Ozone preparation device and method based on condensate electrolysis

Abstract

The application discloses an ozone preparation device and method based on condensate water electrolysis, which comprises a gas pump, a closed humidification tank, an electrolytic cell and a power supply. The gas pump is used for preparing carrier gas and introducing the carrier gas into the closed humidification tank. The closed humidification tank is used for preparing high-humidity gas and introducing the high-humidity gas into the electrolytic cell. The electrolytic cell is used for condensing the high-humidity gas through an anode plate, forming condensate water, entering a membrane electrode assembly and applying a direct current voltage through the power supply. The condensate water is subjected to electrochemical oxidation reaction on an anode catalytic layer to prepare ozone. The application realizes electrochemical ozone preparation of non-pure water under a membrane electrode system through the modes of increasing carrier gas, transferring high-humidity gas and electrolytic cell condensation. The evaporation and condensation process realizes in-situ distillation, provides a relatively pure and uniform condensate water film for the membrane electrode assembly, breaks through the water source purity limitation and provides continuous water source for electrolytic reaction in the membrane electrode assembly.

Description

Technical Field

[0001] This invention pertains to ozone preparation technology, specifically relating to an ozone preparation device and method based on condensate electrolysis. Background Technology

[0002] Ozone is typically produced using either direct water electrolysis or corona discharge. Direct water electrolysis requires pure water or water with low conductivity, and ozone is generated through direct electrolysis using a solid polymer electrolyte or noble metal electrodes.

[0003] For example, patent CN116426947A discloses an apparatus and method for preparing ozone by electrolyzing pure water using an electrolyte-free / zero-gap electrolysis system. A BDD electrode is used as a catalytic electrode to produce O3. Furthermore, while generating ozone, highly reactive free radicals are produced, which can then be used to degrade organic pollutants in wastewater. The method involves assembling the device in the order of BDD electrode – perfluorosulfonic acid proton exchange membrane – stainless steel electrode. The anode and cathode are then clamped and electrically connected to the positive and negative terminals of a power supply via wires on the electrode clamps. The fixed BDD electrode-perfluorosulfonic acid proton exchange membrane-stainless steel electrode assembly is then placed in an electrolytic cell to obtain an electrolyte-free / zero-gap electrolysis system for preparing ozone. Pure water is added to the electrolytic cell, and ozone is prepared by electrolysis of the pure water. This scheme provides an apparatus and method for preparing ozone by electrolyzing pure water using an electrolyte-free / zero-gap electrolysis system.

[0004] The direct water electrolysis method for ozone production faces extremely stringent limitations. For example, the water source must be ultrapure water and is highly sensitive to water quality; uncontrolled water quality can severely impact ozone yield. Currently, direct water electrolysis is primarily used in specific scenarios such as laboratories, medical settings, and semiconductor manufacturing, significantly limiting its commercial application.

[0005] However, in scenarios where water quality cannot be guaranteed, how to achieve stable and reliable ozone production using conventional water sources is a problem that urgently needs to be solved by those skilled in the art. Summary of the Invention

[0006] To address the shortcomings of existing technologies, this invention provides an ozone preparation device and method based on condensate electrolysis. The ozone preparation device includes: a gas pump, a sealed humidification tank, an electrolytic cell, and a power supply. The gas pump prepares a carrier gas and introduces it into the sealed humidification tank. The sealed humidification tank prepares a high-humidity gas and introduces it into the electrolytic cell. The electrolytic cell condenses the high-humidity gas passing through the anode plate to form condensate, which enters the membrane electrode assembly. A DC voltage is applied through the power supply, and the condensate undergoes an electrochemical oxidation reaction in the anode catalyst layer to produce ozone. This invention achieves electrochemical ozone preparation from non-pure water in a membrane electrode system by increasing the carrier gas, transferring high-humidity gas, and condensing in the electrolytic cell, thus solving the ozone preparation problem in scenarios where water quality cannot be guaranteed. The evaporation and condensation processes of this invention achieve in-situ distillation, providing a relatively pure and uniform condensate film for the membrane electrode assembly, overcoming the limitations of water purity and providing a continuous water source for the electrolytic reaction within the membrane electrode assembly.

[0007] In a first aspect, the present invention provides an ozone preparation device based on condensate electrolysis, specifically comprising: an air pump, a sealed humidification tank, an electrolytic cell, and a power supply; An air pump is used to prepare carrier gas and introduce it into a sealed humidification tank. A sealed humidification tank is used to prepare high-humidity gas and introduce the high-humidity gas into an electrolytic cell. An electrolytic cell is used to condense high-humidity gas passing through the anode plate to form condensate, which enters the membrane electrode assembly. A DC voltage is applied through a power source, causing the condensate to undergo an electrochemical oxidation reaction in the anode catalyst layer to produce ozone.

[0008] Furthermore, the DC voltage is 3-5V.

[0009] Furthermore, the relative humidity of high humidity gas is ≥99%, where relative humidity is the ratio of the actual partial pressure of water vapor in moist air to the saturated partial pressure of water vapor under the same temperature and total pressure.

[0010] Furthermore, it also includes a first pipeline and a second pipeline. The front end of the first pipeline is connected to an air pump, and the end of the first pipeline extends into the water-containing liquid in the sealed humidification tank. The carrier gas is introduced into the sealed humidification tank through the first pipeline. A microporous aeration head is provided at the end of the first pipeline, and the average pore size of the microporous aeration head is 3-10 µm. The front end of the second pipeline extends into the sealed humidification tank and is located above the water-containing liquid in the sealed humidification tank. The end of the second pipeline is connected to the anode sub-pipeline and the cathode sub-pipeline. The anode sub-pipeline is connected to the anode plate, and the cathode sub-pipeline is connected to the cathode plate. The insulation temperature of the second pipeline is not less than the temperature of the water-containing liquid in the sealed humidification tank.

[0011] Furthermore, a flow channel structure is provided on the inner surface of the anode plate. The flow channel structure consists of multiple segments with different waveforms. The width of each segment is 0.8-1.5 mm, and the depth is 0.6-0.8 mm. The flow channel structure includes a first straight groove group, a second straight groove group, a third straight groove group, and multiple curved groove sections. The first straight groove group, the second straight groove group, and the third straight groove group are arranged sequentially along the flow direction of the flow channel, and each of the first straight groove group, the second straight groove group, and the third straight groove group includes at least one straight groove section. Each curved groove section is connected to the adjacent straight groove section at both ends. In each straight groove section of the first straight groove group, there are multiple first fins, each of which is parallel to the flow direction of the channel. In each straight groove section of the second straight groove group, there are multiple second fins, each of which is perpendicular to the flow direction of the channel, and adjacent second fins are staggered along the flow direction of the channel.

