Method for improving utilization of active chlorine in electrocatalytic treatment of high-salinity wastewater

Abstract

This invention discloses a method for improving the utilization capacity of active chlorine in electrocatalytic treatment of high-salinity wastewater, comprising the following steps: under ultraviolet and / or heat source conditions, high-salinity wastewater is introduced into an electrocatalytic system, and an electrocatalytic reaction is first carried out in a residence state. When 50 μg / cm³ of active chlorine is reached... 2 ≤Active chlorine content FCS≤350μg / cm³ 2 At that time, the high-salinity wastewater was subjected to an electrocatalytic reaction under flowing conditions, and the influent and effluent flow rates of the high-salinity wastewater were controlled to be consistent and maintained at 30 μg / cm³. 2 ≤Active chlorine content FCS<350μg / cm³ 2 The process continues until the high-salinity wastewater is completely treated. The method of this invention has advantages such as simple operation, rapid reaction start-up, cleanliness and efficiency, no need for additional reagents, no secondary pollution, and strong adaptability to operating conditions. It can efficiently degrade antibiotics in high-salinity wastewater.

Description

Technical Field

[0001] This invention belongs to the fields of electrochemical technology and environmental protection, and specifically relates to a method for improving the utilization capacity of active chlorine in electrocatalytic treatment of high-salt wastewater. Background Technology

[0002] Activated chlorine has wide applications in water disinfection, water quality improvement, and pollutant degradation. In high-salinity wastewater treatment, the generation of activated chloride ions can improve wastewater treatment efficiency. Chinese patent document CN113929187A discloses the use of Ti3C2TX material to enhance the oxidation of traditional anodes, generating a large amount of active chlorine and hydroxyl radicals in the catalytic system for the removal of organic pollutants. However, although the Ti3C2TX-enhanced traditional anode electro-oxidation process does not require the addition of additional chemical reagents, the anode material manufacturing process is relatively complex. Chinese patent document CN111233224A discloses an electrochemical advanced oxidation method that synergistically treats wastewater using electro-oxidation and photocatalysis. This method can simultaneously remove nitrogen, phosphorus, antibiotics, and bactericides from aquaculture wastewater, thereby meeting aquaculture wastewater discharge standards. However, this method still suffers from early-stage and operating costs due to power consumption, equipment purchase, and infrastructure construction.

[0003] Electrocatalytic treatment of high-salinity wastewater offers advantages such as no secondary pollution, rapid reaction, and simple operation. This is because electrocatalysis can convert salts in high-salinity systems into desired substances, such as active chlorine. However, studies have found that while electrocatalytic treatment of high-salinity wastewater can generate active chlorine to improve the speed and efficiency of pollutant treatment, it may also pose a risk of perchlorate formation. Therefore, obtaining a clean and efficient method to improve the utilization of active chlorine in electrocatalytic treatment of high-salinity wastewater, while avoiding the formation of high-valent chlorides, is of great significance for the treatment and disinfection of high-salinity organic wastewater. Summary of the Invention

[0004] The technical problem to be solved by the present invention is to overcome the shortcomings of the prior art and provide a method for improving the utilization capacity of active chlorine in electrocatalytic treatment of high-salt wastewater that is simple to operate, has a fast reaction start-up, is clean and efficient, requires no additional reagents, causes no secondary pollution, and is highly adaptable to operating conditions.

[0005] To solve the above-mentioned technical problems, the present invention adopts the following technical solution.

[0006] A method for improving the utilization capacity of active chlorine in electrocatalytic treatment of high-salinity wastewater includes the following steps: under ultraviolet and / or heat source conditions, high-salinity wastewater is introduced into an electrocatalytic system, and an electrocatalytic reaction is carried out first in a residence state. When the concentration of active chlorine reaches 50 μg / cm³, the reaction proceeds to the next step. 2 ≤Active chlorine content FCS≤350μg / cm³ 2At that time, the high-salinity wastewater was subjected to an electrocatalytic reaction under flowing conditions, and the influent and effluent flow rates of the high-salinity wastewater were controlled to be consistent and maintained at 30 μg / cm³. 2 ≤Active chlorine content FCS<350μg / cm³ 2 The process continues until the high-salinity wastewater is completely treated; the electrocatalytic system includes an anode and a cathode, and the cathode material used has a Tafel slope of 80 mV·dec. -1 ~300mV·dec -1 The oxygen evolution potential of the anode material used in the anode is <2.2V.

