Electro-fenton synergistic treatment method for high-salinity organic wastewater

Abstract

The present application relates to a high-salinity organic wastewater pollution control and treatment method, and belongs to the technical field of high-salinity organic wastewater treatment, comprising: feeding high-salinity organic wastewater containing chlorine ions and organic pollutants into an electro-Fenton oxidation section, a cathode reduction dechlorination section and a re-oxidation section in sequence, supplying oxygen-containing gas to the iron-containing cathode reaction interface in the electro-Fenton oxidation section to generate hydrogen peroxide in situ, and forming hydroxyl radicals under the action of the hydrogen peroxide on the iron-containing active sites to oxidize and degrade the organic pollutants; then, through cathode electron transfer by reducing the oxygen supply, the chlorine-containing organic intermediates and residual chlorine-containing oxidizing components are reduced to obtain dechlorinated organic intermediate products and convert the residual chlorine-containing oxidizing components into chlorine ions; and then the dechlorinated organic intermediate products are introduced into the re-oxidation section for further electro-Fenton oxidation degradation, thereby reducing the content of organic pollutants and organic halogens in the effluent, and the treatment path is continuous and stable.

Description

Technical Field

[0001] This invention relates to the field of high-salt organic wastewater treatment technology, specifically to an electro-Fenton co-treatment method for the control and treatment of high-salt organic wastewater pollution. Background Technology

[0002] In existing technologies, high-salinity organic wastewater generally exhibits characteristics such as high salinity, high conductivity, high concentration of organic pollutants, poor biodegradability, and large fluctuations in water quality. Especially when the wastewater contains a high concentration of chloride ions, conventional biological treatment is easily inhibited by osmotic pressure and toxicity. Conventional advanced oxidation methods such as Fenton oxidation, ozone oxidation, and electrocatalytic oxidation have shortcomings in terms of reagent consumption, energy consumption, sludge disposal, and byproduct control. Among the recently published Chinese patents, CN116917242A discloses a method for treating high-salinity, high-organic wastewater. Targeting high-salinity, high-organic wastewater containing sodium sulfate from the battery recycling industry, it proposes first using activated carbon to adsorb organic matter, then using an organic solvent containing dichloromethane to desorb the activated carbon, and combining this with subsequent resource recovery processes to reduce COD before entering the evaporation and crystallization system. This solution reflects that high-salinity, high-organic wastewater usually requires reduction of organic pollutants before subsequent desalination, evaporation and crystallization, or reuse treatment; otherwise, it easily leads to foaming, mother liquor accumulation, and increased system operating costs.

[0003] CN115124116A discloses an electro-Fenton device and method for treating high-chloride organic wastewater. This method utilizes an electro-Fenton reactor, a storage tank, and an aeration system to generate hydrogen peroxide in situ using a cathode carbon brush, forming an electro-Fenton oxidation system. This achieves the degradation of organic matter in high-chloride wastewater at a relatively low current density and proposes technical advantages such as avoiding chlorine generation, eliminating the need for additional hydrogen peroxide addition, and reducing iron sludge. This type of approach demonstrates that electro-Fenton technology, due to its ability to continuously generate active oxygen species through electrochemical processes, has good applicability to high-salt, high-chloride, and recalcitrant organic wastewater. However, in chloride-containing systems, chloride ions may generate active chlorine, chlorinated oxidizing components, or further form chlorinated organic intermediates after participating in anodic or interfacial reactions. While relying solely on a single oxidation process can reduce some COD, it is difficult to simultaneously achieve the removal of organic pollutants and the control of organic halogen byproducts.

[0004] Therefore, for high-salinity organic wastewater containing both chloride ions and organic pollutants, existing treatment approaches mainly focus on enhanced oxidation, adsorption separation, coagulation pretreatment, or resource-based desalination. These approaches have not adequately addressed the issues of chloride ion accumulation during electro-Fenton oxidation, the continued reaction of residual chloride-containing oxidizing components, and the potential for secondary chlorination during the re-oxidation stage. Particularly under continuous flow or segmented treatment conditions, how to effectively degrade organic pollutants using hydroxyl radicals generated by electro-Fenton oxidation, while simultaneously performing targeted reduction and dechlorination of already formed chloride-containing organic intermediates and residual chloride-containing oxidizing components, and continuing deep oxidation after dechlorination, remains a crucial technical challenge for the control and treatment of high-salinity organic wastewater pollution. Summary of the Invention

[0005] The purpose of this invention is to provide an electro-Fenton co-treatment method for the control and treatment of high-salt organic wastewater pollution, thereby solving some of the drawbacks and shortcomings pointed out in the background art.

[0006] The present invention adopts the following technical solution to solve the above-mentioned technical problems: High-salt organic wastewater containing chloride ions and organic pollutants is sequentially fed into the electro-Fenton oxidation section, the cathode reduction dechlorination section, and the re-oxidation section. In the electro-Fenton oxidation section, oxygen-containing gas is supplied to the iron-containing cathode reaction interface and hydrogen peroxide is generated in situ. Hydrogen peroxide forms hydroxyl radicals under the action of iron-containing active sites, which oxidize and degrade organic pollutants. In the electro-Fenton oxidation section, organic pollutants are brought into contact with chlorine-containing oxidizing components formed by the conversion of chloride ions at the iron-containing cathode reaction interface to generate chlorine-containing organic intermediates. Subsequently, wastewater containing the chlorine-containing organic intermediates and residual chlorine-containing oxidizing components is passed into the cathode reduction dechlorination section, where the chlorine-containing organic intermediates and residual chlorine-containing oxidizing components are reduced by cathode electron transfer with reduced oxygen supply. In the cathodic reduction dechlorination section, dechlorinated organic intermediates are obtained, and the residual chlorinated oxidizing components are converted into chloride ions. Then, the wastewater containing the dechlorinated organic intermediates is introduced into the re-oxidation section, where the dechlorinated organic intermediates are degraded by electro-Fenton oxidation at the iron-containing cathode reaction interface, thereby reducing the content of organic pollutants and organic halogens in the effluent.

[0007] Furthermore, in the electro-Fenton oxidation section, the organic pollutants are first adsorbed or retained at the iron-containing cathode reaction interface, and then come into contact with the chlorine-containing oxidizing component, so that the chlorine-containing oxidizing component participates in the activation of organic pollutants at the iron-containing cathode reaction interface and inhibits the chlorination reaction in the main aqueous phase.

