Anode plate for preparing glycolate by electrocatalytic oxidation of glycol and application thereof

Abstract

The application belongs to the field of electrolytic cell polar plate flow channel structure design, and specifically comprises an anode polar plate for preparing glycolate by electrocatalytic oxidation of ethylene glycol and an application thereof. 2 The above results are obtained based on simulation, so that the optimal anode polar plate configuration in the scaled-up reaction process can be determined preliminarily conveniently and quickly.

Description

Technical Field

[0001] This invention belongs to the field of electrolytic cell electrode channel structure design, specifically including an anode plate for the electrocatalytic oxidation of ethylene glycol to prepare glycolate and its application. Background Technology

[0002] Glycolic acid, as an important platform chemical, has been widely used in various industrial fields such as chemical cleaning, sterilization and disinfection, daily chemical products, biodegradable material synthesis, and electroplating surface treatment. However, the current mainstream industrial glycolic acid preparation processes (chloroacetic acid hydrolysis and formaldehyde cyanidation) all rely on highly toxic chemicals as starting materials, which not only poses serious safety and environmental risks but also results in high product synthesis costs, greatly limiting the large-scale application and industrial upgrading of glycolic acid.

[0003] Electrocatalytic oxidation technology offers a new approach for the green and efficient synthesis of glycolic acid. This technology can directionally convert ethylene glycol (or ethylene glycol, a derivative of waste PET plastic) into glycolates, avoiding the use of highly toxic raw materials at the source, which aligns with the development trend of green chemistry. The industrialization of this technology requires the synergistic support of three core technologies: catalyst materials, electrolysis equipment, and purification processes. Currently, various high-efficiency catalytic systems have been reported in the field of catalyst materials, enabling the efficient conversion of ethylene glycol to glycolates. In terms of purification processes, distillation and bipolar membrane electrodialysis technologies have also been validated through relevant research. However, significant gaps remain in the design and integration of the critical electrolytic cell equipment. As a core component of the electrolytic cell equipment, the flow channel structure design of the electrode plate directly affects the mass transfer efficiency, current distribution, and catalytic activity of the reaction system. It is also a key factor determining whether the electrocatalytic reaction can be scaled up from laboratory scale to industrial production. Breakthroughs in related technologies are of great significance for promoting the industrialization of the entire process. Summary of the Invention

[0004] In view of the problems existing in the prior art, the first objective of this invention is to provide an anode plate for the electrocatalytic oxidation of ethylene glycol to prepare glycolate. In this invention, fluid dynamics simulation software was used to simulate the flow fields of six different anode plates. Finally, the influence of the flow channel structure and parameters on the reaction system was comprehensively evaluated, and the optimal anode plate configuration for large-scale reaction was selected.

[0005] A second objective of this invention is to provide an application of the anode plate described above in the preparation of an electrolysis apparatus.

[0006] A third object of the present invention is to provide an electrolysis apparatus comprising the anode plate as described above.

[0007] The fourth objective of this invention is to provide an electrocatalytic method for the electrocatalytic oxidation of ethylene glycol to prepare glycolate.

[0008] To achieve the first objective mentioned above, the technical solution adopted by the present invention includes: This invention discloses an anode plate for the electrocatalytic oxidation of ethylene glycol to prepare glycolate, wherein the anode plate has a flow channel for the flow of anolyte; The flow field of the anode plate is determined based on its area. The flow field of the anode plate includes one of the following: single serpentine flow field, multiple serpentine flow field, interdigitated flow field, grid flow field, point flow field, and straight-through flow field. When the area of ​​the anode plate is greater than or equal to the first area threshold, the flow field of the anode plate is a multi-serpentine flow field.

[0009] To meet the customized design requirements for dedicated anode plates during the large-scale scaling-up of this reaction system, the applicant used the COMSOL Multiphysics 6.4 fluid dynamics simulation software to study the influence of six anode plate flow field structures on the reaction system. First, simulations were used to select the flow channel parameter combinations for each anode plate structure that resulted in the smallest pressure drop and the largest reaction area, including channel spacing, channel width, and channel depth. Then, based on the simulation results, further studies were conducted on pressure drop, electric field potential (including electrolyte potential and electrode potential to ground), electrolyte flow rate distribution, and reactant concentration distribution (including OH-). - The system simulation study of the concentration of ethylene glycol and the product concentration distribution (including sodium glycolate concentration) comprehensively demonstrated the optimal anode plate configuration under the anode plate area size in the industrial conversion stage from multiple dimensions, providing guidance for further large-scale scaling.

[0010] Furthermore, the first area threshold is 0.1 m. 2 That is, the area of ​​the anode plate is greater than or equal to 0.1 m². 2 At that time, the flow field of the anode plate is a multi-serpentine flow field.

[0011] Furthermore, the channel spacing of the multi-serpentine flow field is 15-35mm, the channel width is 20-30mm, and the channel depth is 20-30mm.

[0012] Furthermore, the channel spacing of the multi-serpentine flow field is 15mm, the channel width is 25mm, and the channel depth is 30mm.

[0013] To achieve the second objective mentioned above, the technical solution adopted by the present invention includes: This invention discloses an application of the anode plate described above in the preparation of an electrolysis device.

[0014] To achieve the third objective mentioned above, the technical solution adopted by the present invention includes: This invention discloses an electrolytic device for the electrocatalytic oxidation of ethylene glycol to prepare glycolate, comprising an electrolytic cell, wherein the electrolytic cell includes a cathode plate, a cathode catalyst, a proton exchange membrane, an anode catalyst, and an anode plate as described above, arranged sequentially. A cathode chamber is formed between the cathode plate and the proton exchange membrane, and an anode chamber is formed between the anode plate and the proton exchange membrane. The anode chamber contains an anolyte, and the cathode chamber contains a cathode electrolyte.

[0015] Furthermore, the anolyte is an alkaline electrolyte containing ethylene glycol.

[0016] Furthermore, the cathode electrolyte is an alkaline electrolyte that does not contain ethylene glycol.

[0017] Furthermore, the flow field of the anode plate is a flow channel for the anolyte to flow through.

[0018] To achieve the fourth objective mentioned above, the technical solution adopted by the present invention includes: This invention discloses an electrocatalytic method for preparing glycolate by electrocatalytic oxidation of ethylene glycol, which uses the electrolysis device described above to perform the electrocatalytic oxidation of ethylene glycol to prepare glycolate; In this process, the cathode electrolyte enters the cathode chamber of the electrolytic cell, and the water in the cathode electrolyte is reduced to hydrogen gas at the cathode plate. The anolyte enters the anode chamber of the electrolytic cell and circulates and reacts in the electrolytic cell along the flow channels on the anode plate. The ethylene glycol in the anolyte is oxidized on the anode plate to form glycolate.