[0012] Furthermore, the ratio of the number of straight groove sections in the first straight groove group, the second straight groove group, and the third straight groove group is (1~2):(4~8):(1~2); The height of each first fin is 10% to 20% of the channel depth, and the height of each second fin is 30% to 50% of the channel depth.

[0013] Furthermore, the membrane electrode assembly also includes a porous transport layer, which is attached to the outer surface of the anode electrode; The porous transport layer has a gradient pore structure with 3-5 steps along the thickness direction, and the inner wall of the pores of the porous transport layer is attached with a hydrophilic ionomer membrane, which is at least one of perfluorosulfonic acid resin, sulfonated polyether ether ketone, and sulfonated polyimide. The average pore size and porosity of the porous transport layer decrease gradually along the thickness direction, while the hydrophilic ionomer membrane loading of the porous transport layer increases gradually along the thickness direction, which is the direction perpendicular to the anode plate and pointing to the anode electrode. Among them, the average pore size of each step in the porous transport layer is reduced from 10-100 μm to 0.1-10 μm, the porosity is reduced from not less than 70% to 40%-60%, and the hydrophilic ionomer membrane loading is increased from 3-5 wt% to 12-15 wt%.

[0014] Furthermore, the anode plate also integrates a heat dissipation fin array, which is attached to the outer surface of the anode plate. The heat dissipation fin array is in the form of a fin array, with a spacing of 2-4 mm between adjacent heat dissipation fins, and the length and width of the heat dissipation fins are both 55-65 mm.

[0015] Furthermore, a hydrophobic coating is provided inside the corrugated flow channel.

[0016] Secondly, the present invention also provides a method for preparing ozone based on condensate electrolysis, using the ozone preparation apparatus based on condensate electrolysis as described above, specifically including the following steps: Step S1: Prepare carrier gas and introduce it into a sealed humidification tank to prepare high humidity gas; Step S2: Introduce the high-humidity gas into the electrolytic cell; Step S3: High humidity gas is condensed by the anode plate to form condensate, which then enters the membrane electrode assembly; Step S4: Apply a DC voltage to the electrolytic cell, and the condensed water undergoes an electrochemical oxidation reaction in the anode catalyst layer to produce ozone. Further, step S1 specifically includes the following steps: Carrier gas is prepared using an air pump, wherein the flow rate of the carrier gas is 0.5-20 L / min; The carrier gas is introduced into the water-containing liquid in the sealed humidification tank through the first pipeline. The liquid level in the sealed humidification tank is 1 / 2 to 3 / 4 of the tank height, and the temperature of the water-containing liquid is 40-60 ℃. The carrier gas in the sealed humidification tank reaches the preset saturation state, resulting in high-humidity gas.

[0017] Furthermore, in step S1, the carrier gas is at least one of air, oxygen, and nitrogen; A microporous aeration head is installed at the end of the first pipeline, with an average pore size of 3-10µm. The carrier gas is introduced into the water-containing liquid in the sealed humidification tank through the first pipeline, specifically including: The carrier gas enters the microporous aeration head through the first pipeline and disperses into the water-containing liquid in the form of bubbles.

[0018] Furthermore, step S2 specifically includes the following steps: High-humidity gas is introduced into the electrolytic cell through a second pipeline. The front end of the second pipeline extends into the sealed humidification tank and is located above the water-containing liquid in the sealed humidification tank. The end of the second pipeline is connected to the anode sub-pipeline and the cathode sub-pipeline. The anode sub-pipeline is connected to the anode plate, and the cathode sub-pipeline is connected to the cathode plate. The insulation temperature of the second pipeline is not less than the temperature of the water-containing liquid.

[0019] Furthermore, in step S3, the anode plate is made of titanium alloy, the surface temperature of the anode plate is 20-30℃, and the membrane electrode assembly also includes a porous transport layer, which is attached to the inner surface of the anode plate. Step S3 specifically includes the following steps: The high-humidity gas passing through the anode sub-pipe comes into contact with the flow channel structure set on the inner surface of the anode plate, forming micro-droplets; Microdroplets converge and permeate into the membrane electrode assembly through the porous transport layer.

[0020] Furthermore, step S4 specifically includes the following steps: DC voltage 3-5V, current density 0.5-2 A / cm² 2 The electrolyte temperature is 20-30 ℃.

[0021] Furthermore, the catalyst loading in the anode catalyst layer is 40-60 mg / cm³. 2 The catalyst type is tin oxide-based catalyst.

[0022] The ozone preparation apparatus and method based on condensate electrolysis provided by this invention have at least the following beneficial effects: This invention achieves electrochemical ozone preparation from non-pure water in a membrane electrode assembly (MEA) system by adding a carrier gas, transferring high-humidity gas, and condensing in the electrolytic cell. The evaporation and condensation processes of this invention achieve in-situ distillation, providing a relatively pure and uniform condensate film for the MEA assembly, overcoming the limitations of water purity and providing a continuous water source for the electrolytic reaction within the MEA assembly. Attached Figure Description

[0023] Figure 1 A structural diagram of an ozone preparation device based on condensate electrolysis provided by the present invention; Figure 2 A schematic diagram of a membrane electrode assembly according to one embodiment of the present invention; Figure 3 A schematic diagram of a waveform flow channel according to one embodiment of the present invention; Figure 4 A schematic diagram of a porous transport layer according to one embodiment of the present invention; Figure 5 The flowchart illustrates a method for preparing ozone based on the electrolysis of condensate water, as provided by this invention.

[0024] Explanation of reference numerals in the attached drawings: 1-Air pump, 11-First straight groove group, 111-First fin, 12-Second straight groove group, 121-Second fin, 13-Third straight groove group, 100-Straight groove section, 14-Bend groove section, 20-First pipeline, 21-Microporous aeration head, 3-Sealed humidification tank, 40-Second pipeline, 41-Anode sub-pipeline, 42-Cathode sub-pipeline, 5-Cathode plate, 6-Cathode electrode, 61-Cathode current collector, 62-Cathode diffusion layer, 63-Cathode catalytic layer, 7-Ion exchange membrane, 8-Anode electrode, 81-Anode current collector, 82-Anode diffusion layer, 83-Anode catalytic layer, 9-Anode plate, 10-Porous transport layer, 10a-Medium side, 10b-Reaction side. Detailed Implementation

[0025] To better understand the above technical solutions, a detailed description of the solutions will be provided below in conjunction with the accompanying drawings and specific embodiments. Obviously, the described embodiments are merely some, not all, of the embodiments of the present invention. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are within the scope of protection of the present invention.

