Method and device for evaluating electrolytic bath pole plate structure, storage medium and electronic equipment

Abstract

The invention relates to a method and device for evaluating an electrolytic bath pole plate structure, a storage medium and electronic equipment, and the method comprises the steps: constructing a multi-physics field model based on an alkaline electrolytic bath, and carrying out finite element grid division to obtain a multi-physics field finite element model; when the multi-physics field finite element model is used for calculating the volume distribution of the bubbles in the small chamber, the bubbles are equivalent to particles, homogeneous flow is adopted, and the radial speed in the running speed is ignored; on the basis of enabling bubbles to be equivalent to particles and adopting homogeneous flow, setting a single-phase flow model equation for describing electrolyte flow by using single-phase flow in each finite element grid in a multi-physics field finite element model, and describing a convection-diffusion equation for describing bubble movement by using convection-diffusion; and iteratively operating the multi-physics field finite element model step by step, obtaining a multi-physics field distribution result of the to-be-evaluated electrolytic bath pole plate, and evaluating the structure of the to-be-evaluated electrolytic bath pole plate based on the multi-physics field distribution result. The structural design evaluation efficiency can be improved.

Description

Technical Field

[0001] This invention relates to the field of structural design technology, and in particular to a method, apparatus, storage medium, and electronic device for evaluating the structure of electrolytic cell electrode plates. Background Technology

[0002] An alkaline electrolyzer is composed of multiple chambers connected in series, each containing an electrolyte. Each chamber includes a cathode plate, a cathode catalytic electrode, a diaphragm, an insulating gasket, an anode catalytic electrode, and an anode plate. During the electrolysis of the electrolyte within each chamber, complex multi-physical processes are coupled, including but not limited to electrochemical processes, thermodynamic processes, gas-liquid two-phase flow processes, and ion mass transfer processes and their coupling.

[0003] In related technologies, the electrodes (referred to as electrolyzer electrodes) in industrial alkaline electrolyzers, such as the cathode and anode electrodes, often employ a papillary structure to enhance the uniformity of electrolyte flow within the chamber, thereby improving electrolysis efficiency. When the electrolyzer electrode structure is poorly designed, air bubbles may accumulate within the chamber, affecting the temperature distribution of the electrolyte and the reaction current, which in turn impacts the hydrogen production rate, energy efficiency, and product purity of the electrolyzer. Therefore, after designing the electrolyzer electrode structure, it is necessary to evaluate the designed electrodes.

[0004] To evaluate the rationality of the electrode structure design in an alkaline electrolyzer, experimental or simulation methods are typically used for verification. Experimental methods involve fabricating and assembling the designed electrode structure, building an alkaline electrolyzer experimental platform, and verifying its safety and performance. The electrode structure design is then evaluated based on the verification results. However, this method is time-consuming and expensive. For example, for a 1000 Nm³ industrial electrohydrogen production unit, the fabrication cost of the electrode can reach nearly one million yuan, while the electricity cost for the experiment alone can be at least several hundred thousand yuan. Furthermore, when the electrode structure design is unreasonable, the experimental plan also carries certain risks. Therefore, experimental methods cannot meet the needs of rapid iterative electrode structure design.

[0005] To meet the requirements of rapid iteration in electrode structure design, a multiphysics model based on the electrolytic cell electrode was constructed using multiphysics simulation technology. The finite element method (FEM) was then used to solve for the multiphysics distributions on the electrolytic cell electrode, including current distribution, temperature distribution, and bubble volume fraction distribution. The electrode structure design was then validated based on these multiphysics distribution results. However, while this method can effectively reduce the experimental cycle and cost of electrolytic cell electrode structure design, and multiphysics simulation technology can reflect the physical field distribution of the electrolytic cell electrode in a small chamber, the complex structure of the electrode surface leads to complex multiphysics process coupling during the finite element solution process, especially gas-liquid two-phase flow and its coupling. This results in poor convergence and slow convergence speed of the multiphysics model during the solution process, leading to low structural evaluation efficiency and failing to meet the performance verification requirements of complex electrode structures. Summary of the Invention

[0006] In view of this, the present invention provides a method, apparatus, storage medium, and electronic device for evaluating the structure of electrolytic cell plates.