[0019] Furthermore, the flow rate of the cathode electrolyte in the flow channel is 0.3-10 L / min, the flow rate of the anode electrolyte in the flow channel is 0.3-10 L / min, and the applied cell voltage is between 1.0-1.5 V.

[0020] Beneficial effects of this invention: This invention utilizes fluid dynamics simulation software to simulate the flow field of the anode plate in the electrocatalytic oxidation of ethylene glycol to prepare glycolic acid during large-scale production. The simulation comprehensively considers factors such as pressure drop, velocity distribution, electric field potential, and reactant concentration (OH-). - Given the concentrations of ethylene glycol and product (sodium glycolate), it was ultimately determined that the anode plate area should be greater than or equal to 0.1 m². 2Under these circumstances, a multi-serpentine flow field is the optimal electrode configuration for the anode plate. At the same time, the flow channel parameters, including the channel spacing, channel width, and channel depth, were determined. This application fills the technological gap in the field of electrocatalytic oxidation of ethylene glycol to prepare glycolic acid, and eliminates the problem of linear scale-up correlation deviation that easily occurs in the process of large-scale scale-up of this reaction system without a dedicated custom design of the flow channel plate. It successfully overcomes the core obstacle in this large-scale scale-up process. Attached Figure Description

[0021] The specific embodiments of the present invention will be described in further detail below with reference to the accompanying drawings.

[0022] Figure 1 A schematic diagram of the electrolysis apparatus protected by the present invention is shown, wherein 1-proton exchange membrane, 2-anode catalyst, 3-cathode catalyst, 4-sealing gasket, 5-anode plate, 6-cathode plate, and 7-end pressure plate.

[0023] Figure 2 The simulation results show the pressure drop and reaction area statistics of a single serpentine flow field under different flow channel parameters.

[0024] Figure 3 The simulation results show the pressure drop and reaction area statistics of the multi-serpentine flow field under different flow channel parameters.

[0025] Figure 4 The simulation results show the pressure drop and reaction area statistics of the interdigitated flow field under different flow channel parameters.

[0026] Figure 5 The simulation results show the pressure drop and reaction area statistics of a straight-through flow field under different flow channel parameters.

[0027] Figure 6 The simulation results show the pressure drop and reaction area statistics of the grid-shaped flow field under different flow channel parameters.

[0028] Figure 7 The simulation results show the pressure drop and reaction area statistics of the point-shaped flow field under different flow channel parameters.

[0029] Figure 8 The pressure distribution in a single serpentine flow field is shown in the simulation.

[0030] Figure 9 The multi-faceted distribution of electrolyte velocity in a single serpentine flow field is shown in the simulation.

[0031] Figure 10 The cross-sectional distribution of electrolyte velocity in a single serpentine flow field is shown in the simulation.

[0032] Figure 11The electrolyte velocity streamlines are shown in the simulation of a single serpentine flow field.

[0033] Figure 12 The OH of a single serpentine flow field in the simulation is shown. - Surface concentration distribution.

[0034] Figure 13 The OH of a single serpentine flow field in the simulation is shown. - Concentration cross-section.

[0035] Figure 14 The OH of a single serpentine flow field in the simulation is shown. - Concentration multi-faceted.

[0036] Figure 15 The surface concentration distribution of ethylene glycol in a single serpentine flow field is shown in the simulation.

[0037] Figure 16 The ethylene glycol concentration cross-section is shown in the simulation of a single serpentine flow field.

[0038] Figure 17 The multi-section of ethylene glycol concentration in a single serpentine flow field is shown in the simulation.

[0039] Figure 18 The surface concentration distribution of sodium glycolate in a single serpentine flow field is shown in the simulation.

[0040] Figure 19 The sodium glycolate concentration cross-section is shown in the simulation of a single serpentine flow field.

[0041] Figure 20 The simulation shows multiple cross-sections of sodium glycolate concentration in a single serpentine flow field.

[0042] Figure 21 The electrolyte potential is shown in the simulation of a single serpentine flow field.

[0043] Figure 22 The ground potential of a single serpentine flow field in the simulation is shown.

[0044] Figure 23 The pressure distribution in the multi-serpentine flow field is shown in the simulation.

[0045] Figure 24 The simulation shows multiple cross-sections of electrolyte flow velocity in a multi-serpentine flow field.

[0046] Figure 25 The cross-section of electrolyte flow velocity in the multi-serpentine flow field is shown in the simulation.

[0047] Figure 26 The electrolyte velocity streamlines are shown in the simulation of a multi-serpentine flow field.

[0048] Figure 27The OH of the multi-serpentine flow field in the simulation is shown. - Surface concentration distribution.

[0049] Figure 28 The OH of the multi-serpentine flow field in the simulation is shown. - Concentration cross-section.

[0050] Figure 29 The OH of the multi-serpentine flow field in the simulation is shown. - Concentration multi-faceted.

[0051] Figure 30 The surface concentration distribution of ethylene glycol in a multi-serpentine flow field is shown in the simulation.

[0052] Figure 31 The ethylene glycol concentration cross-section is shown in the multi-serpentine flow field.

[0053] Figure 32 The simulation shows multiple cross-sections of ethylene glycol concentration in a multi-serpentine flow field.

[0054] Figure 33 The surface concentration distribution of sodium glycolate in a multi-serpentine flow field is shown in the simulation.

[0055] Figure 34 The sodium glycolate concentration cross-section is shown in the simulation of the multi-serpentine flow field.

[0056] Figure 35 The simulation shows multiple cross-sections of sodium glycolate concentration in a multi-serpentine flow field.

[0057] Figure 36 The electrolyte potential is shown in the simulation of a multi-serpentine flow field.

[0058] Figure 37 The ground potential is shown in the simulation of a multi-serpentine flow field.

[0059] Figure 38 The pressure distribution in the straight-through flow field is shown in the simulation.

[0060] Figure 39 The multi-faceted view of electrolyte velocity in the straight-through flow field is shown in the simulation.

[0061] Figure 40 The cross-section of electrolyte velocity in the straight-through flow field is shown in the simulation.

[0062] Figure 41 The electrolyte velocity streamlines are shown in the simulation of a straight-through flow field.

[0063] Figure 42 The OH values ​​of the straight-through flow field in the simulation are shown. - Surface concentration distribution.