[0026] The terminology used in the embodiments of this invention is for the purpose of describing particular embodiments only and is not intended to limit the invention. The singular forms “a,” “the,” and “the” as used in the embodiments of this invention and the appended claims are also intended to include the plural forms, and “multiple” generally includes at least two unless the context clearly indicates otherwise.

[0027] It should also be noted that the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that an article or device that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such an article or device. Without further limitation, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the article or device that includes said element.

[0028] like Figure 1 As shown, the present invention provides an ozone preparation device based on condensate electrolysis, characterized in that it specifically includes: an air pump 1, a sealed humidification tank 3, an electrolytic cell and a power supply; Air pump 1 is used to prepare carrier gas and introduce it into a sealed humidification tank; wherein the carrier gas is at least one of air, oxygen, and nitrogen. The sealed humidification tank 3 is used to prepare high humidity gas and introduce the high humidity gas into the electrolytic cell; An electrolytic cell is used to condense the high-humidity gas passing through the anode plate 9 to form condensate, which enters the membrane electrode assembly. A DC voltage of 3-5 V is applied by a power supply, and the condensate undergoes an electrochemical oxidation reaction in the anode catalyst layer 83 to produce ozone.

[0029] High humidity gas has a relative humidity of ≥99%, where relative humidity is the ratio of the actual partial pressure of water vapor in moist air to the saturated partial pressure of water vapor under the same temperature and total pressure.

[0030] When a DC voltage of 3-5 V is applied to the electrolytic cell, an electrochemical oxidation reaction occurs at the anode under the influence of an electric field to generate ozone (3 H₂O → O₃ + 6H₂O). + + 6e - The cathode undergoes a reduction reaction to produce hydrogen gas (6H₂O). + + 6e -→ 3 H2).

[0031] like Figure 1 , Figure 2 As shown, the electrolytic cell includes a cathode plate 5, a membrane electrode assembly, and an anode plate 9. The membrane electrode assembly includes a cathode electrode 6, an ion exchange membrane 7, and an anode electrode 8. The cathode electrode 6 includes a cathode current collector 61, a cathode diffusion layer 62, and a cathode catalyst layer 63. The anode electrode 8 includes an anode current collector 81, an anode diffusion layer 82, and an anode catalyst layer 83.

[0032] Generally speaking, the cathode catalytic layer 63, ion exchange membrane 7, and anode catalytic layer 83 in a membrane electrode assembly can be referred to as membrane electrodes.

[0033] The membrane electrode assembly (MEA) constructs a complete pathway for efficient and stable electron conduction, reactant distribution, and product effluent. The current collector, acting as a conductive framework for electron convergence, collects or supplies current to the catalyst layer with extremely low resistance, ensuring a uniform potential distribution across the entire reaction interface. The diffusion layer, serving as a buffer and regulating layer between the current collector and the catalyst layer, utilizes its porous structure to uniformly distribute water or reactants to the catalyst layer while simultaneously facilitating the rapid escape of generated ozone gas, preventing bubble accumulation and blockage of active sites. Working in tandem, both layers ensure efficient and stable operation of the reaction at high current densities and play a crucial role in protecting the delicate catalyst layer and membrane, mitigating mechanical stress, and reducing corrosion.

[0034] High-humidity gas condenses at point 9 on the anode plate. The resulting condensate enters the interior of the membrane electrode assembly. When a DC voltage is applied, an anodic reaction occurs in the anode catalyst layer, generating ozone.

[0035] The ozone preparation device based on condensate electrolysis provided by this invention achieves in-situ distillation through evaporation and condensation processes, providing a relatively pure and uniform condensate film for the membrane electrode assembly, breaking through the water purity limitation, and providing a continuous water source for the electrolysis reaction in the membrane electrode assembly.

[0036] The ozone preparation device also includes a first pipeline 20 and a second pipeline 40. The front end of the first pipeline 20 is connected to the air pump 1, and the end of the first pipeline 20 extends into the water-containing liquid in the sealed humidification tank 3. A microporous aeration head 21 is provided at the end of the first pipeline 20. The average pore size of the microporous aeration head 21 is 3-10 µm. The carrier gas is introduced into the sealed humidification tank 3 through the first pipeline 20 and dispersed into the water-containing liquid in the form of bubbles under the action of the microporous aeration head 21, so that the carrier gas and the water-containing liquid are fully mixed, continuously increasing the humidity of the carrier gas until a preset saturation state is reached, forming a high-humidity gas.

[0037] The front end of the second pipe 40 extends into the sealed humidification tank 3 and is located above the water-containing liquid in the sealed humidification tank 3. The end of the second pipe 40 is connected to both the anode sub-pipe 41 and the cathode sub-pipe 42. The anode sub-pipe 41 is connected to the anode plate 9, and the cathode sub-pipe 42 is connected to the cathode plate 5. The insulation temperature of the second pipe 40 is not less than the temperature of the water-containing liquid in the sealed humidification tank.

[0038] The ozone generation device can meet the condensation and electrolysis of high-humidity gases within a flow rate range of 0.5~20 L / min, greatly expanding the application scenarios of ozone generation devices and achieving a dynamic balance between condensation water supply and electrolysis water consumption under different requirements. Specifically, for low flow rate requirements (e.g., 0.5~2 L / min), residence time is the primary factor, resulting in high condensation efficiency, suitable for scenarios prioritizing energy efficiency; for medium flow rate requirements (e.g., 2~10 L / min), an ideal balance between enhanced mass transfer and residence time can be achieved, with efficient synergistic condensation and electrolysis, suitable for scenarios where ozone yield and energy efficiency are matched; for high flow rate requirements (e.g., 10~20 L / min), inertial force is the primary factor, mass transfer reaches its limit, and bubbles are rapidly removed, suitable for scenarios with extremely high current density operation and short-term peak gas production requirements.

[0039] like Figure 1 , Figure 3 As shown, the inner surface of the anode plate 9 is provided with a flow channel structure. The flow channel structure consists of multiple segments with a wave-like distribution. The width of each segment is 0.8-1.5 mm, and the depth is 0.6-0.8 mm. It should be noted that the inner surface of the anode plate refers to the side of the anode plate closest to the membrane electrode assembly, while the outer surface of the anode plate refers to the side of the anode plate furthest from the membrane electrode assembly.