[0007] The cathode material of this invention has high hydrogen evolution activity, enabling selective hydrogen evolution and reducing the cathodic reduction effect of active chlorine. The anode material of this invention controls the oxygen evolution potential to <2.2V, inhibiting the oxygen evolution reaction, effectively improving the oxidation capacity of chloride ions, and promoting the generation of active chlorine at the anode. The external ultraviolet light and / or heat source of this invention assists in activating chloride ions, thereby promoting the activation rate of chloride ions in a short time. In the electrocatalytic reaction of this invention, the influent and effluent flow rates of high-salt wastewater are kept consistent under flowing conditions, thereby preventing active chlorine from being further oxidized by the anode and converted into toxic high-valence chlorides.

[0008] In the above method, preferably, the volume ratio of the influent flow rate per minute to the reaction volume in the stationary state is 1-20:400.

[0009] In the above method, preferably, the electrocatalytic reaction time in the residence state is 30 min to 60 min.

[0010] In the above method, preferably, when the electrocatalytic reaction is carried out in the flowing state, the influent flow rate and effluent flow rate of the high-salt wastewater are both 1 mL / min to 20 mL / min, and the electrocatalytic reaction time in the flowing state is 60 min to 600 min.

[0011] Preferably, in the above method, the intensity of the ultraviolet light is 10 mW / cm. 2 ~100mW / cm 2 The temperature of the heat source is 20℃~80℃.

[0012] In the above method, preferably, the cathode material includes stainless steel or foamed iron-nickel material, and the anode material includes titanium-based or lead-based material.

[0013] In the above method, preferably, the pH value of the high-salt wastewater is 3.0 to 11.0, the NaCl content in the high-salt wastewater is 1000 mg / L to 60000 mg / L, and the Na2SO4 content in the high-salt wastewater is 1.4 g / L to 7.1 g / L.

[0014] In the above method, preferably, the current density in the electrocatalytic system is 2.7 mA / cm². 2 ~8mA / cm 2 .

[0015] In the above method, preferably, the plate spacing between the anode and the cathode is 2.0cm to 4.0cm, the cathode has a thickness of 1mm to 5mm, a length of 30mm to 100mm, and a width of 30mm to 100mm, and the anode has a thickness of 1mm to 5mm, a length of 30mm to 100mm, and a width of 30mm to 100mm.

[0016] In this invention, FCS stands for Free Chlorine Species.

[0017] In this invention, the cathode material can be a modified three-dimensional cathode material, which refers to a cathode material with a three-dimensional structure that has been treated by surface oxidation, surface coating, surface deposition, or acid-base methods. The anode material is an anode material supported on a catalyst, which can be an anode material supported on a metal-doped catalyst, an anode material supported on a nitrogen-doped catalyst, or an anode material supported on a sulfur-doped catalyst.

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

[0019] (1) This invention discloses a method for improving the utilization capacity of active chlorine in electrocatalytic treatment of high-salt wastewater. The method improves the utilization capacity of active chlorine in high-salt wastewater by screening suitable cathode and anode materials, using heat source and / or ultraviolet light assistance, and continuously treating high-salt wastewater (i.e., the inflow and outflow velocities of high-salt wastewater are kept consistent under flowing conditions). Specifically, the method involves using ultraviolet light and / or heat source assistance to activate chloride ions at an anode with a high oxygen evolution potential to generate a large amount of active chlorine. At the same time, the method involves using a cathode with strong hydrogen evolution activity to avoid the reduction of active chlorine and further improve the retention of active chlorine. Furthermore, the method involves continuous electrocatalytic treatment to remove a large amount of active chlorine from the electrocatalytic system, preventing the active chlorine from being deeply oxidized into perchlorate, while introducing fresh high-salt wastewater to replenish the chloride ion consumption. The anode selected in this invention (with an oxygen evolution potential < 2.2V) satisfies two objectives: improving anodic oxidation activity and reducing the formation of high-valence chlorides. In other words, while strong oxidizing electrodes can rapidly oxidize and degrade pollutants, they also oxidize chloride ions in high-salinity wastewater to a higher degree, easily generating toxic high-valence chlorides. However, the anode selected in this invention has a maximum catalytic activity that helps promote the generation of active chlorine and prevents further oxidation; under the condition of an oxygen evolution potential < 2.2V, the oxygen evolution potential can be as high as possible. Simultaneously, considering that the consumption of active chlorine in the electrocatalytic system mainly occurs during cathode reduction and the oxidation of pollutants by active chlorine, the cathode selected in this invention (with a Tafel slope of 80 mV·dec) -1 ~300mV·dec -1 This method reduces the reduction of active chlorine in the electrocatalytic system, leaving a large amount of active chlorine in the electrochemical system and promoting the rapid degradation of pollutants in the electrocatalytic system. Compared with sequencing batch electrocatalytic treatment, the continuous electrocatalytic treatment of high-salinity wastewater of this invention transfers a large amount of active chlorine in the electrocatalytic system, reducing the possibility of further oxidation of active chlorine by the anode during the electrocatalytic treatment process, thereby maximizing the utilization of active chlorine. The method of this invention has the advantages of simple operation, fast reaction start-up, clean and efficient operation, no need for additional reagents, no secondary pollution, and strong adaptability to operating conditions, and can efficiently degrade antibiotics in high-salinity wastewater.