[0007] Specifically, the present invention is achieved through the following technical solution:

[0008] According to a first aspect of the present invention, a method for evaluating the structure of an electrolytic cell electrode plate is provided, the method comprising:

[0009] Based on an alkaline electrolyzer including the electrode plates of the electrolyzer to be evaluated, a multiphysics model is constructed, and the multiphysics model is meshed into a finite element model to obtain a multiphysics finite element model.

[0010] Based on statistics of the diameter of bubbles generated during the electrolysis process of industrial alkaline electrolyzers, it is set that when using the multiphysics finite element model to calculate the volume distribution of bubbles in a small chamber, bubbles are equivalent to particles.

[0011] Based on the characteristics of the industrial alkaline electrolyzer using an alkaline pump to force convection of the electrolyte and the gas movement being affected by the alkaline flow, homogeneous flow is adopted in the multiphysics finite element model.

[0012] Based on the running speed of bubbles generated during the electrolysis process in an industrial alkaline electrolyzer on the surface of the electrolyzer electrode, the radial velocity in the running speed is ignored in the multiphysics finite element model.

[0013] Based on treating bubbles as particles and using homogeneous flow, the multiphysics finite element model sets up a single-phase flow model equation for each finite element mesh in the model to describe the electrolyte flow using single-phase flow, and a convection-diffusion equation to describe the bubble motion using convection-diffusion.

[0014] The multiphysics finite element model is iteratively calculated step by step to obtain the multiphysics distribution results of the electrode plate of the electrolytic cell to be evaluated, and the structure of the electrode plate of the electrolytic cell to be evaluated is evaluated based on the multiphysics distribution results.

[0015] Optionally, the step-by-step iterative calculation of the multiphysics finite element model to obtain the multiphysics distribution results of the electrolytic cell electrode plate to be evaluated includes:

[0016] Based on the single-phase flow model equation and convection-diffusion equation in the multiphysics finite element model, step-by-step iterative calculations are performed to obtain the bubble volume fraction distribution and liquid velocity distribution.

[0017] The current density distribution is calculated based on the electrolytic cell plate voltage, the minimum voltage at which the electrolysis reaction occurs, the current of the catalytic electrode, and the single-phase flow model equation.

[0018] The temperature field distribution is calculated based on the single-phase flow model equation, the convection-diffusion equation, the constant-pressure heat capacity of the electrolyte, the thermal conductivity of the electrolyte, and the heat source quantity.

[0019] Optionally, the single-phase flow model equations are as follows:

[0020]

[0021] Among them, u l It is the electrolyte velocity, ρ l It is the liquid density, φ l It is the liquid volume fraction; p is the pressure; K is the viscous stress tensor; K m Where is the diffusion stress; g is the gravitational acceleration; the convection-diffusion equation is as follows:

[0022]

[0023] Where, ρ g =1-ρ l It is the volume fraction of bubbles, D eff R' is the equivalent diffusion coefficient of the gas, and R' represents the effect of the bubble generation rate on the bubble volume fraction.

[0024] Optionally, the calculation of current density distribution based on the electrolytic cell electrode voltage, the minimum voltage at which the electrolytic reaction occurs, the current of the catalytic electrode, and the single-phase flow model equation includes:

[0025] Given the electrode voltage of the electrolyzer, the equivalent exchange current density of the catalytic electrode is obtained based on the current of the cathode catalytic electrode and the bubble volume fraction obtained from the single-phase flow model equation.

[0026] Based on the reaction current of the cathode catalytic electrode, the contact resistance between the cathode plate and the cathode catalytic electrode, the resistance of the cathode plate, the resistance of the diaphragm, and the ohmic overpotential, a first function for the current density distribution is constructed.