[0040] The flow channel structure provides a condensation space for high-humidity gas. The high-humidity gas condenses and gathers within the flow channel structure before entering the membrane electrode assembly.

[0041] like Figure 3 As shown, the flow channel structure includes a first straight groove group 11, a second straight groove group 12, a third straight groove group 13, and multiple curved groove sections 14. The first straight groove group 11, the second straight groove group 12, and the third straight groove group 13 are arranged sequentially along the flow direction of the flow channel (i.e., from the inlet to the outlet of the flow channel structure), and each of the first straight groove group 11, the second straight groove group 12, and the third straight groove group 13 includes at least one straight groove section 100. Each curved groove section 14 is connected to an adjacent straight groove section 100 at both ends. It should be noted that the starting end of the flow direction of the flow channel is the inlet of the high-humidity gas, that is, the inlet of the high-humidity gas is connected to the first straight groove group 11, and the outlet of the high-humidity gas is connected to the third straight groove group 13.

[0042] The arrangement of multiple straight and curved slots greatly expands the condensation space for high-humidity gases, allowing for thorough condensation and guiding the condensed microdroplets into the membrane electrode assembly for electrolysis, providing a stable electrolyte supply. To further enhance condensation and transport efficiency and increase ozone production rate, the first straight slot group 11 is equipped with first fins 111 parallel to the flow direction, and the second straight slot group 12 is equipped with second fins 121 perpendicular to the flow direction, staggered along the flow direction.

[0043] Different types of fins are set on multiple straight grooves in the flow channel structure to precisely match different areas of the flow channel direction, thereby improving the condensation of high-humidity gas and its penetration into the membrane electrode assembly.

[0044] Specifically, such as Figure 3 As shown, the first straight channel group 11 includes two straight channel sections. Multiple first fins 111 are arranged within each straight channel section of the first straight channel group 11, and each first fin 111 is parallel to the flow direction of the channel. The first straight channel group 11 needs to consider the smooth introduction of high-humidity gas and establish a stable laminar flow. The first fins 111, parallel to the flow direction of the channel, do not affect the flow rate of the high-humidity gas, but instead increase the contact area between the high-humidity gas and the inner surface of the first straight channel group 11. The laminar flow phenomenon within the first straight channel group 11 allows the condensed microdroplets to adhere to the inner surface of the first straight channel group 11, spreading evenly to form a liquid film, thus providing a stable and continuous electrolyte supply for electrolysis.

[0045] The second straight groove group 12 includes four straight groove sections. Each straight groove section of the second straight groove group 12 is provided with multiple second fins 121. Each second fin 121 is perpendicular to the flow direction of the channel, and adjacent second fins 121 are staggered along the flow direction of the channel. The second straight groove group 12 is located in the middle of the channel structure. The condensation of high humidity gas in the second straight groove group 12 and its penetration into the membrane electrode assembly are more easily affected by the high humidity gas flowing through and the gas generated by the electrolysis of the membrane electrode assembly. By arranging multiple second fins 121 staggered along the flow direction of the channel and perpendicular to the flow direction of the channel in the second straight groove group 12, strong turbulence and secondary flow can be generated by maximizing disturbance, thereby destroying the bubbles trapped in the second straight groove group 12 and eliminating the obstruction of bubbles to the penetration of condensate droplets into the membrane electrode assembly.

[0046] Meanwhile, the two fin dimensions are designed differently. The height of each first fin 111 is 10%~20% of the channel depth, and the height of each second fin is 30%~50% of the channel depth. The height of the first fin 111, which is 10%-20% of the corrugated channel depth, can increase the heat transfer area while minimizing the initial pressure drop, meeting the requirements of low resistance and high stability at the inlet. The height of the second fin 121, which is increased to 30%-50% of the corrugated channel depth, can significantly increase the turbulence intensity and heat / mass transfer area, effectively eliminating the severe condensate droplet mass transfer limitation and bubble (i.e., high humidity gas and electrolysis reaction gas flowing through this area) management challenges in the second straight channel group 12 area.

[0047] The fluid velocity (i.e., high-humidity gas or condensed droplets) within each bend section 14 varies greatly, resulting in strong secondary flow and sufficient heat exchange, eliminating the need for additional fins or other structural features. If fins were also installed in each bend section 14, it would drastically increase pressure drop and flow resistance, potentially leading to condensate splashing or stagnation, thus reducing cooling and ozone generation efficiency.

[0048] In addition to setting fins in each straight slot group, the number of straight slot sections within multiple straight slot groups was also set. Specifically, the ratio of the number of straight slot sections 100 in the first straight slot group 11, the second straight slot group 12, and the third straight slot group 13 is (1~2):(4~8):(1~2); for example... Figure 3 As shown, the number of straight groove sections 100 in the first straight groove group 11, the second straight groove group 12, and the third straight groove group 13 are 2, 4, and 1, respectively.

[0049] The second straight-line tank group 12 is the area where high-humidity gas is fully condensed and droplets penetrate, featuring the most straight-line tank sections 100, providing ample water for water electrolysis within the membrane electrode assembly. The first straight-line tank group 11 and the third straight-line tank group 13 are respectively for the full condensation and discharge of gas generated by hydrolysis, leaving necessary space. This ratio ensures that the reaction after condensation of high-humidity gas is complete, resulting in a compact system structure and balanced efficiency.

[0050] In addition, to improve the guiding effect of the third straight channel group 13, multiple third fins can be arranged within the third straight channel group 13. Each third fin is inclined along the flow direction of the channel, with an angle of inclination of 30° to 45°, and the spacing between adjacent third fins gradually increases along the flow direction. The inclined arrangement of each third fin can utilize the lateral force generated by the inclination angle to guide the gas generated by electrolysis to exit. The inclination angle of the third fins can achieve an optimized balance between separation efficiency and flow resistance, effectively guiding phase separation so that the separated liquid phase can repeatedly participate in gas preparation, while also avoiding excessive additional pressure drop.

[0051] The spacing between the third fins gradually increases along the flow path, resulting in a gradual decrease in the number of third fins downstream compared to upstream, achieving a functional gradient transition. The densely packed third fins upstream actively and efficiently complete the primary separation and bubble coalescence of the gas-liquid mixture. As the flow progresses and the separation is gradually completed, the sparser third fins significantly reduce local resistance at the end of the flow path, providing a smooth and unobstructed outlet channel for the separated gas phase while recovering the remaining small amount of liquid phase. This allows for a significant optimization of the overall system pressure drop with minimal loss in separation efficiency, improving operational energy efficiency.