[0064] Figure 43 The OH values ​​of the straight-through flow field in the simulation are shown. - Concentration cross-section.

[0065] Figure 44 The OH values ​​of the straight-through flow field in the simulation are shown. - Concentration multi-faceted.

[0066] Figure 45 The surface concentration distribution of ethylene glycol in a straight-through flow field is shown in the simulation.

[0067] Figure 46 The ethylene glycol concentration cross section is shown in the simulation of the straight-through flow field.

[0068] Figure 47 The simulation shows multiple cross-sections of ethylene glycol concentration in a straight-through flow field.

[0069] Figure 48 The surface concentration distribution of sodium glycolate in a straight-through flow field is shown in the simulation.

[0070] Figure 49 The sodium glycolate concentration cross-section is shown in the simulation of the straight-through flow field.

[0071] Figure 50 The simulation shows multiple cross-sections of sodium glycolate concentration in a straight-through flow field.

[0072] Figure 51 The electrolyte potential is shown in the simulation of a straight-through flow field.

[0073] Figure 52 The potential relative to ground of the straight-through flow field in the simulation is shown.

[0074] Figure 53 The pressure distribution in the grid-shaped flow field is shown in the simulation.

[0075] Figure 54 The multi-section of electrolyte flow velocity in the grid-shaped flow field is shown in the simulation.

[0076] Figure 55 The cross-section of electrolyte velocity in the grid-shaped flow field is shown in the simulation.

[0077] Figure 56 The electrolyte velocity streamlines in the grid-shaped flow field are shown in the simulation.

[0078] Figure 57 The OH values ​​of the grid-shaped flow field in the simulation are shown. - Surface concentration distribution.

[0079] Figure 58 The OH values ​​of the grid-shaped flow field in the simulation are shown. - Concentration cross-section.

[0080] Figure 59 The OH values ​​of the grid-shaped flow field in the simulation are shown. - Concentration multi-faceted.

[0081] Figure 60 The surface concentration distribution of ethylene glycol in the grid-shaped flow field is shown in the simulation.

[0082] Figure 61 The image shows the ethylene glycol concentration cross-section of the grid-shaped flow field in the simulation.

[0083] Figure 62 The simulation shows multiple cross-sections of ethylene glycol concentration in a grid-shaped flow field.

[0084] Figure 63 The surface concentration distribution of sodium glycolate in the grid-shaped flow field is shown.

[0085] Figure 64 The sodium glycolate concentration cross-section is shown in the simulated grid-shaped flow field.

[0086] Figure 65 The simulation shows multiple cross-sections of sodium glycolate concentration in a grid-shaped flow field.

[0087] Figure 66 The electrolyte potential is shown in the simulation of the grid-shaped flow field.

[0088] Figure 67 The ground potential of the grid-shaped flow field in the simulation is shown.

[0089] Figure 68 The pressure distribution of the point-shaped flow field in the simulation is shown.

[0090] Figure 69 The multi-section of electrolyte flow velocity in the point-shaped flow field is shown.

[0091] Figure 70 The cross-section of electrolyte velocity in the point-shaped flow field is shown.

[0092] Figure 71 The electrolyte velocity streamlines are shown in the simulation of the point-shaped flow field.

[0093] Figure 72 The OH values ​​of the point-shaped flow field in the simulation are shown. - Surface concentration distribution.

[0094] Figure 73 The OH values ​​of the point-shaped flow field in the simulation are shown. - Concentration cross-section.

[0095] Figure 74 The OH values ​​of the point-shaped flow field in the simulation are shown. - Concentration multi-faceted.

[0096] Figure 75 The surface concentration distribution of ethylene glycol in the point-shaped flow field is shown.

[0097] Figure 76 The figure shows the ethylene glycol concentration cross-section of the point-shaped flow field in the simulation.

[0098] Figure 77 The simulation shows multiple cross-sections of ethylene glycol concentration in a point-shaped flow field.

[0099] Figure 78 The surface concentration distribution of sodium glycolate in the point-shaped flow field is shown.

[0100] Figure 79 The sodium glycolate concentration cross-section is shown in the simulation of the point-shaped flow field.

[0101] Figure 80 The simulation shows multiple cross-sections of sodium glycolate concentration in a point-shaped flow field.

[0102] Figure 81 The electrolyte potential is shown in the simulation of the point-shaped flow field.

[0103] Figure 82 The ground potential of the point-shaped flow field in the simulation is shown. Detailed Implementation

[0104] To more clearly illustrate the present invention, the following description, in conjunction with preferred embodiments and accompanying drawings, further clarifies the invention. It should be understood that 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 inventive effort are within the scope of protection of the present invention.

[0105] Example 1 This invention protects an electrolytic device for the electrocatalytic oxidation of ethylene glycol to prepare glycolate. The electrolytic device includes an electrolytic cell, which comprises a cathode plate, a cathode catalyst, a proton exchange membrane, an anode catalyst, and an anode plate arranged sequentially opposite to each other. See the structural description below. Figure 1 ; A cathode chamber is formed between the cathode plate and the proton exchange membrane, and an anode chamber is formed between the anode plate and the proton exchange membrane.

[0106] Furthermore, the electrolytic cell also includes an anolyte and a catholyte.

[0107] Furthermore, the anolyte is an alkaline electrolyte containing ethylene glycol (e.g., 2M ethylene glycol + 3M NaOH solution), and the catholyte is an alkaline electrolyte without ethylene glycol (e.g., 3M NaOH solution).

[0108] Furthermore, the anode plate has a rectangular structure and its surface has channels for the flow of anolyte.

[0109] Furthermore, the flow field of the anode plate includes one of the following: single serpentine flow field, multiple serpentine flow field, interdigitated flow field, grid flow field, point flow field, and straight flow field.

[0110] It should be noted that the single serpentine flow field is a common flow field design in electrolytic cells. Its core feature is that a single continuous meandering channel runs through the entire reaction area. The single channel is zigzag or U-shaped and covers the entire electrode surface. The inlet and outlet are located diagonally or on the same side. The cathode electrolyte is forced to flow through the complete path without any branching or parallel branches.

[0111] A multi-serpentine flow field can be understood as splitting a single serpentine flow field into multiple independent, parallel, non-intersecting small serpentine branches that share a common inlet / outlet manifold. After the fluid is split, it flows in parallel across the electrode surface. Each branch is a complete small serpentine, with each branch's flow path being shorter and narrower, resulting in a larger total flow cross-sectional area. After the flow split, the individual paths become shorter, the total flow resistance decreases significantly, and the pump consumption is much lower than that of a single serpentine flow field, making it suitable for large-area electrodes.