[0008] Furthermore, the oxygen supply of the cathode reduction dechlorination section is lower than that of the electro-Fenton oxidation section, so that the cathode electron transfer in the cathode reduction dechlorination section is used for the reduction dechlorination of the chlorine-containing organic intermediate and the residual chlorine-containing oxidizing component.

[0009] Furthermore, before entering the re-oxidation section, the dechlorinated organic intermediate undergoes reduction treatment of the residual chlorine-containing oxidizing components in the cathodic reduction dechlorination section, and continues to react with hydrogen peroxide, iron-containing active sites, and hydroxyl radicals in the re-oxidation section.

[0010] Furthermore, an oxygen-free transition zone is provided before the cathode reduction and dechlorination section, so that the dissolved oxygen brought in from the electro-Fenton oxidation section is consumed or dissipated before contacting the reduction cathode, thereby reducing the competition of oxygen for electron transfer at the cathode.

[0011] Furthermore, a halogenated organic matter retention interface is formed on the cathode surface of the cathode reduction dechlorination section, so that the chlorinated organic intermediate is first retained at the halogenated organic matter retention interface, and then undergoes a dechlorination reaction by accepting electron transfer from the cathode.

[0012] Furthermore, the cathodic reduction dechlorination section reduces the residual chlorine-containing oxidizing components into chloride ions, and allows the chloride ions to enter the re-oxidation section with the dechlorinated wastewater, thereby reducing the re-generation of chlorine-containing organic intermediates in the re-oxidation section.

[0013] Furthermore, the dechlorinated organic intermediate product passes through an iron-containing adsorption interface before entering the re-oxidation section, so that the dechlorinated organic intermediate product is enriched at the iron-containing adsorption interface before entering the re-oxidation section.

[0014] Furthermore, the iron-containing active sites in the re-oxidation section are located at the cathode reaction interface, and the dechlorinated organic intermediate reacts with hydrogen peroxide and hydroxyl radicals at the cathode reaction interface.

[0015] Furthermore, the cathode reaction interface has a dechlorination organic intermediate enrichment zone and a hydroxyl radical generation zone arranged sequentially along the water flow direction, so that the dechlorination organic intermediate is first retained in the dechlorination organic intermediate enrichment zone and then enters the hydroxyl radical generation zone for oxidative degradation.

[0016] This invention involves sequentially passing high-salt organic wastewater containing chloride ions and organic pollutants through an electro-Fenton oxidation section, a cathode reduction dechlorination section, and a re-oxidation section. This allows the wastewater to undergo oxidative degradation, followed by reduction dechlorination, and then further deep degradation through re-oxidation within the same synergistic treatment pathway. In the electro-Fenton oxidation section, oxygen-containing gas is supplied to the iron-containing cathode reaction interface, generating hydrogen peroxide in situ. Under the influence of the iron-containing active sites, hydroxyl radicals are formed, effectively oxidizing and degrading organic pollutants, thus improving the removal capacity of recalcitrant organic matter from high-salt organic wastewater.

[0017] Meanwhile, the present invention sets up a cathode reduction dechlorination section after the electro-Fenton oxidation section, so that the generated chlorinated organic intermediates and residual chlorinated oxidizing components are subjected to cathode electron transfer reduction treatment under reduced oxygen supply conditions, so that the chlorinated organic intermediates are converted into dechlorinated organic intermediates and the residual chlorinated oxidizing components are converted into chloride ions, thereby helping to reduce the content of organic halogens in the subsequent effluent and reducing the possibility of chlorinated oxidizing components continuing to participate in side reactions.

[0018] Furthermore, this invention introduces the dechlorinated organic intermediates into the re-oxidation stage, allowing them to continue electro-Fenton oxidation degradation at the iron-containing cathode reaction interface. This segmented synergistic approach integrates the oxidative removal of organic pollutants, the reduction and dechlorination of chlorinated intermediates, and the re-oxidation treatment of dechlorinated products. This improves the overall treatment effect on high-salt, chlorine-containing organic wastewater, reduces the content of organic pollutants and organic halogens in the effluent, and is suitable for the control and treatment of high-salt organic wastewater pollution. Attached Figure Description

[0019] Figure 1 This is a flowchart of the electro-Fenton co-treatment method for high-salt organic wastewater according to the present invention.

[0020] Figure 2 This is a flowchart of the process from electro-Fenton oxidation to cathode reduction and dechlorination in Example 1 of the present invention.

[0021] Figure 3 This is a graph showing the decrease in organic halogen concentration and the reduction dechlorination rate in Example 1 of the present invention.

[0022] Figure 4 This is a graph showing the oxygen supply reduction rate and electron transfer direction in Embodiment 1 of the present invention.

[0023] Figure 5 This is a flowchart of the enrichment and re-oxidation of dechlorinated organic intermediates in Example 2 of the present invention.

[0024] Figure 6 This is a graph showing the change in organic pollutant concentration and reduction mass during the re-oxidation stage in Example 2 of the present invention.

[0025] Figure 7 This is a diagram showing the residence time distribution between the enrichment region and the hydroxyl radical generation region in Example 2 of the present invention. Detailed Implementation

[0026] As attached Figure 1As shown, in one specific embodiment, high-salt organic wastewater containing chloride ions and organic pollutants sequentially enters the electro-Fenton oxidation section, the cathode reduction dechlorination section, and the re-oxidation section along the treatment flow direction. The electro-Fenton oxidation section, the cathode reduction dechlorination section, and the re-oxidation section can be reaction zones continuously arranged along the water flow direction in the same flow reactor, or they can be multiple reaction chambers connected sequentially, with the wastewater flowing continuously or segmentally between adjacent treatment sections. An iron-containing cathode reaction interface is provided within the electro-Fenton oxidation section. This interface is formed by the conductive cathode surface and iron-containing components disposed on or near the conductive cathode surface, with iron-containing active sites located on or near the surface of the iron-containing components. Oxygen-containing gas is supplied to this iron-containing cathode reaction interface, and hydrogen peroxide is generated in situ under cathode reaction conditions. The oxygen-containing gas can be air, oxygen, or an oxygen-containing mixture, and is supplied to the vicinity of the iron-containing cathode reaction interface through aeration, blowing, or introduction. Hydrogen peroxide generates hydroxyl radicals under the catalysis of iron-containing active sites. These hydroxyl radicals oxidize and degrade organic pollutants in high-salt organic wastewater, thereby weakening the molecular structure of organic pollutants and forming the intermediate reaction system required for subsequent reactions.