[0027] Based on the electrode voltage of the electrolytic cell, the minimum voltage at which the electrolytic reaction occurs, the ohmic overpotential, and the polarization overpotential of the cathode electrochemical reaction, a second function for the current density distribution is constructed.

[0028] Based on the equivalent exchange current density of the cathode catalytic electrode, the transfer coefficient of the cathode plate, the number of electrons transferred in the electrolysis reaction, the polarization overpotential of the electrochemical reaction of the cathode plate, the electrolyte temperature, and the reaction current of the cathode catalytic electrode, a third function of current density distribution is constructed.

[0029] The current density distribution is obtained based on the first current density distribution function, the second current density distribution function, and the third current density distribution function.

[0030] Optionally, the second function of the current density distribution is as follows:

[0031]

[0032] The first function of current density distribution is as follows:

[0033] η ohm =i(r c +r p +r d )

[0034] The third function of current density distribution is as follows:

[0035]

[0036]

[0037] Among them, E cell This refers to the voltage across the electrolytic cell electrodes. It is the minimum voltage at which the electrolysis reaction occurs, η ohm It is an ohmic overpotential, η A and η c These are the polarization overpotentials of the cathode and anodic electrochemical reactions, respectively; ΔG is the Gibbs free energy change; z is the number of electrons transferred in the electrolysis reaction; F is the Faraday constant; i is the current density, r c It is the contact resistance between the bipolar plate and the catalytic electrode, r p It is the resistance of the electrode, r d It is the resistance of the diaphragm; i eA i eC It is the equivalent exchange current density of the cathode catalytic electrode and the anode catalytic electrode; α Ais the transfer coefficient of the cathode plate, T is the electrolyte temperature, and R is the ideal gas constant.

[0038] Optionally, obtaining the current density distribution based on the first current density distribution function, the second current density distribution function, and the third current density distribution function includes:

[0039] The boundary heat source is obtained based on electrode potential, liquid volume fraction, equilibrium potential of electrolysis reaction, local reaction current density, and electrolyte temperature.

[0040] The ohmic heat density in the chamber is obtained based on the reaction current of the electrode, the electrode potential, the reaction current of the electrolyte, the electrode potential, and the electrode liquid potential.

[0041] Based on the boundary heat source and ohmic heat density, the amount of heat source provided by the electrolytic reaction is obtained.

[0042] The temperature field distribution is obtained based on the liquid density, the constant-pressure heat capacity of the electrolyte, the liquid velocity, the thermal conductivity of the electrolyte, and the heat source provided by the electrolysis reaction.

[0043] Optionally, the evaluation of the structure of the electrolytic cell electrode plate based on the multiphysics distribution results includes:

[0044] Based on the bubble volume fraction distribution, current density distribution and temperature field distribution in the multiphysics field distribution results, the highest bubble volume fraction value, the highest current density value and the highest temperature within the set area are obtained respectively.

[0045] If the highest bubble volume fraction value is higher than the preset bubble volume fraction threshold, or the highest current density value is higher than the preset current density threshold, or the temperature difference between the highest temperature and the inlet temperature is higher than the preset temperature difference threshold, the structural evaluation result of the electrolytic cell electrode plate to be evaluated is determined to be unqualified.

[0046] The method for evaluating the electrode structure of an electrolytic cell in this technical solution, based on the statistical analysis of the bubble diameter generated during the electrolysis process in an industrial alkaline electrolytic cell, treats bubbles as particles when calculating the bubble volume distribution in a small chamber using a multiphysics finite element model. Given that industrial alkaline electrolytic cells use an alkaline pump for forced convection of the electrolyte, and gas movement is affected by the alkaline flow, homogeneous flow is adopted in the multiphysics finite element model. Furthermore, based on the running speed of bubbles generated during the electrolysis process on the surface of the electrolytic cell electrode, the radial velocity in the running speed is ignored in the multiphysics finite element model. This effectively reduces the nonlinearity and coupling degree of the multiphysics finite element model, thereby improving computational efficiency and structural design evaluation efficiency.