[0112] The channels of the interdigitated flow field are divided into inlet fingers and outlet fingers, which are arranged alternately in parallel. The cathode electrolyte cannot flow directly through the channel. It must enter from the inlet finger, then pass down through the porous electrode, and flow out from the outlet finger through transverse permeation. The end of each channel is completely closed, and there is no continuous passage.

[0113] The grid-shaped flow field has two types of channels, transverse and longitudinal, which are vertically intersecting and completely connected to form an open grid network. The cathode electrolyte can flow in any direction without a fixed path, making it the most "free" flow field structure.

[0114] The point-shaped flow field is a flow field without any continuous channels. There are only a large number of uniformly distributed discrete small bumps (cylindrical / square / hexagonal pillars) on the electrode plate, and the cathode electrolyte flows freely in the open gaps between the bumps.

[0115] The straight-through flow field is the most basic flow channel form in electrochemistry. It has multiple parallel, straight, and bend-free channels that run directly from the inlet to the outlet. The channels are completely independent and do not connect with each other. The cathode electrolyte flows in a straight line in one direction without any forced disturbance.

[0116] Furthermore, the flow field parameters of the anode plate include the channel spacing, channel width, and channel depth.

[0117] Furthermore, the channel spacing is 15-35mm, the channel width is 20-30mm, and the channel depth is 20-30mm.

[0118] Example 2 To achieve a stable scale-up of the electrocatalytic oxidation of ethylene glycol to prepare glycolate from the laboratory to the pilot-scale stage, this invention uses the CFD module of the fluid dynamics simulation software COMSOL Multiphysics 6.4 to simulate six types of anode plate flow fields (single serpentine flow field, multi serpentine flow field, interdigitated flow field, grid flow field, point flow field, and straight flow field). The boundary conditions are set as follows: the flow field size of the anode plate is 54 cm × 54 cm; Anodizing half-reaction equation: Ethylene glycol + 5OH- - - 4e = glycolate - + 4H2O; Anodic electrolyte composition: 3M NaOH + 2M ethylene glycol; Anode plate area: 0.29 m² 2 ; The cathode plate flow field dimensions are 54 cm × 54 cm; The half-reaction equation for cathodic reduction is: 4H₂O + 4e⁻ = 2H₂ + 4OH⁻ - ; Cathode electrolyte composition: 3M NaOH; Cathode plate area: 0.29 m² 2 Electrolysis reaction conditions: constant current mode, current = 400 A, cell voltage 1.0-1.5 V.

[0119] In simulation analysis, establishing reasonable assumptions is crucial because they can simplify the model, make the problem solvable, and preserve the key characteristics of the phenomenon under study. In this simulation analysis, the following assumptions can be made: 1. The fluid flow pattern involved in the calculation is free flow, laminar flow.

[0120] 2. The diffusion forms are considered as free diffusion, convective diffusion, and electromigration.

[0121] The first step is simulation: Parametric studies are conducted on the channel spacing, channel width, and channel depth of the six anode plate flow fields. The channel parameters with smaller pressure drop and larger reaction area in each flow field are selected as typical representatives.

[0122] The specific steps are as follows: 1) Constructing a single serpentine flow field simulation model: Based on the laminar flow physics field of the CFD module, the secondary current distribution physics field of the electrochemical module, and the rare matter transport physics field of the chemical substance transport module, the following models are constructed: Model 1-1 with channel spacing of 15mm, channel width of 20mm, and channel depth of 25mm; Model 1-2 with channel spacing of 15mm, channel width of 25mm, and channel depth of 20mm; and Model 1-3 with channel spacing of 15mm, channel width of 25mm, and channel depth of 25mm. Models with flow parameters 1-4 (15mm channel width, 25mm channel width, 30mm channel depth), models with flow parameters 1-5 (15mm channel spacing, 30mm channel width, 25mm channel depth), models with flow parameters 1-6 (25mm channel spacing, 25mm channel width, 25mm channel depth), and models with flow parameters 1-7 (35mm channel spacing, 25mm channel width, 25mm channel depth) were used to obtain the pressure drop and reaction area statistics for a single serpentine flow field under different flow parameters. The results are shown in [reference missing]. Figure 2 .

[0123] 2) Following the steps above, construct simulation models for multi-serpentine flow fields, interdigitated flow fields, grid-shaped flow fields, point-shaped flow fields, and straight-through flow fields respectively. Obtain the pressure drop and reaction area statistics for different flow fields under different channel parameters. See the results below. Figure 3-7 .

[0124] 3) Analysis: In the first step of the simulation process, combined with... Figures 2 to 7 Based on the results, flow channel parameters with smaller pressure drop and larger reaction area were selected for each flow field. The final determinations were as follows: For a single serpentine flow field, a flow field design with a channel spacing of 15 mm, a channel width of 25 mm, and a channel depth of 30 mm was selected as a typical representative; for a multi-serpentine flow field, a flow field design with a channel spacing of 15 mm, a width of 25 mm, and a channel depth of 30 mm was selected as a typical representative; for an interdigitated flow field, some areas became dead zones and were not suitable for subsequent research; for a grid-shaped flow field, a flow field design with a channel spacing of 15 mm, a width of 20 mm, and a channel depth of 25 mm was selected as a typical representative; for a point-shaped flow field, a flow field design with a hole spacing of 15 mm, a hole diameter of 25 mm, and a channel depth of 20 mm was selected as a typical representative; for a straight-through flow field, a flow field design with a channel spacing of 15 mm, a width of 20 mm, and a channel depth of 25 mm was selected as a typical representative.

[0125] The second step is simulation: Based on the simulation results from the first step, pressure drop, electrolyte potential, electrode potential to ground, electrolyte flow rate, and OH are measured for typical representatives of each flow field type.- Through simulation calculations of the concentrations of ethylene glycol and sodium glycolate, the optimal flow field configuration was finally optimized.

[0126] The study yields visualizations and related data on fluid velocity, pressure, electrolyte potential, ground electrode potential, and concentration. Velocity contour plots visually represent the flow velocity and direction of the fluid in different regions; pressure distribution plots show pressure changes during flow, helping to identify pressure gradients; electrolyte potential visualizations illustrate the magnitude and direction of potential within the electrolyte; concentration plots show the mass distribution of different substances in the system; and ground electrode potential plots describe the magnitude and direction of the potential of the working electrode (or a point within the electrode) relative to the reference ground.