[0027] Within the electro-Fenton oxidation section, chloride ions in high-salt organic wastewater are transformed into chlorinated oxidizing components under an oxidizing environment. These chlorinated oxidizing components are formed from chloride ions under oxidizing conditions and can participate in the activation or chlorination reactions of organic pollutants. Organic pollutants come into contact with these chlorinated oxidizing components at the iron-containing cathode reaction interface, causing them to participate in the activation of the organic pollutants and generate chlorinated organic intermediates. Subsequently, the wastewater containing these chlorinated organic intermediates and residual chlorinated oxidizing components enters the cathodic reduction dechlorination section. The residual chlorinated oxidizing components are those not consumed in the electro-Fenton oxidation section and enter the cathodic reduction dechlorination section with the wastewater. In the cathodic reduction dechlorination section, by reducing the oxygen supply, the cathode electron transfer is more concentrated on the chlorinated organic intermediates and residual chlorinated oxidizing components, thereby reducing and dechlorinating the chlorinated organic intermediates and reducing and transforming the residual chlorinated oxidizing components.

[0028] After treatment in the cathodic reduction dechlorination stage, dechlorinated organic intermediates are formed in the wastewater, and residual chlorinated oxidizing components are converted into chloride ions. These dechlorinated organic intermediates are organic intermediates formed after cathodic reduction dechlorination of chlorinated organic intermediates and can still be subsequently oxidized and degraded. The wastewater containing these dechlorinated organic intermediates is then introduced into the re-oxidation stage. In the re-oxidation stage, the dechlorinated organic intermediates continue to undergo electro-Fenton oxidation at the iron-containing cathode reaction interface, reacting with in-situ generated hydrogen peroxide, iron-containing active sites, and hydroxyl radicals, further oxidizing and degrading the dechlorinated organic intermediates, thereby reducing the content of organic pollutants and organic halogens in the effluent.

[0029] Based on the above implementation method, the iron-containing cathode reaction interface in the electro-Fenton oxidation section is used to support the interfacial enrichment and oxidative activation process of organic pollutants. After high-salt organic wastewater enters the electro-Fenton oxidation section, the organic pollutants in the wastewater are first adsorbed or retained at the iron-containing cathode reaction interface, causing the organic pollutants to concentrate from the main aqueous phase to the reaction interface. Adsorption or retention can be achieved through the interfacial interaction of the iron-containing cathode reaction interface with the organic pollutants through the pores, rough surfaces, iron-containing components, or conductive carrier surfaces. Subsequently, the chloride-containing oxidizing components formed by chloride ions in the electro-Fenton oxidation environment react with the organic pollutants at the iron-containing cathode reaction interface, allowing the chloride-containing oxidizing components to participate in the activation of organic pollutants. By ensuring that the reaction mainly occurs at the iron-containing cathode reaction interface, the degree of non-directional chlorination reaction between the chloride-containing oxidizing components and organic pollutants in the main aqueous phase can be reduced, thereby inhibiting the chlorination reaction in the main aqueous phase.

[0030] The cathodic reduction dechlorination section is used to reduce chlorinated organic intermediates and residual chlorinated oxidizing components produced in the electro-Fenton oxidation section. The oxygen supply in the cathodic reduction dechlorination section is controlled to be lower than that in the electro-Fenton oxidation section, thus reducing the competition of oxygen for cathode electron transfer in this stage. The reduction in oxygen supply can be achieved by shutting off the oxygen-containing gas supply, reducing the aeration intensity, or reducing the amount of oxygen-containing gas entering the system. Therefore, cathode electron transfer can be used for the reductive dechlorination of chlorinated organic intermediates and for the reductive transformation of residual chlorinated oxidizing components, weakening or removing the chlorinated structures in the chlorinated organic intermediates while reducing the possibility of residual chlorinated oxidizing components continuing to participate in the chlorination reaction.

[0031] Before entering the re-oxidation section, the dechlorinated organic intermediates have already undergone reduction treatment of residual chlorine-containing oxidizing components in the cathodic reduction dechlorination section. After this treatment, the reaction system in the wastewater entering the re-oxidation section primarily targets the dechlorinated organic intermediates for oxidation. The re-oxidation section continues to provide hydrogen peroxide, iron-containing active sites, and hydroxyl radicals, allowing the dechlorinated organic intermediates to undergo further electro-Fenton oxidation. This re-oxidation process further disrupts the organic molecular structure of the dechlorinated organic intermediates, transforming them into low-molecular-weight organic compounds or mineralized products, thereby improving the removal efficiency of organic pollutants from high-salinity organic wastewater and reducing the content of organic halogens in the subsequent effluent.

[0032] Based on the above implementation method, an oxygen-free transition zone is set up before the cathodic reduction dechlorination section. Wastewater flowing out of the electro-Fenton oxidation section passes through this oxygen-free transition zone before entering the cathodic reduction dechlorination section. This oxygen-free transition zone can be a flow channel, compartment, or residence area without an oxygen-containing gas supply structure. In this oxygen-free transition zone, no oxygen-containing gas is supplied to the wastewater, allowing the dissolved oxygen brought in from the electro-Fenton oxidation section to be consumed by the reaction during flow or to dissipate from the wastewater. After this process, the dissolved oxygen content of the wastewater entering the cathodic reduction dechlorination section is reduced, thereby weakening the competition of oxygen for the electron transfer process on the reduction cathode surface, allowing more cathode electron transfer to be used for the reduction treatment of chlorinated organic intermediates and residual chlorinated oxidizing components.

[0033] In the cathodic reduction dechlorination section, a chlorinated organic intermediate retention interface forms on the cathode surface. This interface is formed by pores, rough surfaces, conductive carrier surfaces, or interfacial layers capable of retaining chlorinated organic intermediates on the cathode surface. When wastewater containing chlorinated organic intermediates flows through this cathode surface, the intermediates are initially retained at the retention interface, resulting in a high local reaction concentration near the reduction cathode. Subsequently, the intermediates accept electron transfer from the reduction cathode, undergoing a reduction dechlorination reaction. This weakens or removes the chlorinated structure within the intermediates, forming dechlorinated organic intermediate products.

