Membraneless anti-liquid-flooding ventilation flow type electrolytic cell module and application thereof

Abstract

The present application relates to a membrane-free anti-liquid flooding ventilation flow type electrolytic cell module and application of the electrolytic cell module in situ preparation of hydrogen peroxide by electrocatalytic two-electron oxygen reduction. The present application comprises an electrolytic cell shell, which encloses an electrolytic reaction cavity, and the electrolytic cell shell is provided with a gas inlet, a liquid inlet and a liquid outlet. An anode and a cathode are arranged in the electrolytic reaction cavity. The cathode is a gas diffusion electrode, the side close to the electrolytic cell shell is a gas diffusion layer which can permeate gas, and the side close to the anode is a cathode catalyst layer loaded with a catalyst. There is no ion exchange membrane between the anode and the cathode. The present application overcomes the problem of dependence on expensive ion exchange membranes in the existing electrolytic cell, and the problem of membrane pollution and failure. The present application provides an electrolytic cell module with a membrane-free structure, greatly reduces the equipment cost and operation difficulty, solves the problems of product cross oxidation and low Faraday efficiency in a membrane-free system, realizes efficient generation and immediate export of hydrogen peroxide under the condition of no diaphragm, and solves the problems of easy liquid flooding of the gas diffusion electrode and easy damage of the catalyst layer under the condition of large flow and flow, and significantly improves the stability of long-term operation of the device.

Description

Technical Field

[0001] This invention relates to the field of electrochemical equipment and water treatment technology, and more specifically, to a membrane-free, flood-resistant, gas-permeable electrolyzer module, and its application in the in-situ preparation of hydrogen peroxide by electrocatalytic two-electron oxygen reduction. Background Technology

[0002] Hydrogen peroxide (H2O2) is an extremely important basic chemical raw material and green oxidant, widely used in many fields such as pulp bleaching, wastewater treatment, medical disinfection, and chemical synthesis. Because its decomposition products are only water and oxygen, producing no secondary pollution, its market demand is increasing significantly year by year due to increasingly stringent environmental protection requirements.

[0003] Currently, the mainstream industrial method for producing H2O2 is the anthraquinone process. However, this method has inherent drawbacks, including a long process flow, high energy consumption, the need for large amounts of organic solvents, and the potential for generating toxic byproducts. Furthermore, the anthraquinone process is only suitable for large-scale centralized plant production, while high-concentration H2O2, as a hazardous chemical, poses significant safety risks and high logistics costs during storage and long-distance transportation. Therefore, developing a safe, green, and distributed on-site production technology for H2O2 has become a hot research topic in the industry. Utilizing renewable electricity, water and oxygen are converted into H2O2 through an electrocatalytic two-electron oxygen reduction reaction (2e⁻ORR). The reaction conditions are mild, requiring only air / oxygen, water, and electricity to achieve in-situ product generation. This is a highly promising green alternative that perfectly meets the core requirements of distributed production.

[0004] As this technology advances from the laboratory to industrial applications, scenarios such as large-scale dyeing and printing wastewater treatment and municipal sewage upgrading place extremely high demands on H2O2 production and treatment liquid throughput. However, existing H2O2 electrosynthesis devices are mainly based on gas diffusion electrode flow electrolyzers, whose main components include a cathode gas diffusion electrode, an ion exchange membrane, and an anodic oxidation electrode. When facing large-scale, industrial-grade production, these electrolyzers reveal numerous insurmountable technical obstacles: Ion exchange membranes are expensive and highly susceptible to fouling and degradation. Traditional 2e⁻ORR flow-through electrolyzers typically rely on proton exchange membranes or anion exchange membranes to separate the anode and cathode chambers, preventing the diffusion of H₂O₂ generated at the cathode to the anode where it is oxidized and decomposed. However, commercially available ion exchange membranes are extremely expensive, accounting for the majority of the electrolyzer's material cost. More critically, when treating actual industrial water or wastewater, the membrane material is highly prone to metal ion fouling, organic scaling, or biological blockage, leading to a sharp increase in membrane resistance and even physical damage. This results in extremely high system maintenance costs and a very short lifespan.

[0005] To reduce costs and eliminate membrane fouling, the industry has attempted to develop membrane-free electrolyzers. However, membrane-free systems face the serious problem of product cross-permeation. In traditional membrane-free electrolyzers, the lack of a physical membrane barrier allows H2O2 generated at the cathode to easily cross over to the anode surface through fluid diffusion or convection, resulting in irreversible electrochemical oxidation. This leads to a significant decrease in the system's Faraday efficiency and product accumulation concentration, failing to meet industrial requirements.