[0127] 2) Analysis: Based on the pressure drop, velocity distribution, electric field potential, and reactant (OH) of the five typical flow fields selected above (single serpentine flow field, multi-serpentine flow field, straight-through flow field, grid flow field, and point flow field), - A system simulation study of the concentration distribution of ethylene glycol and product (sodium glycolate) was conducted to comprehensively demonstrate from multiple dimensions the scientific basis for the optimal flow field configuration for the electrocatalytic oxidation of ethylene glycol to glycolic acid under this flow field size.

[0128] Pressure distribution in a single serpentine flow field, multi-sectional distribution of electrolyte velocity, electrolyte velocity streamlines, OH - Surface concentration distribution, OH - Concentration profile, OH - For the results of multi-section concentration analysis, ethylene glycol surface concentration distribution, ethylene glycol concentration profile, ethylene glycol concentration multi-section, sodium glycolate surface concentration distribution, sodium glycolate concentration profile, sodium glycolate concentration multi-section, electrolyte potential, and potential to ground, please refer to the graphs. Figures 8 to 22 .

[0129] Pressure distribution in multi-serpentine flow field, multi-sectional distribution of electrolyte velocity, electrolyte velocity streamlines, OH - Surface concentration distribution, OH - Concentration profile, OH - For the results of multi-section concentration analysis, ethylene glycol surface concentration distribution, ethylene glycol concentration profile, ethylene glycol concentration multi-section, sodium glycolate surface concentration distribution, sodium glycolate concentration profile, sodium glycolate concentration multi-section, electrolyte potential, and potential to ground, please refer to the graphs. Figures 23 to 37 .

[0130] Pressure distribution in a straight-through flow field, multi-sectional distribution of electrolyte velocity, electrolyte velocity streamlines, OH - Surface concentration distribution, OH - Concentration profile, OH -For the results of multi-section concentration analysis, ethylene glycol surface concentration distribution, ethylene glycol concentration profile, ethylene glycol concentration multi-section, sodium glycolate surface concentration distribution, sodium glycolate concentration profile, sodium glycolate concentration multi-section, electrolyte potential, and potential to ground, please refer to the graphs. Figures 38 to 52 .

[0131] Pressure distribution in a grid-shaped flow field, multi-sectional distribution of electrolyte velocity, electrolyte velocity streamlines, OH - Surface concentration distribution, OH - Concentration profile, OH - For the results of multi-section concentration analysis, ethylene glycol surface concentration distribution, ethylene glycol concentration profile, ethylene glycol concentration multi-section, sodium glycolate surface concentration distribution, sodium glycolate concentration profile, sodium glycolate concentration multi-section, electrolyte potential, and potential to ground, please refer to the graphs. Figures 53 to 67 .

[0132] Pressure distribution of point-shaped flow field, multi-sectional distribution of electrolyte velocity, electrolyte velocity streamlines, OH - Surface concentration distribution, OH - Concentration profile, OH - For the results of multi-section concentration analysis, ethylene glycol surface concentration distribution, ethylene glycol concentration profile, ethylene glycol concentration multi-section, sodium glycolate surface concentration distribution, sodium glycolate concentration profile, sodium glycolate concentration multi-section, electrolyte potential, and potential to ground, please refer to the graphs. Figures 68 to 82 .

[0133] The simulation data obtained based on the simulation calculations are shown in Table 1.

[0134] Table 1

[0135] Note: CV is the coefficient of variation for the corresponding indicator.

[0136] Regarding electrolyte flow rate The velocity CV values ​​for the five flow fields are as follows: Single serpentine flow field 0.31 ( Figure 9 ), multi-serpentine flow field 0.90 ( Figure 24 ), point-shaped flow field 1.63 ( Figure 69 ), grid-shaped flow field 1.77 ( Figure 54 Straight-through flow field 1.75 ( Figure 39 Numerically, the single serpentine flow field exhibits the lowest velocity CV and the best surface velocity uniformity. However, further analysis of the average velocity reveals that its average velocity is as high as 0.065 m / s, significantly higher than the 0.014 m / s of the multi-serpentine flow field. By observing the cross-sectional diagram, the velocity distribution within the flow channel can be visually presented. (Single serpentine flow field...) Figure 10 The main flow is evenly distributed along the centerline of the channel, with a higher proportion and continuous distribution of high-velocity regions, resulting in a multi-serpentine flow field. Figure 25 High velocities are concentrated only at local inlets and bends, while velocities are relatively low in most channels. Other flow fields ( Figure 40 , Figure 55 , Figure 70 The velocity distribution within the flow field is clearly uneven. (A straight-through flow field...) Figure 41 ), grid-shaped flow field ( Figure 56 ) and point-shaped flow field ( Figure 71 The flow field streamline diagrams show obvious eddies, significant flow short-circuiting and dead zones, reflecting the highly discrete and homogeneous deterioration of the velocity distribution. Figure 11 The flow diagram shows obvious flow deviation, extremely low fluid flow rate at the wall and edge regions, large potential dead zones, and multiple serpentine flow field streamlines. Figure 26 The results show significantly better flow coverage, with fluid evenly distributed along multiple flow channels, covering most of the electrode surface area without obvious dead zones. This distribution characteristic is consistent with the calculated volume CV: the lower CV value of a single serpentine flow field corresponds to a more uniform velocity distribution, while the high CV value of a multi-serpentine flow field directly reflects the local accumulation and overall dispersion of velocity. Although high velocity can improve local mass transfer efficiency to some extent, it can lead to a sharp increase in pressure drop along the flow channel, easily causing excessive fluid disturbance within the channel and affecting overall operational stability.

[0137] While the velocity cross-section (CV) of the multi-serpentine flow field is higher than that of the single-serpentine flow field, it is the best performing among all the non-single-serpentine flow fields, and the average velocity is more reasonable. Through a multi-channel parallel split design, the electrolyte fluid is evenly distributed across multiple short branches, effectively reducing the velocity distortion caused by the long path of a single channel. The overall velocity distribution is uniform, without local high-velocity zones or fluid stagnation dead zones. This uniform and gentle velocity distribution avoids energy waste caused by high velocities while ensuring smooth electrolyte propagation within the flow channel, providing a stable fluid environment for the mass transfer process. It balances mass transfer efficiency and energy consumption control, outperforming the "uniform but high-energy-consumption" mode of the single-serpentine flow field.