[0052] Furthermore, the corrugated flow channel is provided with both hydrophilic and hydrophobic coatings. Specifically, the first straight channel group 11 and the second straight channel group 12 are both provided with hydrophilic coatings, while the third straight channel group 13 is provided with a hydrophobic coating. This invention does not limit the hydrophilic and hydrophobic coatings, but the hydrophilic coating only needs to possess hydrophilicity, good adhesion, and resistance to electrolyte corrosion. The hydrophobic coating only needs to possess hydrophobicity, good adhesion, and resistance to electrolyte corrosion. The hydrophilic coating in the first straight channel group 11 allows the condensed microdroplets to rapidly spread into a uniform thin liquid film, significantly improving condensation heat transfer efficiency. Simultaneously, in conjunction with the flow guidance of each first fin, it enables directional transport of the liquid film to the membrane electrode assembly. The hydrophilic coating in the second straight channel group 12 ensures that the surface of the membrane electrode assembly is always stably covered by the liquid film, guaranteeing continuous electrolysis. Simultaneously, in conjunction with the strong disturbance effect of each second fin, it enhances mass transfer and helps eliminate bubbles. A hydrophobic coating is provided in the third straight channel group 13, which can cause residual liquid (i.e., droplets containing impurities) to gather into beads and be discharged quickly under the action of gravity and / or flowing gas.

[0053] Correspondingly, the inner surface of the cathode plate 5 also has the same flow channel structure as the anode plate 9. High-humidity gas condenses simultaneously on both the anode plate 9 and the cathode plate 5, simultaneously wetting both sides of the membrane electrode assembly and improving the water supply rate. In practical applications, the spacing between adjacent straight groove sections 100 in the flow channel structure can vary. For example, the spacing between adjacent straight groove sections 100 along the flow direction gradually decreases / increases. Alternatively, the spacing between adjacent straight groove sections 100 at the beginning / end position can be set to be greater than the spacing between other adjacent straight groove sections 100. Preferably, the spacing between adjacent straight groove sections 100 at the beginning position of the flow channel is greater than the spacing between other adjacent straight groove sections 100, thereby increasing the residence time of the high-humidity gas, allowing it to fully contact the cold wall surface and increasing the condensation effect.

[0054] The membrane electrode assembly also includes a porous transport layer 10, which is attached to the outer surface of the anode electrode 8. It should be noted that the outer surface of the anode electrode refers to the surface of the anode electrode closest to the anode plate. Because the porous transport layer 10 is attached to the outer surface of the anode electrode 8, droplets formed by condensation in the flow channel structure will pass through the porous transport layer 10 and then enter the anode electrode 8.

[0055] Specifically, the porous transport layer 10 has a gradient pore structure with 3-5 steps along the thickness direction, and the inner wall of the pores of the porous transport layer is attached with a hydrophilic ionomer membrane, which is at least one of perfluorosulfonic acid resin, sulfonated polyether ether ketone, and sulfonated polyimide. The average pore size and porosity of the porous transport layer decrease gradually along the thickness direction, while the hydrophilic ionomer membrane loading of the porous transport layer increases gradually along the thickness direction, which is the direction perpendicular to the anode plate and pointing to the anode electrode. Among them, the average pore size of each step in the porous transport layer is reduced from 10-100 μm to 0.1-10 μm, the porosity is reduced from not less than 70% to 40%-60%, and the hydrophilic ionomer membrane loading is increased from 3-5 wt% to 12-15 wt%.

[0056] Specifically, such as Figure 4 As shown, in the porous transport layer 10, the step near the anode plate is 10a. Step 10a has a large pore size and high porosity, with an average pore size of 10-100 μm and a porosity of not less than 70%. From step 10a along the thickness direction, the average pore size and porosity of each step gradually decrease, until the step near the anode electrode is 10b. Step 10b has an average pore size of 0.1-10 μm and a porosity between 40% and 60%. It should be noted that although the ranges of average pore size and porosity for steps 10a, 10b, and the gas step overlap, in each specific embodiment, the average pore size and porosity of each step gradually decrease along the thickness direction. That is, the average pore size and porosity of step 10a are greater than those of the intermediate steps, and the average pore size and porosity of the intermediate steps are also greater than those of step 10b.

[0057] The large pore size and high porosity of the stepped 10a structure provide a low-resistance diffusion channel for high-humidity gases, enabling them to quickly and deeply penetrate into the electrode interior. This expands the effective condensation surface area and avoids the limitation of condensation occurring only on the surface. As the thickness extends, the average pore size and porosity gradually decrease, forming a microporous stepped structure with small pore size and high tortuosity. Vapor in the smaller pores is more likely to undergo capillary condensation at lower supersaturation, reducing the energy barrier required for phase change and improving condensation efficiency.

[0058] Meanwhile, to enhance the transport and penetration of condensate droplets into the membrane electrode assembly, the porous transport layer 10 underwent gradient hydrophilic modification. Specifically, the entire three-dimensional framework of the porous transport layer 10 was coated with a hydrophilic ionomer to form a hydrophilic ionomer film. This treatment can be performed by impregnation, spraying, or chemical grafting, and no specific limitation is made here. Perfluorosulfonic acid resin (such as Nafion), sulfonated polyether ether ketone (SPEEK), or other proton-conducting ionomers are uniformly attached to the inner wall of the pores in the form of a thin film, forming a functionalized hydrophilic layer. The hydrophilic ionomer film can expand the effective wetting area and improve the initial condensation rate and heat and mass transfer efficiency. At the same time, the hydrophilic ionomer itself is a proton conductor, which can provide an additional proton transport path for condensate during transport, which is beneficial to reducing the ion transport resistance of the electrolyte.

[0059] The hydrophilic ionomer film loading of the porous transport layer 10 increases gradually along the thickness direction, from 3-5 wt% to 12-15 wt%. The hydrophilic ionomer film loading is the ratio of the mass of the hydrophilic ionomer film in the stepped porous transport layer to the total mass of the stepped porous transport layer.

[0060] The hydrophilic ionomer film loading of step 10a is relatively low, preferably 3-5 wt%. As the thickness increases, the hydrophilic ionomer film loading of each step gradually increases, reaching 12-15 wt% at step 10b. Step 10b, closer to the anode electrode 8, has a high hydrophilic ionomer content, which significantly enhances the water collection capacity and proton conduction network density of the porous transport layer. This directional property change directly optimizes the three-phase interface in the core reaction region, reduces droplet transport resistance, and thus effectively improves the electrolysis reaction efficiency and the local stability of the electrolyzer structure.