[0047] According to a second aspect of the present invention, an apparatus for evaluating the structure of an electrolytic cell electrode plate is provided, the apparatus comprising:

[0048] The finite element model construction module is used to construct a multiphysics model based on an alkaline electrolyzer including the electrode plates of the electrolyzer to be evaluated, and to perform finite element meshing on the multiphysics model to obtain a multiphysics finite element model.

[0049] The first simplification module is used to, based on statistics of the diameter of bubbles generated during the electrolysis process of industrial alkaline electrolyzers, set up to treat bubbles as particles when calculating the volume distribution of bubbles in a small chamber using the multiphysics finite element model.

[0050] The second simplification module is used to set homogeneous flow in the multiphysics finite element model based on the characteristic that the industrial alkaline electrolyzer uses an alkaline pump to force convection of the electrolyte and the gas movement is affected by the alkaline flow.

[0051] The third simplification module is used to set the radial velocity in the running speed of the bubbles generated during the electrolysis process of the industrial alkaline electrolyzer on the surface of the electrolyzer electrode to be ignored in the multiphysics finite element model.

[0052] The model parameter setting module is used to set the single-phase flow model equations for describing the electrolyte flow using single-phase flow for each finite element mesh in the multiphysics finite element model, based on equating bubbles to particles and using homogeneous flow, and the convection-diffusion equations for describing bubble motion using convection-diffusion.

[0053] The structural design evaluation module is used to perform step-by-step iterative calculations on the multiphysics finite element model, obtain the multiphysics distribution results of the electrolytic cell electrode plate to be evaluated, and evaluate the structure of the electrolytic cell electrode plate to be evaluated based on the multiphysics distribution results.

[0054] According to a third aspect of the invention, a storage medium is provided having a computer program stored thereon, which, when executed by a processor, implements the steps of the method for evaluating the electrode structure of an electrolytic cell in any possible implementation of the first aspect.

[0055] According to a fourth aspect of the present invention, an electronic device is provided, including a memory, a processor, and a computer program stored in the memory and executable on the processor, wherein the processor executes the program to implement the steps of the method for evaluating the electrode structure of an electrolytic cell in any possible implementation of the first aspect. Attached Figure Description

[0056] The accompanying drawings, which are incorporated in and form part of this specification, illustrate embodiments consistent with the invention and, together with the description, serve to explain the principles of the invention.

[0057] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or related technologies will be briefly introduced below. Obviously, those skilled in the art can obtain other drawings based on these drawings without creative effort.

[0058] Figure 1 A flowchart illustrating a method for evaluating the electrode structure of an electrolytic cell according to an embodiment of the present invention;

[0059] Figure 2 This is a schematic diagram of the structure of an electrolytic cell in a method for evaluating the electrode structure of an electrolytic cell according to an embodiment of the present invention;

[0060] Figure 3 This is a schematic diagram of the structure of the electrolytic cell electrode plate in the electrolytic cell provided in an embodiment of the present invention;

[0061] Figure 4 This is a partial schematic diagram of a multiphysics model constructed based on electrolytic cell plates provided in an embodiment of the present invention;

[0062] Figure 5 A schematic diagram of the electrolyte velocity distribution field and streamlines in a multiphysics finite element model provided in an embodiment of the present invention;

[0063] Figure 6 A schematic diagram of the bubble volume fraction distribution field in a multiphysics finite element model provided in an embodiment of the present invention;

[0064] Figure 7 A schematic diagram of the current density distribution field of the multiphysics finite element model provided in this embodiment of the invention;

[0065] Figure 8 A schematic diagram of the temperature distribution field of a multiphysics finite element model provided in an embodiment of the present invention;

[0066] Figure 9 A schematic diagram of an apparatus for evaluating the electrode structure of an electrolytic cell provided in an embodiment of the present invention;