[0020] (2) In view of the problem that the high salt content in the water body can easily clog and inhibit the electrode active material when treating high salinity wastewater by traditional electrochemical treatment, the method of the present invention transforms the hindrance of NaCl in the actual treatment process of high salinity wastewater into an aid to pollutant degradation, effectively converting a large amount of chloride ions in high salinity wastewater into active chlorine, and using the oxidation capacity of active chlorine to improve the pollutant removal capacity. Attached Figure Description

[0021] Figure 1 This is a graph showing the change in the yield of active chlorine over time during the electrocatalytic treatment process in Example 1 of the present invention.

[0022] Figure 2 This is a graph showing the change in the yield of active chlorine over time during the electrocatalytic reaction in the residence state in Example 1 of the present invention.

[0023] Figure 3 This is a graph showing the change in the yield of active chlorine over time during the electrocatalytic reaction in a flowing state in Example 1 of the present invention.

[0024] Figure 4 This is a graph showing the change in active chlorine production over time during the electrocatalytic reaction under different cathode material conditions in Example 2 of the present invention.

[0025] Figure 5 This is a linear current-voltage characteristic curve of stainless steel and carbon felt materials in Example 2 of the present invention.

[0026] Figure 6 This is a Tafel slope diagram of stainless steel and carbon felt materials in Embodiment 2 of the present invention.

[0027] Figure 7 This is a graph showing the degradation effect of tetracycline in high-salt wastewater under different pH conditions in Example 3 of the present invention.

[0028] Figure 8 This is a graph showing the yield-time variation of chlorate and perchlorate ions during the electrocatalytic reaction in Comparative Example 1 under the residence state. Detailed Implementation

[0029] The present invention will be further described below with reference to the accompanying drawings and specific preferred embodiments, but this does not limit the scope of protection of the present invention. All materials and instruments used in the following embodiments are commercially available.

[0030] Example 1:

[0031] A method for improving the utilization capacity of active chlorine in electrocatalytic treatment of high-salinity wastewater according to the present invention comprises the following steps:

[0032] (1) The electrocatalytic system includes a cathode, anode, electrode clamps, a power source, and a stirring device. The cathode is a Tafel cathode with a slope of 140.09 mV·dec. -1 The foamed iron-nickel bimetallic electrode sheet has a titanium-coated anode with an oxygen evolution potential of 1.6V. The cathode and anode are connected to the power supply by electrode clamps and are vertically immersed in high-salt wastewater. The anode and cathode are parallel and opposite each other, and the plate spacing is adjusted to 3.5cm. The cathode has a thickness of 1mm, a length of 50mm, and a width of 30mm, and the anode has a thickness of 1mm, a length of 50mm, and a width of 30mm.

[0033] (2) The high-salinity wastewater was introduced into the above electrocatalytic system. Under the conditions of activation by external ultraviolet light and heat source, the high-salinity wastewater was kept in the electrocatalytic system for 60 min to carry out the electrocatalytic reaction. The active chlorine content (FCS) reached 122.88 μg / cm³. 2 Then, the influent and effluent flow rates of the high-salinity wastewater were adjusted to 1 mL / min to allow the electrocatalytic reaction to proceed under flowing conditions. At this point, the active chlorine concentration (FCS) was 78 μg / cm³. 2 -122μg / cm 2 The temperature fluctuates within a certain range, and after 600 minutes of treatment, the electrocatalytic treatment of high-salt wastewater is completed.

