.8 hours.

[0133] The electro-Fenton and electrocatalytic synergistic unit in this embodiment is as follows: Figure 17 As shown, the results indicate that the COD removal rate of coking wastewater reached 100%.

[0134] The electro-Fenton and electrocatalytic enhanced synergistic unit of this invention consists of a surface / mesh electrode and a comb / grid electrode parallel to it. The cathode and anode are connected to a power source via wires. An aeration device and a stirring device are installed in the reaction device to perform electro-Fenton and electrocatalytic synergistic enhanced degradation of wastewater. Firstly, this invention utilizes the comb / grid electrode structure to facilitate wastewater entry through the comb / grid electrodes. This leverages fluid dynamics principles, cleverly solving the problem of increased mass transfer resistance caused by the reduced distance between the anode and cathode through the combined use of the surface / mesh electrode and the parallel comb / grid electrode. Secondly, this invention utilizes the laws of electric field distribution and fluid dynamics to achieve a smaller electrode spacing (i.e., the mass transfer distance between the anode and cathode) while simultaneously obtaining lower operating voltage, lower processing energy consumption, and better mass transfer performance. Thirdly, while shortening the mass transfer distance between the anode and cathode, this invention also enhances the mass transfer between the two electrodes through stirring. The "enhanced" synergistic unit proposed in this invention utilizes the above three aspects to achieve "enhanced" synergistic degradation, which helps to improve synergistic degradation efficiency and reduce operating costs.

[0135] The above merely describes the preferred embodiments of the present application, and it should be pointed out that, for those skilled in the art, several improvements and refinements can be made without departing from the principles of the present application, and these improvements and refinements should also be considered as falling within the protection scope of the present application.

Claims

1. An electro-Fenton and electro-catalytic enhanced synergistic unit, characterized in that, The electro-Fenton and electro-catalysis reinforced synergistic unit is composed of a plane / net electrode and a comb / grid electrode, and the plane / net electrode and the comb / grid electrode are arranged in parallel in each synergistic unit; In the reaction device, from outside to inside, there are in sequence a reaction device wall, a plane / net electrode, and a comb / grid electrode; The arrangement mode of the synergistic unit is of three types: the first type is that the synergistic units form a closed loop along the reaction device wall; the second type is that a plurality of non-connected synergistic units are arranged along the reaction device wall, and the number n of the synergistic units is greater than or equal to 1; and the third type is a combination of the first type and the second type; The electro-Fenton and electro-catalysis reinforced synergistic unit comprises a plane / net cathode and a comb / grid anode, or the electro-Fenton and electro-catalysis reinforced synergistic unit comprises a plane / net anode and a comb / grid cathode; The distance between the plane on which the plane / net electrode is located and the plane on which the comb / grid electrode is located is 1-50 mm; When the pollutants are benzene ring-containing compounds, the electro-Fenton and electro-catalysis reinforced synergistic unit is a plane / net cathode combined with a comb / grid anode; and when the pollutants are chain alkane-containing compounds, the electro-Fenton and electro-catalysis reinforced synergistic unit is a plane / net anode combined with a comb / grid cathode.

2. The electro-Fenton and electrocatalytic enhanced synergistic unit according to claim 1, characterized in that, The plane formed by the synergistic units is of a flat plate type and / or an arc surface type.

3. The electro-Fenton and electrocatalytic enhanced synergistic unit according to claim 1 or 2, characterized in that, The ratio of the length of the comb teeth / grid strips in the comb / grid electrode to the length of the corresponding plane / net electrode is 0.05-1:1, the gap between the comb teeth / grid strips is 1-50 mm, and the width of the comb teeth / grid strips is 1-50 mm.

4. The electro-Fenton and electrocatalytic enhanced synergistic unit according to claim 3, characterized in that, The transverse ribs of the grid electrode in the comb / grid electrode include conductive transverse ribs or non-conductive transverse ribs, and the distance between the transverse ribs is 1-500 mm; The conductive transverse ribs include one or more of titanium ribs, titanium-based ruthenium iridium ribs, titanium-based lead dioxide ribs, and titanium-based tin antimony ribs; and the non-conductive transverse ribs include one or more of aluminum oxide ribs, zirconium oxide ribs, and silicon carbide ribs.

5. The electro-Fenton and electrocatalytic enhanced synergistic unit of claim 3, wherein, In the comb / grid electrode, the cross section of the comb teeth / grid strips is one or more of a circular cross section, a semi-circular cross section, an elliptical cross section, a square cross section, a rectangular cross section, a parallelogram cross section, an arch cross section, a diamond cross section, a trapezoidal cross section, a triangular cross section, a pentagonal cross section, a hexagonal cross section, a wave cross section, a V-shaped cross section, a semi-V-shaped cross section, a U-shaped cross section, a semi-U-shaped cross section, and an X-shaped cross section. The cross section of the reaction device is a circular cross section, a rectangular cross section, a square cross section, a triangular cross section, a pentagonal cross section, or a hexagonal cross section.

6. The electro-Fenton and electrocatalytic enhanced synergistic unit of claim 5, wherein, The cathode is a homogeneous electro-Fenton cathode or a heterogeneous electro-Fenton cathode; the homogeneous electro-Fenton cathode is a metal material electrode or a carbon material electrode; the heterogeneous electro-Fenton cathode is an electrode obtained by impregnating a transition metal into an oxide and loading the homogeneous electro-Fenton material, the oxide is an iron oxide, an iron-chlorine oxide, or an iron-copper oxide, and the homogeneous electro-Fenton material is a metal material or a carbon material; The anode is a noble metal anode, a DSA anode, or a carbon anode; The metal material comprises one or more of iron, nickel, copper, manganese, cobalt, silver, platinum, gold, zinc, and cadmium; and the carbon material comprises diamond, graphite, amorphous carbon, or modified carbon. The amorphous carbon comprises wood-based activated carbon, fruit shell-based activated carbon, coal-based activated carbon, regenerated carbon, iron oxychloride-modified activated carbon, or petroleum-based activated carbon; and the modified carbon is a heteroatom-modified carbon, and the heteroatom comprises one or more of fluorine, nitrogen, phosphorus, and sulfur. The iron oxide is Fe2O3, Fe3O4 or FeOOH; the iron oxychloride is FeOCl; the transition metal comprises one or more of iron, nickel, copper, manganese, cobalt, silver, platinum, gold, zinc and cadmium; The noble metal comprises one or more of gold, silver, platinum, ruthenium, rhodium, palladium, osmium and iridium; the carbon anode comprises a coke anode, a graphite anode or a diamond anode; the DSA anode comprises a titanium-based ruthenium-iridium electrode, a titanium-based iridium-tantalum electrode, a titanium-based lead dioxide electrode or a titanium-based tin-antimony electrode.

7. The electro-Fenton and electrocatalytic enhanced synergistic unit of claim 5, wherein, An aeration device is arranged below the positive side of the comb / grid-shaped anode or cathode, and air, oxygen or a mixture of air and oxygen is introduced into the electro-Fenton and electro-catalysis enhanced synergistic unit through the aeration device, and the flow rate of the aeration is 50-800 mL / min; A stirring device is arranged on the side of the comb / grid-shaped electrode, and the distance between the stirring device and the water surface is 0.01-0.99:1 of the water depth.

8. The electro-Fenton and electrocatalytic enhanced synergistic unit of claim 7, wherein, Current density is 1-70 mA / cm 2 .

9. Use of the electro-Fenton and electro-catalysis enhanced synergistic unit according to any one of claims 1-8 in water treatment.

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