[0138] The velocity coefficients (CVs) of point-shaped, grid-shaped, and straight-through flow fields all exceeded 1.4, exhibiting extremely uneven velocity distribution and significant performance defects. Specifically, the point-shaped flow field contained numerous fluid stagnation zones (dead zones), leading to low mass transfer efficiency within the flow channel and hindering the full progress of the electrolysis reaction. The grid-shaped and straight-through flow fields, on the other hand, contained localized high-velocity regions, which not only exacerbated energy loss but also resulted in localized excessively rapid or insufficient mass transfer within the flow channel, disrupting the overall reaction consistency of the electrolyzer. In summary, the multi-serpentine flow field achieved an optimal balance between velocity uniformity and energy consumption rationality, laying the foundation for the overall stable operation of the electrolyzer.

[0139] In OH - Concentration OH in each flow channel -The concentration CV and average concentration test results are as follows: serpentine flow field 0.65 (average concentration 1.94 M) Figure 27 Single serpentine flow field 0.67 (average concentration 1.76 M) Figure 12 Point-shaped flow field 0.5 (average concentration 2.27 M) Figure 72 ), grid-shaped flow field 0.15 (average concentration 2.84 M) Figure 57 Straight-through flow field 0.15 (average concentration 2.86 M) Figure 42 From the CV values, the OH values ​​of single-serpentine flow field and multi-serpentine flow field are... - The concentration CV was the highest, while other flow fields were lower than the two mentioned above. However, a point-like flow field could be observed from the multi-section diagram. Figure 74 ), grid-shaped flow field ( Figure 59 Straight-through flow field Figure 44 The overall high concentration and uneven distribution of key components stem from insufficient electrolyte renewal caused by numerous eddies and dead zones in the flow field. Reactants are excessively consumed in some areas, while electrolyte participation is minimal in other areas, resulting in severe local depletion. This significantly exacerbates concentration polarization and reduces reaction efficiency. From the cross-sectional view, the single serpentine flow field ( Figure 13 The concentration of OH- exhibits a significant gradient along the flow direction, with the highest concentration at the inlet. As the electrolyte flows and participates in the reaction within the channel, the concentration of OH- increases. - The concentration gradually decreases, reaching its lowest near the outlet, reflecting a significant dispersion in the component distribution within the flow channel, resulting in a multi-serpentine flow field. Figure 28 The cross-sectional cloud map shows that the electrolyte components exhibit a concentration gradient from the inlet to the outlet in each channel. However, due to the parallel distribution of multiple channels, the overall concentration distribution is more balanced, without the extreme local concentration distortion seen in a single serpentine flow field. This indicates that the multi-serpentine flow field achieves extensive coverage of the electrolyte on the electrode surface through the multi-channel structure, effectively avoiding severe flow deviation in a single channel and demonstrating a significant advantage in suppressing local concentration differences.

[0140] Regarding pressure Pressure CV is used to evaluate the uniformity of pressure distribution across the entire flow field. It is a key indicator for measuring the energy consumption and operational stability of the flow channel. Uneven pressure distribution can lead to local high-pressure or low-pressure areas in the flow field, which not only increases energy consumption but also causes fluid velocity distortion, affecting mass transfer efficiency and electrode reaction consistency, and even shortening the service life of the electrolyzer.

[0141] The pressure CV and average pressure test results for each flow field are as follows: Multi-serpentine flow field 0.20 (average pressure 6.53 Pa) Figure 23 Single serpentine flow field 0.61 (average pressure 27.60 Pa) Figure 8Point-shaped flow field 0.04 (average pressure 4.79 Pa) Figure 68 ), grid-shaped flow field 0.03 (average pressure 11.13 Pa) Figure 53 Straight-through flow field 0.07 (average pressure 10.79 Pa) Figure 38 The pressure coefficient (CV) of a single serpentine flow field is 0.61, indicating poor pressure distribution uniformity. The average pressure is as high as 27.60 Pa, which is 4.2 times that of a multi-serpentine flow field. The excessively high average pressure significantly increases the operating cost of the electrolyzer. At the same time, the long channel structure of the single serpentine flow field results in a large pressure loss along the flow path. The difference in the distribution of high pressure at the front end and low pressure at the rear end will cause fluid velocity distortion, further affecting the mass transfer and reaction consistency of the flow channel.

[0142] The multi-serpentine flow field, through its multi-channel parallel design, increases the total flow cross-sectional area, effectively reducing pressure loss along the flow path and resulting in a more uniform pressure distribution across the entire area, eliminating localized high-pressure or low-pressure zones. Its average pressure is 6.53 Pa, significantly lower than that of a single-serpentine flow field, substantially reducing operating costs. Simultaneously, the uniform pressure distribution ensures smooth fluid flow in each branch, preventing velocity distortion and providing a stable environment for mass transfer and electrode reactions, further enhancing the overall operational stability of the electrolyzer.

[0143] While the pressure coefficients (CVs) of point-shaped, grid-shaped, and straight-through flow fields are lower than those of the multi-serpentine flow field, they have significant performance limitations: the average pressure of the point-shaped flow field is only 4.79 Pa, which is too low, resulting in insufficient fluid velocity and low mass transfer efficiency; the average pressure of the grid-shaped flow field is as high as 11.13 Pa, leading to higher energy consumption; and although the pressure distribution of the straight-through flow field is more uniform, the average pressure fluctuates greatly, making it impossible to balance energy consumption and mass transfer efficiency. In summary, the multi-serpentine flow field exhibits the best overall performance in terms of pressure distribution uniformity and energy consumption control, making it the optimal choice for reducing electrolyzer operating costs and improving operational stability.

[0144] Regarding sodium glycolate concentration C2H3O3 - As the core product of the electrolysis reaction, its concentration variation coefficient is a key indicator for evaluating the uniformity of product distribution and the consistency of electrode reactions within the flow field. Measured data show that the C2H3O3 concentration in the five flow channels... - The concentration CVs are as follows: 0.79 for a single serpentine flow field. Figure 18 ), multi-serpentine flow field 1.16 ( Figure 33 ), point-shaped flow field 1.16 ( Figure 78 ), grid-shaped flow field 2.8 ( Figure 63 Straight-through flow field 3.48 ( Figure 48 ).

[0145] The CV values ​​are largest for grid-shaped and straight-through flow fields, and are obtained from multiple cross-sections of the grid-shaped flow field. Figure 65) and straight-through flow field with multiple sections ( Figure 50 It can be determined that reactants in local areas are excessively consumed, while electrolytes in other areas hardly participate in the reaction, indicating a serious local depletion phenomenon. This will significantly aggravate concentration polarization and reduce reaction efficiency.