[0034] Within the cathodic reduction dechlorination section, residual chlorine-containing oxidizing components also undergo cathode electron transfer and are reduced to chloride ions. The wastewater, carrying chloride ions, enters the re-oxidation section. Because the residual chlorine-containing oxidizing components have already been reduced in the cathodic reduction dechlorination section before entering the re-oxidation section, the number of chlorine-containing oxidizing components that can participate in the formation of chlorine-containing organic intermediates is reduced in the re-oxidation section. This decreases the degree of re-formation of chlorine-containing organic intermediates in the re-oxidation section and facilitates the subsequent oxidative degradation of dechlorinated organic intermediates in the re-oxidation section.

[0035] Based on the above implementation method, the dechlorinated organic intermediates pass through an iron-containing adsorption interface before entering the re-oxidation section. The iron-containing adsorption interface can be located adjacent to the iron-containing cathode reaction interface within the re-oxidation section, or it can be set as an independent filling interface at the inlet of the re-oxidation section. When wastewater containing the dechlorinated organic intermediates flows through the iron-containing adsorption interface, the dechlorinated organic intermediates undergo adsorption and enrichment at the interface, causing the dechlorinated organic intermediates to be oxidized to concentrate from the flowing aqueous phase towards the reaction interface. The enriched dechlorinated organic intermediates then enter the re-oxidation section with the wastewater, thereby improving the sufficiency of their contact with the electro-Fenton reaction system within the re-oxidation section.

[0036] A cathode reaction interface, specifically an iron-containing interface, is set up within the re-oxidation section, with iron-containing active sites located thereon. Oxygen-containing gas is continuously supplied to the vicinity of the cathode reaction interface within the re-oxidation section, enabling in-situ generation of hydrogen peroxide. Upon entering the re-oxidation section, the dechlorinated organic intermediates come into contact with the in-situ generated hydrogen peroxide at the cathode reaction interface and undergo an oxidation reaction with hydroxyl radicals under the influence of the iron-containing active sites. Through this reaction process, the organic molecular structure of the dechlorinated organic intermediates is further disrupted, allowing them to continue transforming into low-molecular-weight organic compounds or mineralized products.

[0037] The cathode reaction interface is sequentially configured with a dechlorination organic intermediate enrichment zone and a hydroxyl radical generation zone along the water flow direction. Wastewater containing dechlorination organic intermediates enters the cathode reaction interface and first passes through the dechlorination organic intermediate enrichment zone, where the intermediates are retained and their local concentration at the interface is increased. Subsequently, the wastewater continues to flow into the hydroxyl radical generation zone, where hydrogen peroxide generates hydroxyl radicals under the action of iron-containing active sites. These hydroxyl radicals oxidize and degrade the already enriched dechlorination organic intermediates. By sequentially arranging the enrichment and oxidation reaction zones along the water flow direction, the dechlorination organic intermediates can first undergo interface enrichment before being oxidized by hydroxyl radicals, thereby improving the degradation efficiency of the dechlorination organic intermediates in the re-oxidation stage.

[0038] Example 1: A certain unit uses an electro-Fenton co-treatment device to treat high-salinity organic wastewater containing chloride ions and organic pollutants. The electro-Fenton co-treatment device consists of an electro-Fenton oxidation section, an oxygen-free transition zone, a cathode reduction dechlorination section, and a re-oxidation section, arranged sequentially along the wastewater flow direction. The chloride ion concentration in the high-salinity organic wastewater is 18600 mg / L, the organic pollutant concentration is 428 mg / L, and the organic halogen concentration (calculated as chlorine) is 12.4 mg / L.

[0039] Wastewater first enters the electro-Fenton oxidation section. An iron-containing cathode reaction interface is set up within the electro-Fenton oxidation section, formed by the conductive cathode surface and the iron-containing components distributed on that surface. Oxygen-containing gas is supplied near the iron-containing cathode reaction interface at a rate of 0.80 L / min, causing the oxygen to generate hydrogen peroxide under cathode reaction conditions. The hydrogen peroxide then forms hydroxyl radicals under the action of iron-containing active sites.

[0040] Within the electro-Fenton oxidation stage, organic pollutants in the wastewater are first adsorbed or retained at the iron-containing cathode reaction interface, causing them to concentrate from the bulk aqueous phase towards the reaction interface. Chloride ions in the wastewater, under oxidizing conditions, form chlorinated oxidizing components, which then contact the organic pollutants already enriched at the iron-containing cathode reaction interface. This allows the chlorinated oxidizing components to participate in the activation of the organic pollutants, forming chlorinated organic intermediates. Because organic pollutants preferentially participate in the reaction at the iron-containing cathode reaction interface, the degree of non-directional chlorination of the chlorinated oxidizing components in the bulk aqueous phase is reduced.

[0041] The wastewater flowing out of the electro-Fenton oxidation section then enters the oxygen-free transition zone. No oxygen-containing gas is added to this zone, allowing the dissolved oxygen introduced from the electro-Fenton oxidation section to be consumed by the reaction or escape from the wastewater during the flow process. After treatment in the oxygen-free transition zone, the dissolved oxygen content of the wastewater entering the cathode reduction dechlorination section is reduced, thereby weakening the competition of oxygen for electron transfer on the reduction cathode surface.

[0042] The oxygen gas supply rate in the cathode reduction dechlorination section is controlled at 0.05 L / min, which is lower than the oxygen gas supply rate in the electro-Fenton oxidation section. A halogenated organic matter retention interface forms on the cathode surface within the cathode reduction dechlorination section. When wastewater containing the chlorinated organic intermediates and residual chlorinated oxidizing components flows through this interface, the chlorinated organic intermediates are first retained at the halogenated organic matter retention interface, resulting in a higher local reaction concentration near the reduction cathode.

[0043] like Figure 2 As shown, the wastewater treatment pathway consists of an electro-Fenton oxidation section, an oxygen-free transition zone, a cathode reduction dechlorination section, and a re-oxidation section in sequence. Different shaded areas in the figure distinguish the oxidation activation, oxygen-free transition, reduction dechlorination, and re-oxidation processes. The attached figure further shows that 0.80 L / min of oxygen-containing gas is mainly supplied to the electro-Fenton oxidation section, while the oxygen supply in the cathode reduction dechlorination section decreases to 0.05 L / min. The oxygen-free transition zone, located between the two, is used to ensure that dissolved oxygen is consumed or dissipated before contacting the reduction cathode, thereby creating a low-oxygen electron transfer environment suitable for reduction dechlorination.