[0034] In this embodiment, the volume ratio of the influent flow rate per minute to the reaction volume in the stationary state is controlled to be 1:400. In this embodiment, the total treatment volume of high-salt wastewater is 600mL, and the high-salt wastewater treated in the stationary state is 400mL.

[0035] In this embodiment, the high-salinity wastewater has a NaCl content of 20000 mg / L, a Na2SO4 content of 7.1 g / L, and an initial pH value of 5. Sulfuric acid and sodium hydroxide are used to adjust the pH value of the high-salinity wastewater. The stirring device speed is set to 500 rpm, and the power supply output DC current is adjusted to 100 mA with a current density of 6.67 mA / cm³. 2 The ultraviolet radiation intensity is 10 mW / cm 2 The temperature at which the heat source is activated, i.e. the ambient temperature of the reaction, is 30℃.

[0036] In this embodiment, the influent and effluent flow rates of the high-salt wastewater during the electrocatalytic reaction in a flowing state were also adjusted to 20 mL / min, while other conditions remained the same.

[0037] Control group: No external ultraviolet light or heat source was added for activation, and all other conditions were the same.

[0038] The steps for determining the concentration of active chlorine are as follows: (1) Weigh 24.0g of anhydrous disodium hydrogen phosphate and 46.0g of potassium dihydrogen phosphate, dissolve them in 100mL of 8.0g / L EDTA disodium dihydrate solution, transfer them to a 1000mL volumetric flask, and prepare a phosphate buffer solution with pH=6.5; (2) Add 15.0mL of the phosphate buffer solution from step (1), 5.0mL of 1.1g / L N,N-diethyl-1,4-phenylenediamine solution, and 100mL of diluted water sample to a 250mL conical flask; (3) Determine the concentration of active chlorine by visible ultraviolet spectrophotometry.

[0039] In this embodiment, samples were taken at 0, 2, 4, 6, 8, 10, 20, 30, 60, 90, 120, 180, 240, 300, 360, 460, 560, and 660 minutes of the reaction, and the results are as follows. Figure 1 As shown.

[0040] Figure 1 This is a graph showing the yield-time variation of active chlorine in the electrocatalytic treatment of Example 1 of the present invention. Figure 1 It can be seen that from 0 to 60 minutes, the high-salt wastewater enters the reaction vessel and is electrocatalytically oxidized, a process that lasts for 60 minutes. During this period, active chlorine is continuously produced, and the FCS content reaches 122.88 μg / cm³ at 60 minutes. 2 Subsequently, the influent and effluent flow rates in the reaction vessel were both 1 mL / min for 600 min. During this period, active chlorine was discharged from the outlet, and the chloride ions brought in by the influent were oxidized into active chlorine. The overall FCS content showed a decreasing trend, and at 660 min after the start of the reaction, the FCS content decreased to 78.66 μg / cm³. 2 .

[0041] In this embodiment, the concentration of active chlorine was measured during the electrocatalytic reaction in a stationary state, specifically at sampling times of 0, 2, 4, 6, 8, 10, 20, 30, and 60 minutes after the start of the reaction. The results are as follows: Figure 2 As shown.

[0042] Figure 2 This is a graph showing the change in the yield of active chlorine over time during the electrocatalytic reaction in the residence state in Example 1 of the present invention. Figure 2 It can be seen that in this embodiment and the control group, the active chlorine production during electrocatalytic treatment of high-salt wastewater increases with the increase of reaction time. Compared with the control group, in this embodiment, when an external heating source and ultraviolet irradiation are used to assist electrocatalytic treatment, the active chlorine production in the system increases by about 1.3 times after 60 minutes of reaction. This confirms that the external heating source and ultraviolet irradiation help to increase the production of active chlorine.

[0043] In this embodiment, the concentration of active chlorine was measured during the electrocatalytic reaction under flowing conditions, specifically at 0, 30, 60, 120, 180, 240, 300, 400, 500, and 600 minutes after the start of the reaction. The results are as follows: Figure 3 As shown.