[0146] The single serpentine flow field had the lowest CV value and the highest average concentration (0.6846 M) among all groups, but the cross-sectional view of the single serpentine flow field ( Figure 19 It can be observed that its single-channel long flow channel structure brings extremely high pressure drop along the flow path, and at the same time, it is easy to cause product accumulation and concentration polarization at the back end of the flow channel, resulting in poor scale-up and inability to meet the long-term stable operation requirements of the electrolyzer.

[0147] The CV value of the multi-serpentine flow field is 1.16, which is comparable to that of the point-shaped flow field, but the average concentration is higher than that of the point-shaped flow field. While maintaining a reasonable distribution uniformity, it achieves a higher product yield; from the cross-sectional view ( Figure 34 It can be seen that its multi-channel parallel design effectively shortens the product discharge path, avoids local accumulation, and significantly reduces pumping energy consumption, taking into account reaction uniformity, yield, and operating economy. Although the CV of the point-shaped flow field is comparable to that of the multi-serpentine flow field, the cross-sectional view shows that... Figure 79 It can be seen that there are a large number of fluid dead zones, resulting in insufficient mass transfer efficiency and yield, and the overall performance is far inferior to that of multi-serpentine systems.

[0148] In summary, the multi-serpentine flow field in C2H3O3 - The optimal balance is achieved in terms of product distribution, yield, and energy consumption, making it the flow channel structure with the best overall performance in this study.

[0149] Regarding ethylene glycol concentration Ethylene glycol, as a reactant in the electrolysis reaction, has a coefficient of variation (CV) that is a key indicator for evaluating the uniformity of reactant distribution and the consistency of electrode reactions within the flow field. Measured data show that the CV of ethylene glycol concentration in the five flow channels is as follows: Single serpentine flow field 0.45 (… Figure 15 ), multi-serpentine flow field 0.47 ( Figure 30 ), point-shaped flow field 0.45 ( Figure 75 ), grid-shaped flow field 0.12 ( Figure 60 Straight-through flow field 0.12 ( Figure 45 ).

[0150] Although the CV values ​​of the grid-shaped flow field and the straight-through flow field are the smallest, the multi-section diagram of the grid-shaped flow field ( Figure 62 ) and multi-section diagram of straight flow field ( Figure 47 Observations show that reactants are excessively consumed in some areas, while electrolytes in other areas hardly participate in the reaction, indicating severe local depletion. This will significantly exacerbate concentration polarization and reduce reaction efficiency. This is evident from the multi-section diagram of the point-shaped flow field. Figure 77Observations show that although the concentration polarization phenomenon is better than that of grid-shaped and straight-through flow fields, it is still more pronounced than that of single serpentine and multi-serpentine flow fields.

[0151] From the cross-sectional view of the single serpentine flow field ( Figure 16 ) and multi-serpentine flow field cross-section diagram ( Figure 31 As can be seen, the concentration is highest in the inlet region of the single serpentine flow field. As the electrolyte flows and participates in the reaction in the channel, the concentration of ethylene glycol gradually decreases, and the concentration is lowest near the outlet. This reflects that the distribution of components in the channel is highly discrete. In the multi-serpentine flow field, the electrolyte components show a concentration gradient from the inlet to the outlet in each channel. However, due to the parallel distribution of multiple channels, the overall concentration distribution is more balanced, and there is no risk of extreme local concentration distortion as in the single serpentine flow field.

[0152] Regarding electrolyte potential Electrolyte potential CV reflects the uniformity of electrolyte potential distribution across the entire flow field and is a core indicator for evaluating the electrochemical performance of an electrolyzer. Its uniformity directly affects the consistency of electrode reactions, cell internal resistance, and overall reaction efficiency. Uneven potential distribution can lead to excessively high or low local electrode potentials, triggering activation polarization and ohmic polarization, increasing cell internal resistance, reducing electrolysis reaction efficiency, and even causing accelerated electrode wear and shortening the electrolyzer's service life.

[0153] The CV test results for electrolyte potential in each flow field are as follows: 0.03 for the multi-serpentine flow field. Figure 36 ), single serpentine flow field 0.04 ( Figure 21 Point-shaped flow field 0.03 ( Figure 81 ), grid-shaped flow field 0.56 ( Figure 66 Straight-through flow field 0.02 ( Figure 51 Test results show that the multi-serpentine flow field and the point-shaped flow field have the best stability of electrolyte potential electrochemical performance. Compared with the point-shaped flow field and the straight-through flow field, the multi-serpentine flow field has a greater advantage in the adaptability of electrochemical performance and overall flow field performance.

[0154] The electrolyte potential CV of a single serpentine flow field is 0.04, slightly higher than that of a multi-serpentine flow field, but the potential distribution uniformity is slightly worse. Its high flow velocity and high pressure drop lead to excessive electrolyte disturbance within the flow channel, resulting in large local potential fluctuations and increased battery internal resistance. Simultaneously, the mass transfer unevenness caused by the high flow velocity further exacerbates the potential distribution differences, leading to decreased electrode reaction consistency, enhanced activation polarization and ohmic polarization, and reduced electrolysis efficiency.

[0155] The multi-serpentine flow field exhibits an electrolyte potential CV of 0.03, with extremely uniform potential distribution and good electrode surface potential consistency. This effectively suppresses activation polarization and ohmic polarization, reduces battery internal resistance, and improves electrolysis efficiency. Its uniform flow rate, pressure, and mass transfer distribution provide a stable electrochemical environment for the electrolyte-electrode reaction, ensuring consistent electrode reaction rates across all regions and preventing electrode wear caused by excessively high or low local potentials, thus extending the electrolyzer's lifespan. Simultaneously, the uniform potential distribution also reduces side reactions, improving reaction selectivity and product purity.

[0156] Regarding the electrode potential to ground The external potential of the anode under different flow field structures reflects the combined effect of the flow field on ohmic voltage drop and concentration polarization. Under the same current density, the lower the potential, the lower the energy consumption and the higher the energy efficiency of the electrolysis system. Single serpentine flow field: 48.1V ( Figure 22 ), multi-serpentine flow field 43.5V ( Figure 37 ), point-shaped flow field 42.9V ( Figure 82 ), grid-shaped flow field 3.88V ( Figure 67 Straight-through flow field 42.2V ( Figure 52 ).

[0157] The total potential of the grid-shaped flow field is only 3.88 V, far lower than other structures. This phenomenon does not represent a reduction in energy consumption, but rather a severe deterioration of the reaction environment caused by defects in the flow field structure. Numerous eddies and dead zones in the flow field lead to chaotic electrolyte flow, severe local ion supply insufficiency, extremely uneven distribution of concentration polarization and ohmic voltage drop, a significant reduction in the effective reaction area on the electrode surface, and extremely low actual electrochemical reaction efficiency.