[0044] Subsequently, the chlorinated organic intermediates retained at the halogenated organic matter retention interface accept electron transfer from the reducing cathode and undergo a reductive dechlorination reaction, weakening or removing the chlorinated structure in the chlorinated organic intermediates and forming dechlorinated organic intermediates. At the same time, the residual chlorinated oxidizing components in the wastewater also accept electron transfer from the cathode and are reduced to chloride ions, thereby reducing their possibility of further participation in the chlorination reaction.

[0045] The reduction dechlorination rate of the cathode reduction dechlorination section is calculated using the following formula:

[0046] In the formula, The reduction dechlorination rate of the cathode reduction dechlorination section is expressed in % (%). This indicates the mass concentration of organic halogens in the wastewater before entering the cathode reduction dechlorination section, expressed in mg / L. This represents the mass concentration of organic halogens in the effluent from the cathodic reduction dechlorination section, expressed as chlorine, in mg / L. The derivation of this formula is based on the fact that the reduction dechlorination effect is represented by the reduction in the mass concentration of organic halogens before and after treatment, where the reduction is... The mass concentration of organic halogens before entering the cathode reduction and dechlorination section. As a baseline, the ratio of the reduction to the baseline value is the reduction dechlorination rate, which is then multiplied by... Result in a percentage.

[0047] In this embodiment, the mass concentration of organic halogens in the wastewater before entering the cathode reduction dechlorination section is expressed as chlorine. The concentration of organic halogens in the effluent from the cathodic reduction dechlorination section, expressed as chlorine, is 12.4 mg / L. The concentration is 4.1 mg / L. Substituting this into the above formula, we get:

[0048] like Figure 3 As shown, the concentration of organic halogens decreased from 12.4 mg / L before entering the cathodic reduction dechlorination section to 4.1 mg / L in the effluent from the cathodic reduction dechlorination section. The dashed line connecting the paths illustrates the direction of concentration decrease before and after treatment. The 66.9% reduction dechlorination rate marked in the figure is consistent with the above calculation results, indicating that the cathodic reduction dechlorination section can significantly weaken or remove the chlorine-containing structure in chlorine-containing organic intermediates and reduce the organic halogen content in the wastewater.

[0049] The oxygen supply reduction rate of the cathode reduction dechlorination section relative to the electro-Fenton oxidation section is calculated using the following formula:

[0050] In the formula, The oxygen supply reduction rate of the cathode reduction dechlorination section relative to the electro-Fenton oxidation section is expressed in % (%). This indicates the oxygen-containing gas supply rate in the electro-Fenton oxidation section, expressed in L / min. This represents the oxygen-containing gas supply rate in the cathode reduction dechlorination section, expressed in L / min. The derivation of this formula is based on the following: the cathode reduction dechlorination section needs to reduce the oxygen supply rate to weaken the competition of oxygen for cathode electron transfer; the difference between the oxygen supply rate in the electro-Fenton oxidation section and the oxygen supply rate in the cathode reduction dechlorination section is... Oxygen supply from the electro-Fenton oxidation section As a baseline, the ratio of the difference to the baseline value is the percentage reduction in oxygen supply, which is then multiplied by... Result in a percentage.

[0051] In this embodiment, the oxygen-containing gas supply amount in the electro-Fenton oxidation section The oxygen-containing gas supply rate in the cathode reduction dechlorination section is 0.80 L / min. The flow rate is 0.05 L / min. Substituting this into the above formula, we get:

[0052] like Figure 4 As shown, the difference in oxygen supply between the electro-Fenton oxidation section and the cathodic reduction dechlorination section is compared using a bar graph. The cathodic reduction dechlorination section is in a low-oxygen-supply reduction zone, as indicated by the oxygen supply reduction rate curve. The efficiency reached 93.75%. The attached figure further shows that, within the cathodic reduction dechlorination section, reducing the oxygen supply weakens the competition of oxygen for cathode electron transfer, allowing cathode electron transfer to act more on chlorine-containing organic intermediates and residual chlorine-containing oxidizing components, which is beneficial for reduction dechlorination treatment and the reduction and conversion of residual chlorine-containing oxidizing components.

[0053] The wastewater, after being treated in the cathodic reduction dechlorination section, carries the dechlorination organic intermediates and the reduced chloride ions into the re-oxidation section. Since the residual chlorinated oxidizing components have already been reduced in the cathodic reduction dechlorination section before entering the re-oxidation section, the chlorinated oxidizing components that can participate in the formation of chlorinated organic intermediates are reduced in the re-oxidation section. This is beneficial for the subsequent electro-Fenton oxidation degradation of the dechlorination organic intermediates and reduces the content of organic pollutants and organic halogens in the effluent.

[0054] Example 2: A certain unit uses an electro-Fenton co-treatment device to re-oxidize high-salt organic wastewater after it has been treated by the cathodic reduction dechlorination stage. After the initial reduction treatment, the wastewater contains dechlorinated organic intermediates, and the residual chlorine-containing oxidizing components have been reduced, thus reducing the amount of chlorine-containing oxidizing components in the wastewater that can continue to participate in the formation of chlorine-containing organic intermediates.

[0055] Before entering the re-oxidation section, the wastewater containing the dechlorinated organic intermediates first flows through an iron-containing adsorption interface. The iron-containing adsorption interface is formed by an interface structure containing iron components and allowing wastewater to pass through, which enables the dechlorinated organic intermediates to be adsorbed and enriched at the interface, causing the dechlorinated organic intermediates to be oxidized to concentrate from the flowing aqueous phase towards the reaction interface.

[0056] The wastewater, enriched by the iron-containing adsorption interface, enters the re-oxidation section. A cathode reaction interface is set up in the re-oxidation section, with iron-containing active sites located thereon. Oxygen-containing gas is supplied to the vicinity of the cathode reaction interface, causing oxygen to be converted in situ into hydrogen peroxide under cathode reaction conditions. The hydrogen peroxide then forms hydroxyl radicals under the action of the iron-containing active sites.

[0057] After the wastewater enters the re-oxidation stage, the dechlorinated organic intermediates come into contact with in-situ generated hydrogen peroxide at the cathode reaction interface, and undergo an oxidation reaction with hydroxyl radicals under the action of iron-containing active sites. This reaction further destroys the organic molecular structure of the dechlorinated organic intermediates, transforming them into low-molecular-weight organic compounds or mineralized products.

[0058] The cathode reaction interface is sequentially configured with a dechlorination organic intermediate enrichment zone and a hydroxyl radical generation zone along the water flow direction. Wastewater containing the dechlorination organic intermediates first passes through the dechlorination organic intermediate enrichment zone, where the intermediates are retained and their local concentration is increased. Subsequently, the wastewater enters the hydroxyl radical generation zone, where it undergoes hydroxyl radical oxidative degradation.