[0006] Another key factor limiting the performance of flow electrolyzers is the susceptibility of gas diffusion electrodes to flooding and mechanical damage under high flow rates. While active aeration or the use of gas diffusion electrodes can enhance oxygen mass transfer, traditional electrode structures are highly susceptible to severe flooding under the intense physical scouring of high-flow-rate fluids and high liquid back pressure. This means that electrolyte is forcibly injected into the pores, which not only restricts oxygen supply but also leads to mechanical stripping and physical damage to the catalyst layer, making long-term stable operation difficult.

[0007] In summary, existing electrolyzer technology cannot effectively address the issues of product cross-oxidation, efficient oxygen mass transfer, and gas diffusion electrode flooding or water inrush under high-flow conditions while removing expensive and fragile ion exchange membranes. There is an urgent need to develop a novel membrane-free, flow-through electrolyzer structure to achieve low-cost, high-throughput, and long-life industrial production of H2O2. Summary of the Invention

[0008] In view of the above-mentioned deficiencies of the prior art, the present invention aims to achieve the following objectives: 1. Overcome the problems of existing electrolyzers relying on expensive ion exchange membranes and the membranes being prone to fouling and failure, and provide a membrane-free electrolyzer module, which greatly reduces equipment costs and maintenance difficulty; 2. To solve the problems of cross-oxidation of products and low Faraday efficiency in membrane-free systems, and to achieve efficient generation and immediate export of H2O2 under membrane-free conditions; 3. It fundamentally solves the problems of easy flooding of gas diffusion electrodes and easy damage to the catalyst layer under high flow conditions, significantly improving the long-term stability of the device; it overcomes the limitations of low oxygen mass transfer efficiency and large system pressure drop under high flow conditions, and is suitable for industrial-grade high-throughput in-situ preparation of H2O2.

[0009] To achieve the above-mentioned objectives, the present invention adopts the following technical solution: A membrane-free, flood-resistant, gas-permeable electrolytic cell module includes an electrolytic cell shell, which encloses an electrolytic reaction chamber. The electrolytic cell shell has an air inlet, a liquid inlet, and a liquid outlet. An anode and a cathode are disposed inside the electrolytic reaction chamber. The cathode is a gas diffusion electrode, with a gas diffusion layer permeable to gas on its side near the electrolytic cell shell and a cathode catalytic layer loaded with a catalyst on its side near the anode. There is no ion exchange membrane between the anode and the cathode. A cathode gas flow channel is formed between the cathode and the outer shell of the electrolytic cell, and the gas inlet is connected to the cathode gas flow channel; a gas-liquid balance chamber is formed between the sides of the cathode and anode near the liquid outlet and the outer shell of the electrolytic cell, and the gas-liquid balance chamber is simultaneously connected to the cathode gas flow channel and the liquid outlet; The liquid inlet is connected to the liquid inlet end of the electrolysis reaction chamber, and the liquid outlet is connected to the liquid outlet end of the electrolysis reaction chamber. The electrolyte flows into the electrolysis reaction chamber through the liquid inlet, and after flowing through the gap between the anode and the cathode, it carries the product generated by the cathode and flows out from the liquid outlet. Gas enters the cathode gas flow channel through the inlet, passes through the cathode and enters the gas-liquid balance chamber, where a gas phase pressure buffer layer is formed. The dynamic balance between gas and liquid phase pressures suppresses flooding. Finally, the gas is bubbled through the electrolyte and discharged from the outlet along with the electrolyte.

[0010] Furthermore, the outer shell of the electrolytic cell module is a plate-like stacked structure, which includes a cathode end plate, a cathode plate, an anode plate and an anode end plate in sequence from the gas inlet side to the liquid outlet side. The cathode is fixed on the cathode plate and the anode is fixed on the anode plate.

[0011] Furthermore, an air inlet is provided on the cathode end plate, and a cathode plate air inlet and outlet hole and a cathode gas flow channel are provided on the cathode plate. The air inlet, cathode plate air inlet and outlet hole and cathode gas flow channel are connected in sequence to form an air passage from the air inlet to the back side of the cathode.