[0158] The total potential of the single serpentine flow field is 48.1 V, the highest among all structures. This is mainly because its single-channel serpentine structure results in the longest electrolyte flow path, the largest ohmic voltage drop due to electrolyte resistance, and significant flow deviation. At the same time, there is a noticeable flow deviation phenomenon, insufficient electrolyte renewal at the flow channel edge, and intensified local concentration polarization, which further increases the total voltage of the system.

[0159] The total potentials of the point-shaped flow field, the multi-serpentine flow field, and the straight-through flow field were 42.9 V, 43.5 V, and 42.2 V, respectively, which were significantly lower than those of the single-serpentine flow field. The multi-serpentine flow field, through the parallel distribution of multiple flow channels, shortened the overall flow path of the electrolyte and effectively reduced the ohmic voltage drop; at the same time, it had better flow coverage, higher electrolyte renewal efficiency, and suppressed concentration polarization, thus significantly reducing the total potential level.

[0160] Although the potential levels of point-shaped and straight-through flow fields are slightly lower than those of multi-serpentine flow fields, they have flow short-circuit and local dead zones, poor uniformity of electrode surface reaction, and long-term operational stability is not as good as that of multi-serpentine flow fields.

[0161] Overall performance summary and discussion Based on the test results and analysis of the above five CV indicators, it can be seen that the five flow fields have significant differences in flow characteristics, mass transfer efficiency, energy consumption control and electrochemical performance. Among them, the multi-serpentine flow field, with its advantages of multi-channel parallel structure, shows excellent comprehensive performance in all CV indicators and is the optimal electrolyzer flow channel structure in this study.

[0162] Although the single serpentine flow field has different velocities CV and OH - While exhibiting some uniformity in concentration CV, it suffers from fatal flaws such as high pressure drop, high energy consumption, and low reaction rate, failing to meet the requirements of efficient, energy-saving, and stable operation of electrolyzers. Point-shaped flow fields show good performance in product and potential distribution, but suffer from problems such as fluid dead zones, low mass transfer efficiency, and insufficient total product generation, making them unsuitable for large-scale, efficient production. Grid-shaped flow fields have complex structures, resulting in poor performance in all CV indicators, and their flow, mass transfer, and electrochemical properties cannot meet the requirements for stable operation of electrolyzers. Straight-through flow fields, although simple in structure, suffer from uneven distribution of flow velocity, mass transfer, and pressure, which can easily lead to electrode wear and side reactions during long-term operation, resulting in poor overall performance.

[0163] The multi-serpentine flow field, through a multi-channel parallel design, effectively addresses the performance shortcomings of other flow channels: in terms of velocity (CV), it achieves a balance between uniform flow velocity and reasonable energy consumption, avoiding dead zones and high-velocity distortion; in terms of OH... - On the concentration and ethylene glycol concentration CV, uniform mass transfer at high concentrations was achieved, balancing reaction rate and consistency; on the pressure CV, uniform pressure distribution was achieved globally; on C2H3O3... - In terms of concentration CV, it ensures uniform product distribution and efficient discharge, improving product purity and production efficiency; in terms of electrolyte potential CV, it achieves uniform potential distribution, suppresses polarization, and extends the service life of the electrolyzer.

[0164] In summary, the multi-serpentine flow field achieves optimal balance in five core dimensions: flow uniformity, mass transfer efficiency, energy consumption control, product discharge, and electrochemical stability. Its comprehensive performance is significantly better than that of single-serpentine, point-shaped, grid-shaped, and straight-through flow fields. It can fully adapt to the high-efficiency, energy-saving, and stable operation requirements of electrolyzers and provides reliable theoretical and experimental basis for the optimized design of electrolyzer flow fields.

[0165] Obviously, the above embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the implementation of the present invention. Those skilled in the art can make other variations or modifications based on the above description. It is impossible to exhaustively list all possible implementations here. All embodiments falling under the scope of the present invention... Obvious variations or modifications derived from the technical solution are still within the scope of protection of this invention.

Claims

1. An anode plate for the electrocatalytic oxidation of ethylene glycol to prepare glycolate, characterized in that, When the area of ​​the anode plate is greater than or equal to the first area threshold, the flow field of the anode plate is a multi-serpentine flow field.

2. The anode plate according to claim 1, characterized in that, The first area threshold is 0.1 m. 2 .

3. The anode plate according to claim 1, characterized in that, The flow field of the anode plate is a flow channel for the anolyte to flow through.

4. The anode plate according to claim 1, characterized in that, The flow field of the anode plate has a channel spacing of 15-35mm, a channel width of 20-30mm, and a channel depth of 20-30mm.

5. The application of the anode plate as described in any one of claims 1-4 in the preparation of an electrolysis device.

6. An electrolytic apparatus for the electrocatalytic oxidation of ethylene glycol to prepare glycolate, characterized in that, The electrolytic cell includes a cathode plate, a cathode catalyst, a proton exchange membrane, an anode catalyst, and the anode plate as described in any one of claims 1-4, arranged sequentially. The cathode plate and the ion exchange membrane form a cathode chamber, the anode plate and the ion exchange membrane form an anode chamber, the anode chamber contains an anolyte, and the cathode chamber contains a cathode electrolyte.

7. The electrolysis apparatus according to claim 6, characterized in that, The cathode electrolyte is an alkaline electrolyte that does not contain ethylene glycol.

8. The electrolysis apparatus according to claim 6, characterized in that, The anolyte is an alkaline electrolyte containing ethylene glycol.

9. An electrocatalytic method for the electrocatalytic oxidation of ethylene glycol to prepare glycolate, characterized in that, The electrolytic apparatus according to any one of claims 6-8 is used to prepare glycolate by electrocatalytic oxidation of ethylene glycol; In this process, the cathode electrolyte enters the cathode chamber of the electrolytic cell, and the water in the cathode electrolyte is reduced to hydrogen gas at the cathode plate. The anolyte enters the anode chamber of the electrolytic cell and circulates and reacts in the electrolytic cell along the flow channels on the anode plate. The ethylene glycol in the anolyte is oxidized on the anode plate to form glycolate.

10. The electrocatalytic method according to claim 9, characterized in that, The flow rate of the cathode electrolyte in the flow channel is 0.3-10 L / min, the flow rate of the anolyte in the flow channel is 0.3-10 L / min, and the applied cell voltage is between 1.0-1.5 V.

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