[0059] like Figure 5 As shown, the incoming water first passes through the iron-containing adsorption interface, and then enters the re-oxidation section, where the dechlorinated organic intermediates are continuously enriched and the hydroxyl radical generation zone is arranged along the water flow direction. The figure distinguishes the iron-containing adsorption interface, the enrichment zone, the hydroxyl radical generation zone, and the re-oxidation section with different shades, demonstrating the treatment path where the dechlorinated organic intermediates are first enriched at the interface, and then enter the region where iron-containing active sites and hydroxyl radicals interact. Structurally, this indicates that the re-oxidation section is not a single oxidation space, but rather an interfacial reaction process involving enrichment followed by degradation.

[0060] In this embodiment, the wastewater flow rate VT entering the re-oxidation stage is 18.0 L / h, the organic pollutant concentration US in the influent to the re-oxidation stage is 312 mg / L, and the organic pollutant concentration UE in the effluent from the re-oxidation stage is 74 mg / L. The organic pollutant reduction MO per hour in the re-oxidation stage is calculated using the following formula:

[0061] In the formula, MO represents the mass of organic pollutants reduced per hour in the re-oxidation stage, in g / h; VT represents the volumetric flow rate of wastewater entering the re-oxidation stage, in L / h; US represents the mass concentration of organic pollutants in the influent of the re-oxidation stage, in mg / L; and UE represents the mass concentration of organic pollutants in the effluent of the re-oxidation stage, in mg / L. The derivation of this formula is based on the following: the reduction of organic pollutants by the re-oxidation stage is represented by the difference in organic pollutant concentrations between the influent and effluent, which is US - UE, in mg / L; multiplying the concentration difference by the wastewater volumetric flow rate VT yields the mass of organic pollutants reduced per hour, in mg / h; since 1000 mg equals 1 g, dividing by 1000 gives MO in g / h.

[0062] Substituting VT = 18.0 L / h, US = 312 mg / L, and UE = 74 mg / L into the above formula, we get:

[0063] like Figure 6 As shown, the concentration of organic pollutants in the influent and effluent of the re-oxidation section decreased from 312 mg / L to 74 mg / L. The dashed line representing the decreasing path corresponds to the direction in which the organic intermediates from dechlorination are further oxidized and degraded within the re-oxidation section. The hourly reduction rate indicated in the figure is 4.284 g / h, consistent with the above calculation results, indicating that under the stated flow rate conditions, the re-oxidation section can continue to reduce the oxidizable organic intermediates formed after the preceding reductive dechlorination.

[0064] In this embodiment, the residence time TF of the wastewater in the dechlorination organic intermediate enrichment zone is 9 min, and the residence time TG of the wastewater in the hydroxyl radical generation zone is 21 min. The residence time proportion θZ in the dechlorination organic intermediate enrichment zone is calculated according to the following formula:

[0065] In the formula, θZ represents the proportion of residence time in the dechlorination organic intermediate enrichment zone, in %; TF represents the residence time of wastewater in the dechlorination organic intermediate enrichment zone, in min; and TG represents the residence time of wastewater in the hydroxyl radical generation zone, in min. The derivation of this formula is based on the following: the cathode reaction interface along the water flow direction includes both the dechlorination organic intermediate enrichment zone and the hydroxyl radical generation zone. The total interfacial residence time of wastewater in these two zones is TF + TG; TF is the residence time of wastewater in the dechlorination organic intermediate enrichment zone, and the ratio of TF to the total interfacial residence time represents the proportion of residence time in the enrichment zone, which is then multiplied by 100% to obtain the percentage.

[0066] Substituting TF = 9 min and TG = 21 min into the above formula, we get:

[0067] like Figure 7 As shown, the total residence time at the cathode reaction interface is 30 min, of which the residence time in the dechlorination organic intermediate enrichment zone is 9 min, accounting for 30%, and the residence time in the hydroxyl radical generation zone is 21 min, accounting for 70%. This residence time allocation allows the dechlorination organic intermediate to undergo interfacial retention and concentration increase before entering the hydroxyl radical generation zone, thereby enhancing its contact continuity with the subsequent oxidation reaction zone.

[0068] After treatment in the re-oxidation stage, the concentration of organic pollutants in the effluent decreased from 312 mg / L to 74 mg / L. At the same time, since the residual chlorine-containing oxidizing components had already undergone reduction treatment before entering the re-oxidation stage, the degree of regeneration of chlorine-containing organic intermediates in the re-oxidation stage was reduced.

[0069] By means of the above method, the dechlorination organic intermediate products are first enriched in the enrichment zone of the iron-containing adsorption interface and the cathode reaction interface, and then enter the hydroxyl radical generation zone for oxidative degradation. This improves the degradation efficiency of the dechlorination organic intermediate products in the re-oxidation section and reduces the content of organic pollutants and organic halogens in the effluent.

[0070] Example 3: A certain unit used the same electro-Fenton co-treatment pathway as described above to continuously treat another batch of high-salt organic wastewater containing chloride ions and organic pollutants. This embodiment illustrates the treatment process when the electro-Fenton oxidation section, the oxygen-free transition zone, the cathode reduction dechlorination section, the iron-containing adsorption interface, and the re-oxidation section are continuously combined. The volumetric flow rate of the high-salt organic wastewater being treated was 20.0 L / h, the influent chloride ion concentration was 20500 mg / L, the organic pollutant concentration was 465 mg / L, and the organic halogen concentration (calculated as chlorine) was 10.8 mg / L.

[0071] like Figure 1 As shown, high-salt organic wastewater first enters the electro-Fenton oxidation section. This section features an iron-containing cathode reaction interface, allowing organic pollutants to be adsorbed or retained on the pores, rough surfaces, iron-containing components, or conductive carrier surfaces of the iron-containing cathode reaction interface, and then concentrated from the main aqueous phase towards the reaction interface. Oxygen-containing gas is introduced near the iron-containing cathode reaction interface at a supply rate of 0.90 L / min. The wastewater's residence time in this section is 26 min, allowing oxygen to continuously generate hydrogen peroxide in situ under cathode reaction conditions, and forming hydroxyl radicals under the action of iron-containing active sites.