[0012] Furthermore, the cavity between the anode plate and the cathode plate forms the electrolysis reaction chamber and the gas-liquid balance chamber, and the liquid inlet and liquid outlet are located on the anode end plate or the cathode plate.

[0013] Furthermore, the anode is a mesh anode with a mesh pore size of 0.5-5mm, a porosity of ≥60%, and is made of any one of titanium-based coating material, stainless steel, or graphite.

[0014] Furthermore, the gas diffusion layer of the cathode is any one of carbon paper, carbon felt, or waterproof carbon cloth, and the cathode catalytic layer provided with the cathode is loaded with a two-electron oxygen reduction highly selective catalyst.

[0015] Furthermore, the opening height of the liquid outlet is lower than the lowest liquid level height of the gas-liquid balance chamber.

[0016] Another objective of this invention is to provide an application of the aforementioned membrane-free, flood-resistant, aeration-through-flow electrolyzer module, specifically a method for preparing hydrogen peroxide using the electrolyzer module, comprising the following steps: S1. The electrolyte is introduced into the electrolysis reaction chamber through the inlet of the electrolytic cell module, and the electrolyte flow rate is controlled to be 10-1000 mL / min. S2. Oxygen-containing gas is introduced into the cathode gas flow channel through the inlet, and the gas flow rate is controlled at 0.5-5 L / min; S3. Apply voltage to the anode and cathode, and control the current density to 10-200 mA / cm². When the electrolyte flows through the cathode surface, it carries hydrogen peroxide generated by the two-electron oxygen reduction reaction and outputs hydrogen peroxide solution from the outlet.

[0017] Furthermore, the electrolyte is any one of tap water, industrial wastewater, or municipal sewage, and the oxygen-containing gas is air or oxygen.

[0018] Beneficial effects Compared with the prior art, the present invention has the following significant advantages: This invention completely eliminates the need for ion exchange membranes required in traditional electrolyzers, thus eliminating the high equipment costs associated with membrane materials. At the same time, it completely solves the problems of performance degradation and shortened lifespan caused by ion exchange membrane fouling, scaling, and clogging in industrial water treatment scenarios, significantly reducing system operation and maintenance costs and adapting to the long-term operation requirements of complex water qualities.

[0019] 2. This invention forms a stable gas-phase pressure buffer layer on the cathode surface by setting a gas-liquid balance cavity connected to the liquid outlet in the gas diffusion layer of the cathode. This can dynamically balance the gas-liquid phase pressure on both sides of the cathode, avoid flooding caused by the electrolyte flowing back into the cathode pores under a large flow of liquid phase, and prevent the catalyst layer from being washed away by the liquid phase, thus significantly improving the long-term operational stability of the electrode.

[0020] 3. This invention employs a flow field design, where the electrolyte flows in from the inlet and is swept at high speed along the gap between the anode and cathode. This immediately carries the H2O2 generated on the cathode surface out of the electrolysis chamber, significantly shortening the residence time of the product in the electrolysis chamber and preventing the product from diffusing to the anode and being oxidized and decomposed. At the same time, the continuous ventilation on the cathode side forms a gas-liquid two-phase interface barrier, further blocking the diffusion of H2O2 to the anode side. This achieves high Faraday efficiency and high product concentration under membrane-free conditions.

[0021] 4. This invention adopts an active ventilation cathode design, which allows oxygen to directly pass through the gas diffusion electrode to reach the catalytic reaction interface of the cathode. This breaks through the mass transfer limit of the traditional dissolved oxygen mode and significantly improves the oxygen mass transfer efficiency. It can maintain high current density and high product generation rate under high flow conditions. At the same time, the flow channel structure design reduces the system pressure drop under high flow conditions and reduces pumping parasitic energy consumption, making it suitable for industrial-grade high-throughput applications.

[0022] 5. The electrolytic cell of the present invention has a modular stacked structure, which can be flexibly assembled and scaled up. It can be miniaturized and integrated into small household appliances such as dishwashers, floor scrubbers, and drinking water disinfection equipment as a single module, or stacked in multiple modules for industrial scenarios such as large-scale dyeing and printing wastewater treatment and municipal sewage upgrading and transformation, so as to realize the "on-demand use" of H2O2 and completely solve the safety hazards and cost problems of H2O2 storage and transportation. Attached Figure Description

[0023] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0024] Figure 1 is a cross-sectional schematic diagram of the working principle of the membrane-free anti-flooding ventilated electrolytic cell module of the present invention; in the figure, A is the airflow direction and B is the water flow direction.