[0061] In addition, the porous transport layer 10 with gradient pore size and gradient hydrophilic ionomer loading is designed to construct a property gradient structure that allows high-humidity gas to permeate into the catalytic active site, thereby achieving synergistic optimization management of water, protons, and gaseous products. This ensures efficient water supply and uniform distribution, strengthens the proton conduction network, and promotes rapid desorption of ozone bubbles generated by electrolysis. This maximizes the three-phase reaction interface, improves the current efficiency and yield of ozone generation, and effectively alleviates the impact of insufficient condensate supply on the lifespan of the membrane electrode assembly. Ultimately, this achieves the goal of improving the overall performance and operational stability of the electrolyzer.

[0062] In addition, a flexible sealing gasket is provided around the outer periphery of the membrane electrode assembly. This flexible sealing gasket can be enclosed with the anode plate 9 and the cathode plate 5 to form an area that accommodates the entire membrane electrode assembly, thereby achieving ozone preparation in a sealed state. At the same time, the flexible sealing gasket can also play a buffering role to avoid excessive compression when the anode plate 9 and the cathode plate 5 are fixed, which could damage the membrane electrode assembly.

[0063] Furthermore, the anode plate 9 also integrates a heat dissipation fin assembly, which is attached to the outer surface of the anode plate 9. The heat dissipation fin assembly is in the form of a fin array, with a spacing of 2-4 mm between adjacent heat dissipation fins, and the length and width of the heat dissipation fins are both 55-65 mm.

[0064] The heat dissipation fins are surrounded by heat dissipation devices (such as fans) for forced convection cooling. The heat dissipation fins can efficiently conduct and dissipate the Joule heat and reaction heat generated by the electrolysis reaction in the electrolytic cell.

[0065] like Figure 5 As shown, this invention provides a method for preparing ozone based on the electrolysis of condensate, specifically including the following steps: Step S1: Prepare carrier gas and introduce it into the sealed humidification tank 3 to prepare high humidity gas; Step S2: Introduce the high-humidity gas into the electrolytic cell; Step S3: High humidity gas is condensed by the anode plate 9 to form condensate, which enters the membrane electrode assembly; Step S4: Apply a DC voltage of 3-5V to the electrolytic cell. The condensed water undergoes an electrochemical oxidation reaction in the anode catalyst layer to produce ozone.

[0066] Furthermore, step S1 specifically includes the following steps: Carrier gas is prepared using air pump 1, wherein the flow rate of the carrier gas is 0.5-20 L / min; The carrier gas is introduced into the water-containing liquid in the sealed humidification tank 3 through the first pipeline 20. The liquid level of the water-containing liquid in the sealed humidification tank 3 is 1 / 2 to 3 / 4 of the tank height, and the temperature of the water-containing liquid is 40-60 ℃. The carrier gas in the sealed humidification tank 3 reaches the preset saturation state, thus preparing a high humidity gas.

[0067] Furthermore, in step S1, the carrier gas is at least one of air, oxygen, and nitrogen; A microporous aeration head 21 is provided at the end of the first pipeline 20, and the average pore size of the microporous aeration head 21 is 3-10 µm. The carrier gas is introduced into the water-containing liquid in the sealed humidification tank 3 through the first pipeline 20, specifically including: The carrier gas enters the microporous aeration head 21 through the first pipeline 20 and disperses into the water-containing liquid in the form of bubbles.

[0068] Furthermore, step S2 specifically includes the following steps: High-humidity gas is introduced into the electrolytic cell through the second pipe 40. The front end of the second pipe 40 extends into the sealed humidification tank 3 and is located above the water-containing liquid in the sealed humidification tank 3. The end of the second pipe 40 is connected to the anode sub-pipe 41 and the cathode sub-pipe 42. The anode sub-pipe 41 is connected to the anode plate 9, and the cathode sub-pipe 42 is connected to the cathode plate 5. The insulation temperature of the second pipe 40 is not less than the temperature of the water-containing liquid in the sealed humidification tank 3.

[0069] Furthermore, in step S3, the anode plate 9 is made of titanium alloy, the surface temperature of the anode plate 9 is 20-30℃, and the membrane electrode assembly also includes a porous transport layer 10, which is attached to the outer surface of the anode electrode 8. Step S3 specifically includes the following steps: The high-humidity gas passing through the anode sub-pipe 41 comes into contact with the flow channel structure set on the inner surface of the anode plate 9, forming micro-droplets; Microdroplets converge and permeate into the membrane electrode assembly through the porous transport layer 10.

[0070] Furthermore, step S4 specifically includes the following steps: DC voltage 3-5 V, current density 0.5-2 A / cm² 2 The electrolyte temperature is 20-30 ℃.

[0071] Furthermore, in step S4, the catalyst loading in the anode catalyst layer is 40-60 mg / cm³. 2 The catalyst type is tin oxide-based catalyst.

[0072] Example 1: This embodiment provides an ozone preparation device based on condensate electrolysis, including: an oil-free diaphragm pump, a first pipeline 20, a microporous aeration head 21, a sealed humidification tank 3, a second pipeline 40, an anode sub-pipeline 41, a cathode sub-pipeline 42, a cathode plate 5, a cathode electrode 6, an ion exchange membrane 7, an anode electrode 8, and an anode plate 9.

[0073] The first pipeline 20 is connected to an oil-free diaphragm pump at its front end, and extends into the aqueous liquid in the sealed humidification tank 3 at its rear end. Carrier gas is introduced into the sealed humidification tank 3 through the first pipeline 20. A microporous aeration head 21, made of titanium, is installed at the rear end of the first pipeline 20, with an average pore size of approximately 5 µm. The liquid level in the sealed humidification tank 3 is 2 / 3 of the tank's height. The first pipeline 20 is made of polytetrafluoroethylene (PTFE) and has an inner diameter of 6 mm. The sealed humidification tank 3 is a 3 L polycarbonate tank.

[0074] The front end of the second pipe 40 extends into the sealed humidification tank 3 and is located above the water-containing liquid in the sealed humidification tank 3. The end of the second pipe 40 is connected to the anode sub-pipe 41 and the cathode sub-pipe 42. The anode sub-pipe 41 is connected to the anode plate 9, and the cathode sub-pipe 42 is connected to the cathode plate 5.