[0072] Within the electro-Fenton oxidation stage, some organic pollutants are oxidized by hydroxyl radicals, their molecular structures are destroyed, and organic intermediates that can continue to react are formed. Simultaneously, high concentrations of chloride ions form chlorine-containing oxidizing components in the oxidizing environment, which then contact the organic pollutants already enriched at the iron-containing cathode reaction interface. By ensuring that this contact primarily occurs at the iron-containing cathode reaction interface, the chlorine-containing oxidizing components participate in the activation of organic pollutants, reducing their non-directional chlorination in the main aqueous phase.

[0073] After treatment in the electro-Fenton oxidation stage, the concentration of organic pollutants decreased from 465 mg / L to 338 mg / L. Because chlorine-containing oxidizing components formed during chloride ion conversion also occurred in this stage, some organic intermediates formed chlorine-containing organic intermediates, resulting in an organic halogen concentration (based on chlorine) of 14.2 mg / L before entering the subsequent oxygen-free transition zone. This change characterizes the state of the chlorine-containing organic intermediates after oxidative activation entering the subsequent reductive dechlorination step, and does not consider the complete removal of organic halogens by the electro-Fenton oxidation stage alone as the treatment endpoint.

[0074] The effluent from the electro-Fenton oxidation section then enters an oxygen-free transition zone. No oxygen-containing gas is supplied to this zone, and the wastewater remains for 8 minutes, allowing the dissolved oxygen introduced from the preceding section to be further consumed or dissipated during the flow. Therefore, before the wastewater contacts the reduction cathode of the cathodic reduction dechlorination section, the competition for electron transfer between oxygen and the cathode is weakened, creating low-oxygen conditions for chlorinated organic intermediates and residual chlorinated oxidizing components to accept electron transfer.

[0075] After leaving the oxygen-free transition zone, the wastewater enters the cathode reduction dechlorination section. The oxygen gas supply in this section is controlled at 0.06 L / min, significantly lower than the 0.90 L / min in the electro-Fenton oxidation section; the wastewater residence time in this section is 18 min. A halogen-containing organic matter retention interface is set on the cathode surface, causing chlorinated organic intermediates to first remain near the reduction cathode and increase the local reaction concentration. Subsequently, they accept electron transfer from the cathode, weakening or removing the chlorine-containing structures and forming dechlorinated organic intermediates.

[0076] The oxygen supply reduction rate of the cathode reduction dechlorination section relative to the electro-Fenton oxidation section is (0.90-0.06) / 0.90×100%=93.3%. Under this oxygen supply difference, less of the cathode electrons are consumed in competition with oxygen, and more are used for the reduction dechlorination of chlorine-containing organic intermediates and the reduction and conversion of residual chlorine-containing oxidizing components.

[0077] After treatment in the cathode reduction dechlorination section, the concentration of organic halogens, calculated as chlorine, decreased from 14.2 mg / L before entering the section to 4.5 mg / L, with a corresponding reduction dechlorination rate of (14.2 - 4.5) / 14.2 × 100% = 68.3%. Simultaneously, the residual chlorine-containing oxidizing components, calculated as available chlorine, decreased from 6.8 mg / L to 0.9 mg / L, indicating that the residual chlorine-containing oxidizing components were significantly reduced under the cathode electron transfer effect and mainly converted towards chloride ions.

[0078] The concentration of organic pollutants in the effluent from the cathodic reduction dechlorination stage was 301 mg / L. The primary function of this stage is not solely to achieve deep oxidation of organic pollutants, but rather to preferentially weaken or remove the chlorine-containing structures in chlorinated organic intermediates and to reduce residual chlorinated oxidizing components. Therefore, after the cathodic reduction dechlorination stage, the main target of treatment in the wastewater changes from chlorinated organic intermediates to dechlorinated organic intermediates that can still be oxidized.

[0079] Subsequently, the wastewater containing dechlorination organic intermediates first flows through an iron-containing adsorption interface located at the inlet of the re-oxidation section. This iron-containing adsorption interface is formed by iron-containing components and an interfacial structure that allows wastewater to pass through, causing the dechlorination organic intermediates to migrate and accumulate from the flowing aqueous phase towards the iron-containing adsorption interface. After passing through this interface, the wastewater continues into the dechlorination organic intermediate enrichment zone and the hydroxyl radical generation zone, which are sequentially arranged along the water flow direction.

[0080] In this embodiment, the residence time of wastewater in the dechlorination organic intermediate enrichment zone is 10 min, and the residence time in the hydroxyl radical generation zone is 24 min, for a total interfacial residence time of 34 min. The residence time in the enrichment zone accounts for 10 / (10+24)×100%=29.4%. This residence time allocation allows the dechlorination organic intermediates to undergo interfacial retention and local concentration increase before entering the hydroxyl radical generation zone.

[0081] In the re-oxidation section, oxygen-containing gas is supplied at a rate of 0.78 L / min to the vicinity of the cathode reaction interface, allowing oxygen to be regenerated in situ as hydrogen peroxide under cathode reaction conditions. Hydrogen peroxide forms hydroxyl radicals at iron-containing active sites, which then oxidize and degrade the dechlorinated organic intermediates that have already accumulated at the iron-containing adsorption interface and enrichment zone. Since the residual chlorinated oxidizing components have already undergone reduction treatment before entering the re-oxidation section, the amount of chlorinated oxidizing components that can continue to participate in the formation of chlorinated organic intermediates in the re-oxidation section is reduced, thus helping to minimize re-chlorination during the re-oxidation process.

[0082] After treatment in the re-oxidation stage, the concentration of organic pollutants decreased from 301 mg / L in the influent to 62 mg / L. The removal rate of organic pollutants by the re-oxidation stage was (301-62) / 301×100%=79.4%. Based on a wastewater volumetric flow rate of 20.0 L / h, the re-oxidation stage reduced the organic pollutant mass by 20.0×(301-62) / 1000=4.780 g / h per hour, indicating that the dechlorinated organic intermediates formed after reduction dechlorination can continue to be effectively reduced in the re-oxidation stage.

[0083] Based on the entire electro-Fenton co-treatment pathway, the influent organic pollutant concentration is 465 mg / L, and the final effluent organic pollutant concentration is 62 mg / L, with a comprehensive removal rate of (465-62) / 465×100%=86.7%. Calculated at a continuous treatment flow rate of 20.0 L / h, the organic pollutant reduction per hour throughout the entire treatment pathway is 20.0×(465-62) / 1000=8.060 g / h.