[0025] Figure 2 is an exploded view of the stacked structure of the membrane-free anti-flooding ventilated electrolytic cell module of the present invention; Figure 3 This is a cross-sectional schematic diagram of the anti-flooding mechanism of the membrane-free anti-flooding ventilated electrolytic cell module of the present invention. In the figure, B represents the water flow direction, Δpτ represents the pressure released by the bubble 15, and Δp represents the pressure disturbance caused by the water flow at the inlet.

[0026] Explanation of reference numerals in the attached diagram: 1 - Electrolytic cell outer shell; 2 - Liquid outlet; 3 - Electrolyte; 4 - Anode; 41 - Anode plate; 42 - Anode end plate; 5 - Liquid inlet; 6 - Gas inlet; 7 - Cathode; 71 - Cathode plate; 72 - Cathode end plate; 8 - Cathode catalyst layer; 9 - Gas-liquid balance chamber; 10 - Cathode plate gas inlet / outlet hole; 11 - Cathode slot; 12 - Cathode gas flow channel; 13 - Anode slot; 14 - Fixing screw hole; 15 - Bubbling; 16 - Electrolysis reaction chamber. Detailed Implementation

[0027] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention. Those skilled in the art should understand that the specific embodiments described below are only for illustrating and explaining the present invention, and are not intended to limit the present invention.

[0028] Example 1 This embodiment provides a membrane-free, flood-resistant, ventilated, and flow-through electrolytic cell module, which has a plate-like stacked structure. Its exploded structure is shown in Figure 2. From the air inlet side to the liquid outlet side, the cathode end plate 72, cathode plate 71, anode plate 41, and anode end plate 42 are stacked in sequence. The cathode end plate 72 and anode end plate 42 are locked and fixed to the electrolytic cell shell 1 by fasteners in the outer peripheral fixing screw holes 14. The effective reaction area of ​​the cathode 7 and anode 4 is 50 cm².

[0029] The cathode plate 71 has a cathode slot 11, and the cathode 7 (gas diffusion electrode) is fixedly installed in the cathode slot 11; the anode plate has an anode slot 13, and the mesh anode 4 is fixedly installed in the anode slot 13; there is no ion exchange membrane between the cathode 7 and the mesh anode 4, and the gap between the two forms an electrolysis reaction chamber 16.

[0030] An air inlet 6 is provided at the bottom of the cathode end plate 72, and a cathode plate air inlet 10 and a cathode gas flow channel 12 are provided on the cathode plate 71. The air inlet 6 is connected to the cathode gas flow channel 12 through the cathode plate air inlet 10. The cathode gas flow channel 12 is located on the back side of the cathode 7, forming an air supply path from the air inlet to the back side of the cathode.

[0031] A gas-liquid balance chamber 9 is formed in the gap between the sides of the anode plate 41 and the cathode plate 72 above the electrolysis reaction chamber 16 and the outer shell 1 of the electrolysis cell. The gas-liquid balance chamber 9 is connected to the side of the cathode 7 facing the anode 4, and is also connected to the liquid outlet of the electrolysis reaction chamber 16. The anode plate 42 is provided with a liquid inlet 5 and a liquid outlet 2. The liquid inlet 5 is connected to the liquid inlet of the electrolysis reaction chamber 16, and the liquid outlet 2 is connected to the liquid outlet of the electrolysis reaction chamber 16. The opening height of the liquid outlet 2 is lower than the lowest liquid level of the gas-liquid balance chamber 9. If the liquid outlet height is higher than the lowest liquid level of the gas-liquid balance chamber 9, the liquid part of the liquid outlet will flow back to the back of the cathode, thus preventing gas from entering the cathode.