[0075] The inner surface of the anode plate 9 is provided with a flow channel structure. The flow channel structure consists of multiple segments with a wave-like distribution. The width of each segment is about 1 mm and the depth is about 0.8 mm. The flow channel structure includes a first straight groove group 11, a second straight groove group 12, a third straight groove group 13, and multiple curved groove sections 14. The first straight groove group 11, the second straight groove group 12, and the third straight groove group 13 are arranged sequentially along the flow direction of the flow channel. The number of straight groove sections 100 in the first straight groove group 11, the second straight groove group 12, and the third straight groove group 13 are 2, 4, and 1, respectively. Each curved groove section 14 is connected to the adjacent straight groove section 100 at both ends.

[0076] In each straight groove section 100 of the first straight groove group 11, a plurality of first fins 111 are provided, each of which is parallel to the flow direction of the channel. In each straight groove section 100 of the second straight groove group 12, a plurality of second fins 121 are provided, each of which is perpendicular to the flow direction of the channel. Adjacent second fins 121 are staggered along the flow direction of the channel. The height of each first fin 111 is approximately 20% of the depth of the channel, and the height of each second fin 121 is approximately 50% of the depth of the channel.

[0077] The anode electrode in the membrane electrode assembly uses a titanium-based gas diffusion layer (250 μm thick) and an anode catalyst layer (50 mg / cm³ loading). 2 The ion exchange membrane is a perfluorosulfonic acid ion exchange membrane (125 μm thick), and the cathode electrode consists of a cathode catalyst layer (loaded with 0.4 mg / cm² Pt / C catalyst) and a carbon-based gas diffusion layer (250 μm thick).

[0078] The membrane electrode assembly is pressed together on both sides by an anode plate 5 and a cathode plate 9, respectively.

[0079] The membrane electrode assembly includes a porous transport layer 10, which is attached to the outer surface of the anode electrode 8. The porous transport layer 10 has a gradient pore structure with three steps along the thickness direction, and the inner walls of the pores of the porous transport layer are coated with a perfluorosulfonic acid resin membrane. In the porous transport layer 10, the average pore size of step 10a is about 50 μm, the average pore size of the intermediate step is about 10 μm, and the average pore size of step 10b is about 5 μm.

[0080] In the porous transport layer 10, the porosity of the step 10a is about 80%, the porosity of the intermediate step is about 70%, and the porosity of the step 10b is about 50%.

[0081] The perfluorosulfonic acid resin membrane loading of the porous transport layer 10 in the middle step 10a is about 3%, the perfluorosulfonic acid resin membrane loading of the intermediate step is about 10%, and the perfluorosulfonic acid resin membrane loading of the step 10b is about 15%.

[0082] This embodiment also provides an ozone preparation method using an ozone preparation device based on condensate electrolysis, which specifically includes the following steps: Step S1: Air is blown out using an oil-free diaphragm pump to form a carrier gas with a flow rate of approximately 10 L / min. The carrier gas is then dispersed into the tap water in the sealed humidification tank 3 via the first pipeline 20 and the microporous aeration head 21 in a bubbling manner. The tap water is kept at a temperature of 50 ℃, and the humidity of the carrier gas in the sealed humidification tank 3 reaches 100%, thus preparing a high-humidity gas. The total dissolved solids (TDS) content of the tap water in the sealed humidification tank 3 is approximately 200 ppm. Step S2: Set a switch in the second pipeline 40. After the high humidity gas is prepared, the high humidity gas is introduced into the anode plate 9 and the cathode plate 5 through the second pipeline 40, and then through the anode sub-pipeline 41 and the cathode sub-pipeline 42 respectively. The heat preservation temperature of the second pipeline 40 is also 50 ℃. Step S3: The high-humidity gas comes into contact with the flow channel structure located on the inner surface of the anode plate 9 and has a surface temperature of 20 °C, forming microdroplets. The microdroplets converge and permeate into the membrane electrode assembly through the porous transport layer 10. Step S4: Apply a 5V DC voltage to the electrolytic cell, with a current density of 1 A / cm². 2 The electrolyte temperature is 20 °C. The condensate undergoes an electrochemical oxidation reaction on the anode catalyst layer to generate ozone gas. The ozone concentration is stable at around 500 ppm (based on the outlet gas). The condensate undergoes an electrochemical reduction reaction on the cathode catalyst layer to generate hydrogen gas.

[0083] Example 2: This embodiment uses the same ozone preparation apparatus as in Embodiment 1. The ozone preparation method in this embodiment is adjusted in step S1 compared to the ozone preparation method in Embodiment 1.

[0084] Step S1 of this embodiment: Air is blown out using an oil-free diaphragm pump to form a carrier gas with a flow rate of approximately 10 L / min. The carrier gas is then dispersed through the first pipeline 20 and the microporous aeration head 21 in the form of bubbles into the seawater (which has undergone preliminary sedimentation and filtration) in the sealed humidification tank 3. The seawater is kept at a temperature of 50 °C, and the humidity of the carrier gas in the sealed humidification tank 3 reaches 100%, thus preparing a high-humidity gas.

[0085] In this embodiment, ozone-containing gas is produced, and the ozone concentration is stabilized at around 500 ppm (based on the outlet gas).

[0086] Example 3: This embodiment uses the same ozone preparation apparatus as in Embodiment 1. The ozone preparation method in this embodiment is adjusted in step S1 compared to the ozone preparation method in Embodiment 1.

[0087] Step S1 of this embodiment: Step S1: Air is blown out using an oil-free diaphragm pump to form a carrier gas with a flow rate of approximately 15 L / min. The carrier gas is then dispersed into the tap water in the sealed humidification tank 3 via the first pipeline 20 and the microporous aeration head 21 in a bubbling manner. The tap water is kept at a temperature of 50 ℃, and the humidity of the carrier gas in the sealed humidification tank 3 reaches 100%, thus preparing a high-humidity gas. The total dissolved solids (TDS) content of the tap water in the sealed humidification tank 3 is approximately 200 ppm.

[0088] In this embodiment, ozone-containing gas is generated, and the ozone concentration is stabilized at around 800 ppm (based on the outlet gas).

[0089] This invention presents a method and apparatus for ozone preparation based on condensate electrolysis. The water source directly utilizes non-pure water (TDS ≥ 500 ppm), such as tap water, groundwater, or even compliant wastewater. By increasing the carrier gas and employing a unique condensation mechanism, a breakthrough is achieved in the electrochemical ozone preparation of non-pure water within a membrane electrode system, preventing most dissolved impurities in the water from being carried into the core electrolysis reaction zone. The evaporation-condensation process is equivalent to an in-situ distillation, providing a relatively pure condensate film to the electrode surface. This fundamentally overcomes the limitation of water purity, extending the lifespan of the non-pure water membrane electrode by 2-3 orders of magnitude.