[0044] Figure 3 This is a graph showing the yield-time variation of active chlorine during the electrocatalytic reaction in flowing conditions in Example 1 of the present invention. Figure 3 It can be seen that when the electrocatalytic reaction time is 600 min under flowing conditions, the active chlorine yield decreases with increasing reaction time during the electrocatalytic reaction at influent and effluent flow rates of 1 mL / min and 20 mL / min. Specifically, when the influent and effluent flow rates are 1 mL / min, the rate of decrease in active chlorine content during the electrocatalytic reaction is slower, reaching 78.66 μg / cm³ after 600 min of reaction.2 The active chlorine content is approximately twice that at a flow rate of 20 mL / min. The relatively low active chlorine content in the treatment system when the influent and effluent flow rates of high-salt wastewater are 20 mL / min is due to the following reasons: 1. The faster effluent flow rate removes more active chlorine from the electrocatalytic system; 2. Although the faster influent flow rate brings more chloride ions, it also dilutes the total amount of active chlorine in the reaction vessel to a greater extent; 3. The shorter residence time of chloride ions in the system means they are directly discharged from the reaction vessel before they have a chance to be oxidized into active chlorine.

[0045] Example 2:

[0046] This invention discloses a method for improving the utilization capacity of active chlorine in the electrocatalytic treatment of high-salinity wastewater. The method employs an electrocatalytic system to treat the high-salinity wastewater, and is essentially the same as the method in Example 1, except that in step (1), a stainless steel electrode is used as the cathode, and the Tafel slope of the stainless steel electrode is 168.35 mV dec. -1 .

[0047] Control group: Carbon felt material was used instead of stainless steel electrode as cathode. The Tafel slope of the carbon felt material electrode was 388.71 mV dec. -1 All other conditions are the same.

[0048] Figure 4 This is a graph showing the change in active chlorine production over time during the electrocatalytic reaction under different cathode material conditions in Example 2 of the present invention, during the residence state. Figure 4 It can be seen that the electrocatalytic system using stainless steel as the cathode has a stronger ability to produce active chlorine. At a reaction time of 60 min, the active chlorine yield of the electrocatalytic system using stainless steel as the cathode is 126.00 μg / cm³. 2 The electrocatalytic system using carbon felt as the cathode has a density of approximately 29.83 μg / cm³. 2 4 times that of ).

[0049] Figure 5 This is a linear current-voltage characteristic curve of stainless steel and carbon felt materials in Example 2 of the present invention. Figure 6 This is a Tafel slope diagram of the stainless steel and carbon felt materials used in Embodiment 2 of the present invention. Figure 5 and Figure 6 It can be seen that the Tafel slopes of carbon felt and stainless steel are 388.71mV·dec. -1 and 168.35mV·dec -1 .

[0050] Example 3:

[0051] The application of the method of the present invention for improving the utilization capacity of active chlorine in electrocatalytic treatment of high-salinity wastewater to the treatment of tetracycline, that is, using the method of the present invention to degrade tetracycline in high-salinity wastewater under different pH conditions, is basically the same as the method in Example 1, except that in step (2), the concentration of tetracycline in the high-salinity wastewater is 50.0 mg / L, and the initial pH values ​​of the high-salinity wastewater are 5 and 11, respectively. The tetracycline content is determined by ultraviolet spectrophotometry at 357 nm.

[0052] Figure 7 This image shows the degradation effect of tetracycline in high-salt wastewater under different pH conditions in Example 3 of the present invention. Figure 7 It can be seen that the tetracycline content decreases with increasing electrocatalytic reaction time; at the same time, the electrocatalytic degradation of tetracycline is stronger under acidic conditions. When the pH is 5 and 11, the tetracycline degradation rate is 99.82% and 91.84%, respectively. This may be due to the stronger oxidizing power of active chlorine and the higher content of active chlorine under acidic conditions.

[0053] Comparative Example 1:

[0054] A method for electrocatalytic treatment of high-salinity wastewater is basically the same as that in Example 1, except that in step (1), the anode used is a BDD electrode (i.e., boron-doped diamond electrode), and the oxygen evolution potential of the BDD electrode is 2.25V. During the electrocatalytic reaction in the residence state, samples were taken at 0, 2, 4, 6, 8, 10, 20, 30, and 60 min of the reaction, and the contents of chlorate and perchlorate were determined by ion chromatography.