[0032] The working process of the electrolytic cell module in this embodiment is as follows: Electrolyte (tap water) flows into the electrolytic reaction channel through the inlet 2, flows along the surface of the mesh anode 4 towards the cathode 7, and washes the surface of the cathode catalyst layer 8 of the cathode 7 at high speed; Oxygen-containing gas (air or oxygen) enters through the inlet 6, enters the cathode gas channel 12 through the cathode plate air inlet and outlet holes 10, diffuses evenly to the back side of the cathode 7, passes through the gas diffusion layer of the cathode 7 to reach the cathode catalyst layer 8, and provides oxygen for the two-electron oxygen reduction reaction; The remaining gas after the reaction passes through the cathode 7 and enters the gas-liquid balance chamber 9, forming a stable gas phase pressure buffer layer in the gas-liquid balance chamber 9, so that the gas-liquid phase pressure on both sides of the cathode reaches dynamic balance. When the inlet 5 applies a pressure disturbance Δp, the pressure can be quickly conducted to the air in the gas-liquid balance chamber 9 through the liquid phase. The air is compressed and gradually pressurized, and then bubbles 15 from the outlet (see Figure 3 The release of pressure Δpτ allows pressure disturbance Δp to be discharged in a timely manner, while preventing gas accumulation in the reaction area of ​​the cathode catalyst layer 8 and inhibiting backflow of electrolyte into the cathode pores, which could cause flooding. It should be noted that bubbling 15 occurs because unreacted gas and generated hydrogen peroxide react on the catalyst layer surface, creating bubbles in the electrolyte due to pressure changes. These bubbles approach and enter the gas-liquid equilibrium chamber 9, where they break up with pressure changes, releasing hydrogen peroxide and unreacted gas. The hydrogen peroxide then dissolves in the electrolyte as hydrogen peroxide, which is discharged through the outlet. More active bubbling prevents gas accumulation on the catalyst layer surface, thus promoting the electrochemical reaction and hydrogen peroxide production.

[0033] Hydrogen peroxide generated on the cathode surface through the two-electron oxygen reduction reaction is immediately captured by the high-speed flowing electrolyte and flows towards the outlet 2 along with the electrolyte. The gas in the gas-liquid balance chamber 9 is bubbled by the electrolyte and discharged from the outlet 2 together with the electrolyte carrying hydrogen peroxide, thus completing the in-situ preparation of hydrogen peroxide.

[0034] Example 2 Example 2 uses the membrane-free, flood-resistant, gas-flow-through electrolyzer module described in Example 1 to conduct performance tests on in-situ electrocatalytic hydrogen peroxide production. All tests used tap water as the electrolyte and air as the oxygen-containing gas, with the gas flow rate controlled at a constant 2 L / min. The hydrogen peroxide concentration was tested under different current densities and electrolyte flow rates. The test results are shown in the table below:

[0035] The test results above show that the electrolyzer module of the present invention can stably produce hydrogen peroxide in a wide range of current densities and flow rates under conditions of no ion exchange membrane. The product concentration increases linearly with the increase of current density, but decreases as the flow rate of the electrolyte increases too much. Therefore, by adjusting the current density and the electrolyte flow rate, the requirements of hydrogen peroxide concentration and flux in different scenarios can be flexibly adapted.

[0036] Under high current density of 80mA / cm² and high flow rate of 500mL / min, it can still stably produce 70ppm of hydrogen peroxide solution, which fully meets the needs of drinking water disinfection, deep sewage treatment and other scenarios. At the same time, during continuous operation, there are no performance degradation problems caused by electrode flooding, catalyst layer stripping and product cross-oxidation, which have excellent long-term operational stability.

[0037] Furthermore, the modular structure of this invention can be flexibly stacked and scaled up. It can achieve in-situ preparation of industrial-grade high-flow-rate hydrogen peroxide through parallel connection of multiple modules, or it can be miniaturized and integrated into small household appliances such as dishwashers, floor scrubbers, and drinking water disinfection equipment to achieve "on-demand production and use" of hydrogen peroxide, with a wide range of application scenarios.

[0038] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of the present invention should be included within the protection scope of the present invention. Furthermore, the technical features of the various embodiments described in this specification can be arbitrarily combined without contradiction, and all combined technical solutions fall within the protection scope of the present invention.