[0090] When high-humidity gas at a temperature of 50-60 ℃ enters the electrolytic cell channel, water vapor comes into contact with the lower-temperature electrode plates, causing some of the water vapor to condense on the channel wall, gas diffusion layer, and membrane electrode surface, forming a uniform thin liquid film, thereby continuously providing water for the electrolysis reaction.

[0091] Although preferred embodiments of the invention have been described, those skilled in the art, upon learning the basic inventive concept, can make other changes and modifications to these embodiments. Therefore, the appended claims are intended to be interpreted as including both the preferred embodiments and all changes and modifications falling within the scope of the invention. Clearly, those skilled in the art can make various alterations and modifications to the invention without departing from its spirit and scope. Thus, if these modifications and modifications of the invention fall within the scope of the claims and their equivalents, the invention is also intended to include these modifications and modifications.

Claims

1. An ozone preparation device based on condensate electrolysis, characterized in that, Specifically, it includes: Air pump, sealed humidification tank, electrolytic cell and power supply; An air pump is used to prepare carrier gas and introduce it into a sealed humidification tank. A sealed humidification tank is used to prepare high-humidity gas and introduce the high-humidity gas into an electrolytic cell. An electrolytic cell is used to condense high-humidity gas passing through the anode plate to form condensate, which enters the membrane electrode assembly. A DC voltage is applied by a power source, and the condensate undergoes an electrochemical oxidation reaction in the anode catalyst layer to produce ozone.

2. The ozone generation device based on condensate electrolysis as described in claim 1, characterized in that, It also includes a first pipeline and a second pipeline. The front end of the first pipeline is connected to an air pump, and the end of the first pipeline extends into the water-containing liquid in the sealed humidification tank. The carrier gas is introduced into the sealed humidification tank through the first pipeline. A microporous aeration head is installed at the end of the first pipeline. The average pore size of the microporous aeration head is 3-10 µm. The front end of the second pipeline extends into the sealed humidification tank and is located above the water-containing liquid in the sealed humidification tank. The end of the second pipeline is connected to the anode sub-pipeline and the cathode sub-pipeline. The anode sub-pipeline is connected to the anode plate, and the cathode sub-pipeline is connected to the cathode plate. The insulation temperature of the second pipeline is not less than the temperature of the water-containing liquid in the sealed humidification tank.

3. The ozone preparation device based on condensate electrolysis as described in claim 1, characterized in that, The inner surface of the anode plate is provided with a flow channel structure, which consists of multiple segments with a wave-like distribution. The width of each segment is 0.8-1.5 mm and the depth is 0.6-0.8 mm. The flow channel structure includes a first straight groove group, a second straight groove group, a third straight groove group, and multiple curved groove sections. The first straight groove group, the second straight groove group, and the third straight groove group are arranged sequentially along the flow direction of the flow channel, and each of the first straight groove group, the second straight groove group, and the third straight groove group includes at least one straight groove section. Each curved groove section is connected to the adjacent straight groove section at both ends. In each straight groove section of the first straight groove group, there are multiple first fins, each of which is parallel to the flow direction of the channel. In each straight groove section of the second straight groove group, there are multiple second fins, each of which is perpendicular to the flow direction of the channel, and adjacent second fins are staggered along the flow direction of the channel.

4. The ozone preparation device based on condensate electrolysis as described in claim 3, characterized in that, The ratio of the number of straight groove sections in the first straight groove group, the second straight groove group, and the third straight groove group is (1~2):(4~8):(1~2); The height of each first fin is 10% to 20% of the channel depth, and the height of each second fin is 30% to 50% of the channel depth.

5. The ozone preparation device based on condensate electrolysis as described in claim 1, characterized in that, The membrane electrode assembly also includes a porous transport layer, which is attached to the outer surface of the anode electrode.

6. The ozone preparation apparatus based on condensate electrolysis as described in claim 5, characterized in that, The porous transport layer has a gradient pore structure with 3-5 steps along the thickness direction, and the inner wall of the pores of the porous transport layer is attached with a hydrophilic ionomer membrane, which is at least one of perfluorosulfonic acid resin, sulfonated polyether ether ketone, and sulfonated polyimide. The average pore size and porosity of the porous transport layer decrease gradually along the thickness direction, while the hydrophilic ionomer membrane loading of the porous transport layer increases gradually along the thickness direction, which is the direction perpendicular to the anode plate and pointing to the anode electrode. Among them, the average pore size of each step in the porous transport layer is reduced from 10-100 μm to 0.1-10 μm, the porosity is reduced from not less than 70% to 40%-60%, and the hydrophilic ionomer membrane loading is increased from 3-5 wt% to 12-15 wt%.

7. A method for preparing ozone based on condensate electrolysis, characterized in that, The ozone generation apparatus based on condensate electrolysis as described in any one of claims 1-6 specifically includes the following steps: Step S1: Prepare carrier gas and introduce it into a sealed humidification tank to prepare high humidity gas; Step S2: Introduce the high-humidity gas into the electrolytic cell; Step S3: High humidity gas is condensed by the anode plate to form condensate, which then enters the membrane electrode assembly; Step S4: Apply DC voltage to the electrolytic cell, and the condensate undergoes an electrochemical oxidation reaction in the anode catalyst layer to produce ozone.

8. The ozone preparation method based on condensate electrolysis as described in claim 7, characterized in that, Step S1 specifically includes: The flow rate of the carrier gas is 0.5-20 L / min, the liquid level of the water-containing liquid in the sealed humidification tank is 1 / 2-3 / 4 of the tank height, and the temperature of the water-containing liquid is 40-60 ℃.

9. The ozone preparation method based on condensate electrolysis as described in claim 7, characterized in that, Step S2 specifically includes: the gas flow rate of the high-humidity gas in the second pipeline is 0.5-20 L / min; In step S3, the anode plate is made of titanium alloy, and the surface temperature of the anode plate is 20-30℃.

10. The ozone preparation method based on condensate electrolysis as described in claim 7, characterized in that, Step S4 specifically includes the following steps: DC voltage 3-5 V, current density 0.5-2 A / cm² 2 The electrolyte temperature is 20-30 ℃; The catalyst loading in the anode catalyst layer is 40-60 mg / cm³. 2 The catalyst type is tin oxide-based catalyst.

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