[0084] The final effluent concentration of organic halogens (calculated as chlorine) was 2.7 mg / L, a 75.0% reduction compared to the initial influent concentration of 10.8 mg / L. This result indicates that although chloride ions participate in the formation of chlorinated organic intermediates during the electro-Fenton oxidation stage, the subsequent low-oxygen cathode reduction dechlorination stage, which first targets and reduces chlorinated organic intermediates and residual chlorinated oxidizing components, followed by interfacial enrichment and re-oxidation of the dechlorinated organic intermediates, can simultaneously reduce both organic pollutants and organic halogens in the final effluent.

[0085] In this embodiment, a continuous oxidation, reduction, and re-oxidation treatment path is formed from the electro-Fenton oxidation section, the oxygen-free transition zone, the cathodic reduction dechlorination section, to the re-oxidation section. The initial electro-Fenton oxidation section weakens the structure of recalcitrant organic pollutants and forms an intermediate system that can continue to react; the oxygen-free transition zone and the low-oxygen cathodic reduction dechlorination section preferentially direct electron transfer towards chlorinated organic intermediates and residual chlorinated oxidizing components; the subsequent iron-containing adsorption interface, enrichment zone, and hydroxyl radical generation zone enrich the dechlorinated organic intermediates before deep oxidation. Through the continuous functional coordination of each treatment section, the oxidation and removal of organic pollutants, the reduction and dechlorination of chlorinated organic intermediates, and the subsequent deep degradation of dechlorination products can be achieved under high chlorine and high salinity conditions.

Claims

1. A method for the electro-Fenton co-treatment of high-salt organic wastewater for water pollution control and treatment, characterized in that, include: High-salt organic wastewater containing chloride ions and organic pollutants is sequentially fed into the electro-Fenton oxidation section, the cathode reduction dechlorination section, and the re-oxidation section. In the electro-Fenton oxidation section, oxygen-containing gas is supplied to the iron-containing cathode reaction interface and hydrogen peroxide is generated in situ. Hydrogen peroxide forms hydroxyl radicals under the action of iron-containing active sites, which oxidize and degrade organic pollutants. In the electro-Fenton oxidation section, organic pollutants are brought into contact with chlorine-containing oxidizing components formed by the conversion of chloride ions at the iron-containing cathode reaction interface to generate chlorine-containing organic intermediates. Subsequently, wastewater containing the chlorine-containing organic intermediates and residual chlorine-containing oxidizing components is passed into the cathode reduction dechlorination section, where the chlorine-containing organic intermediates and residual chlorine-containing oxidizing components are reduced by cathode electron transfer with reduced oxygen supply. In the cathodic reduction dechlorination section, dechlorinated organic intermediates are obtained, and the residual chlorinated oxidizing components are converted into chloride ions. Then, the wastewater containing the dechlorinated organic intermediates is introduced into the re-oxidation section, where the dechlorinated organic intermediates are degraded by electro-Fenton oxidation at the iron-containing cathode reaction interface, thereby reducing the content of organic pollutants and organic halogens in the effluent.

2. The electro-Fenton co-treatment method for controlling and treating high-salt organic wastewater pollution according to claim 1, characterized in that, In the electro-Fenton oxidation section, the organic pollutants are first adsorbed or retained at the iron-containing cathode reaction interface, and then come into contact with the chlorine-containing oxidizing component, so that the chlorine-containing oxidizing component participates in the activation of organic pollutants at the iron-containing cathode reaction interface and inhibits the chlorination reaction in the main aqueous phase.

3. The electro-Fenton synergistic treatment method for controlling and treating high-salt organic wastewater pollution according to claim 1, characterized in that, The oxygen supply in the cathode reduction dechlorination section is lower than that in the electro-Fenton oxidation section, so that the cathode electrons in the cathode reduction dechlorination section are transferred for the reduction dechlorination of the chlorine-containing organic intermediate and the residual chlorine-containing oxidizing components.

4. The electro-Fenton co-treatment method for controlling and treating high-salt organic wastewater pollution according to claim 1, characterized in that, Before entering the re-oxidation section, the dechlorinated organic intermediate undergoes reduction treatment of the residual chlorine-containing oxidizing components in the cathodic reduction dechlorination section, and continues to react with hydrogen peroxide, iron-containing active sites, and hydroxyl radicals in the re-oxidation section.

5. The electro-Fenton synergistic treatment method for controlling and treating high-salt organic wastewater pollution according to claim 3, characterized in that, An oxygen-free transition zone is set before the cathode reduction and dechlorination section, so that the dissolved oxygen brought in from the electro-Fenton oxidation section is consumed or dissipated before contacting the reduction cathode, thereby reducing the competition of oxygen for electron transfer at the cathode.

6. The electro-Fenton co-treatment method for controlling and treating high-salt organic wastewater pollution according to claim 3, characterized in that, A halogenated organic matter retention interface is formed on the cathode surface of the cathode reduction dechlorination section, so that the chlorinated organic intermediate is first retained at the halogenated organic matter retention interface, and then undergoes dechlorination reaction by accepting electron transfer from the cathode.

7. The electro-Fenton co-treatment method for controlling and treating high-salt organic wastewater pollution according to claim 3, characterized in that, The cathodic reduction dechlorination section reduces the residual chlorine-containing oxidizing components to chloride ions, and allows the chloride ions to enter the re-oxidation section with the dechlorinated wastewater, thereby reducing the re-generation of chlorine-containing organic intermediates in the re-oxidation section.

8. The electro-Fenton co-treatment method for controlling and treating high-salt organic wastewater pollution according to claim 4, characterized in that, Before entering the re-oxidation section, the dechlorinated organic intermediate product passes through an iron-containing adsorption interface, which enriches the dechlorinated organic intermediate product at the iron-containing adsorption interface before it enters the re-oxidation section.

9. The electro-Fenton co-treatment method for controlling and treating high-salt organic wastewater pollution according to claim 4, characterized in that, The iron-containing active sites in the re-oxidation section are located at the cathode reaction interface, and the dechlorinated organic intermediate reacts with hydrogen peroxide and hydroxyl radicals at the cathode reaction interface.

10. The electro-Fenton synergistic treatment method for controlling and treating high-salt organic wastewater pollution according to claim 9, characterized in that, The cathode reaction interface has a dechlorination organic intermediate enrichment zone and a hydroxyl radical generation zone arranged sequentially along the water flow direction, so that the dechlorination organic intermediate is first retained in the dechlorination organic intermediate enrichment zone and then enters the hydroxyl radical generation zone for oxidative degradation.

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