Claims

1. A membrane-free, flood-resistant, ventilated, flow-through electrolytic cell module, comprising an electrolytic cell shell, the electrolytic cell shell enclosing an electrolytic reaction chamber, the electrolytic cell shell having an air inlet, a liquid inlet, and a liquid outlet, and an anode and a cathode disposed within the electrolytic reaction chamber, characterized in that, The cathode is a gas diffusion electrode, with a gas diffusion layer that is permeable to gas on the side near the outer shell of the electrolytic cell, and a cathode catalytic layer loaded with catalyst on the side near the anode. There is no ion exchange membrane between the anode and the cathode. A cathode gas flow channel is formed between the cathode and the outer shell of the electrolytic cell, and the gas inlet is connected to the cathode gas flow channel; a gas-liquid balance chamber is formed between the sides of the cathode and anode near the liquid outlet and the outer shell of the electrolytic cell, and the gas-liquid balance chamber is simultaneously connected to the cathode gas flow channel and the liquid outlet; The liquid inlet is connected to the liquid inlet end of the electrolysis reaction chamber, and the liquid outlet is connected to the liquid outlet end of the electrolysis reaction chamber. The electrolyte flows into the electrolysis reaction chamber through the liquid inlet, and after flowing through the gap between the anode and the cathode, it carries the product generated by the cathode and flows out from the liquid outlet. Gas enters the cathode gas flow channel through the inlet, passes through the cathode and enters the gas-liquid balance chamber, where a gas phase pressure buffer layer is formed. The dynamic balance between gas and liquid phase pressures suppresses flooding. Finally, the gas is bubbled through the electrolyte and discharged from the outlet along with the electrolyte.

2. The membrane-free, flood-resistant, aerated flow-through electrolytic cell module according to claim 1, characterized in that, The outer shell of the electrolytic cell module is a plate-like stacked structure, which includes a cathode end plate, a cathode plate, an anode plate and an anode end plate in sequence from the gas inlet side to the liquid outlet side. The cathode is fixed on the cathode plate and the anode is fixed on the anode plate.

3. The membrane-free, flood-resistant, aerated flow-through electrolytic cell module according to claim 2, characterized in that, An air inlet is provided on the cathode end plate, and a cathode plate air inlet and outlet hole and a cathode gas flow channel are provided on the cathode plate. The air inlet, cathode plate air inlet and outlet hole and cathode gas flow channel are connected in sequence to form an air passage from the air inlet to the back side of the cathode.

4. The membrane-free, flood-resistant, aerated flow-through electrolytic cell module according to claim 2, characterized in that, The cavity between the anode plate and the cathode plate forms the electrolysis reaction chamber and the gas-liquid balance chamber, and the liquid inlet and liquid outlet are located on the anode plate or the cathode plate.

5. The membrane-free, flood-resistant, aerated flow-through electrolytic cell module according to claim 1, characterized in that, The anode is a mesh anode with a mesh pore size of 0.5-5mm and a porosity of ≥60%, and is made of any one of titanium-based coating material, stainless steel or graphite.

6. The membrane-free, flood-resistant, aerated flow-through electrolytic cell module according to claim 1, characterized in that, The gas diffusion layer of the cathode is any one of carbon paper, carbon felt or waterproof carbon cloth, and the cathode catalytic layer of the cathode is loaded with a two-electron oxygen reduction highly selective catalyst.

7. The membrane-free, flood-resistant, ventilated, flow-through electrolytic cell module according to claim 1, characterized in that, The outlet is positioned at a height lower than the minimum liquid level in the gas-liquid balance chamber.

8. An application of the membrane-free, flood-resistant, aerated flow-through electrolyzer module according to any one of claims 1-7, specifically a method for preparing hydrogen peroxide using the electrolyzer module, characterized in that, Includes the following steps: S1. The electrolyte is introduced into the electrolysis reaction chamber through the inlet of the electrolytic cell module, and the electrolyte flow rate is controlled to be 10-1000 mL / min. S2. Oxygen-containing gas is introduced into the cathode gas flow channel through the inlet, and the gas flow rate is controlled at 0.5-5 L / min; S3. Apply voltage to the anode and cathode, and control the current density to 10-200 mA / cm². When the electrolyte flows through the cathode surface, it carries hydrogen peroxide generated by the two-electron oxygen reduction reaction and outputs hydrogen peroxide solution from the outlet.

9. The application of the membrane-free, flood-resistant, aerated flow-through electrolytic cell module according to claim 8, characterized in that, In step S3, the pressure disturbance Δp caused by the water flow at the inlet is offset by the pressure Δpτ released by the hydrogen peroxide generated by the reaction of the cathode catalyst layer and the bubbles formed by the unreacted gas in the electrolyte. This causes the unreacted gas and the electrolyte carrying hydrogen peroxide to be discharged from the outlet, thus completing the preparation of the hydrogen peroxide solution.

10. The application of the membrane-free, flood-resistant, aerated flow-through electrolytic cell module according to claim 8, characterized in that, The electrolyte is any one of tap water, industrial wastewater, or municipal sewage, and the oxygen-containing gas is air or oxygen.

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