[0055] Figure 8 This is a graph showing the yield-time changes of chlorate and perchlorate ions during the electrocatalytic reaction in Comparative Example 1 under the residence state. Figure 8 It can be seen that as the reaction time increases, the chlorate ion (ClO3) increases. - ) and perchlorate (ClO4) - The increasing content of chlorate indicates the formation of high-valence chlorides in the electrocatalytic system with BDD as the anode. Simultaneously, the chlorate content remains consistently higher than the perchlorate content. This is because the anodic oxidation of chloride ions produces active chlorine, which is then oxidized to chlorate, and subsequently converted to perchlorate. Furthermore, this comparative example confirms that an anode with an oxygen evolution potential greater than 2.2V oxidizes chloride ions to produce both chlorate and perchlorate.

[0056] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any way. Although the present invention has been disclosed above with reference to preferred embodiments, it is not intended to limit the present invention. Any person skilled in the art can make many possible variations and modifications to the technical solutions of the present invention using the methods and techniques disclosed above, or modify them into equivalent embodiments with equivalent changes, without departing from the spirit and technical essence of the present invention. Therefore, any simple modifications, equivalent substitutions, equivalent changes, and modifications made to the above embodiments based on the technical essence of the present invention without departing from the content of the technical solutions of the present invention shall still fall within the protection scope of the technical solutions of the present invention.

Claims

1. A method for improving the utilization of active chlorine in the electrocatalytic treatment of high-salinity wastewater, characterized by, The method comprises the following steps: Under ultraviolet light and / or heat source conditions, high-salinity wastewater is introduced into the electrocatalytic system, and the electrocatalytic reaction is first carried out in a residence state. When 50 μg / cm³ is reached... 2 ≤Active chlorine content FCS≤350μg / cm³ 2 At that time, the high-salinity wastewater was subjected to an electrocatalytic reaction under flowing conditions, and the influent and effluent flow rates of the high-salinity wastewater were controlled to be consistent and maintained at 30 μg / cm³. 2 ≤Active chlorine content FCS<350μg / cm³ 2 The process continues until the high-salinity wastewater is completely treated; the electrocatalytic system includes an anode and a cathode, and the cathode material used has a Tafel slope of 80 mV·dec. -1 ~300mV·dec -1 The anode material used in this anode has an oxygen evolution potential of < 2.2V; The volume ratio of the water inflow per minute in the flow state to the reaction volume in the residence state is 1-20:400; The inflow and outflow flow rates of the high-salinity wastewater in the electrocatalytic reaction in the flow state are both 1-20 mL / min; The pH value of the high-salinity wastewater is 3.0-11.0, the content of NaCl in the high-salinity wastewater is 1000-60000 mg / L, and the content of Na2SO4 in the high-salinity wastewater is 1.4-7.1 g / L.

2. The method for improving the utilization of active chlorine in the electrocatalytic treatment of high-salinity wastewater according to claim 1, characterized in that, The electrocatalytic reaction time in the residence state is 30-60 min.

3. The method for improving the utilization of active chlorine in the electrocatalytic treatment of high-salinity wastewater according to claim 1, characterized in that, The electrocatalytic reaction time in the flow state is 60-600 min.

4. The method for improving the utilization of active chlorine in the electrocatalytic treatment of high-salinity wastewater according to claim 1, characterized in that, The intensity of the ultraviolet rays is 10 mW / cm 2 ~ 100 mW / cm 2 The temperature of the heat source is 20°C ~ 80°C.

5. The method for improving the utilization of active chlorine in the electrocatalytic treatment of high-salinity wastewater according to any one of claims 1 to 4, characterized in that, The cathode material comprises a stainless steel material or a foamed iron-nickel material, and the anode material comprises a titanium-based material or a lead-based material.

6. The method of improving the utilization of active chlorine in the electrocatalytic treatment of high-salinity wastewater according to any one of claims 1 to 4, characterized in that, The current density in the electrocatalytic system is 2.7 mA / cm 2 ~ 8 mA / cm 2 .

7. The method for improving the utilization of active chlorine in the electrocatalytic treatment of high-salinity wastewater according to any one of claims 1 to 4, characterized in that, The plate spacing of the anode and the cathode is 2.0-4.0 cm, the thickness of the cathode is 1-5 mm, the length is 30-100 mm, and the width is 30-100 mm, and the thickness of the anode is 1-5 mm, the length is 30-100 mm, and the width is 30-100 mm.

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