[0067] Figure 10 This is a schematic diagram of the structure of an electronic device provided in an embodiment of the present invention. Detailed Implementation

[0068] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0069] In related technologies, multiphysics simulation technology is used to construct a multiphysics model based on the electrode plate of an electrolytic cell. The multiphysics distribution results on the electrode plate in the multiphysics model are solved using the finite element method. The electrode plate structure design is evaluated based on the multiphysics distribution results. However, due to the complex multiphysics process coupling during the finite element solution process, especially the gas-liquid two-phase flow and its coupling, the multiphysics model has poor convergence and slow convergence speed, resulting in low efficiency in structural evaluation and failing to meet the performance verification requirements of complex electrode plate structures. Furthermore, the equations for solving the multiphysics field and its coupled fields are large in scale, requiring high computational resources and consuming a lot of memory. Generally, cloud platforms are needed for computation, which leads to high computational costs and difficulties in maintaining confidentiality during data transmission.

[0070] In this embodiment, by decoupling the multiphysics model, the nonlinearity in the multiphysics model is reduced, thereby reducing the computational scale of the multiphysics model, improving the convergence of the multiphysics model, improving the evaluation efficiency of the electrolytic cell structure, and realizing the rapid verification and evaluation of the electrode structure of the electrolytic cell of the alkaline electrohydrogen production equipment. The verification and evaluation include, but are not limited to: reaction dead zone test, reaction current density limit test, and temperature limit test.

[0071] See Figure 1 This invention provides a method for evaluating the structure of an electrolytic cell electrode plate, which may include the following steps:

[0072] S101. Based on an alkaline electrolytic cell including the electrode plates of the electrolytic cell to be evaluated, a multiphysics model is constructed, and the multiphysics model is meshed into a finite element model to obtain a multiphysics finite element model.

[0073] Figure 2 This is a schematic diagram of the structure of an electrolytic cell in a method for evaluating the electrode structure of an electrolytic cell according to an embodiment of the present invention;

[0074] Figure 3 This is a schematic diagram of the structure of the electrolytic cell electrode plate in the electrolytic cell provided in an embodiment of the present invention;

[0075] Figure 4 This is a partial schematic diagram of a multiphysics model constructed based on electrolytic cell plates, provided in an embodiment of the present invention.

[0076] like Figures 2 to 4 As shown, in this embodiment, an alkaline electrolyzer with a diameter of 40 cm, including the electrode plates of the electrolyzer to be evaluated, is used as an example. The geometric structure of the alkaline electrolyzer for structural design is obtained and used as a multiphysics model. Finite element meshing is then performed on the multiphysics model. As an optional embodiment, for the electrode plate area of ​​the electrolyzer to be evaluated, which has a large number of covered bubbles according to experimental statistics, a smaller finite element mesh is set. For example, for the papillary structure, the finite element mesh density is larger, and the mesh parameters of the finite element mesh are set.

[0077] S102. Based on the statistics of the diameter of bubbles generated during the electrolysis process of industrial alkaline electrolyzers, when using the multiphysics finite element model to calculate the volume distribution of bubbles in the small chamber, the bubbles are equivalent to particles.

[0078] In this embodiment, for industrial alkaline electrolyzers, a woven nickel mesh is generally used as the substrate for the catalytic electrode. By statistically analyzing the diameter of bubbles generated during the electrolysis process in industrial alkaline electrolyzers using densely woven nickel mesh electrode structures, it can be seen that the bubble diameter generally does not exceed 100 μm. Therefore, in this embodiment, when calculating the bubble volume distribution in the small chamber, the bubbles can be treated as particles without affecting the accuracy of the bubble volume distribution calculation.

[0079] S103. Based on the characteristic that the industrial alkaline electrolytic cell uses an alkaline pump to force convection of the electrolyte and the gas movement is affected by the alkaline flow, homogeneous flow is adopted in the multiphysics finite element model.

[0080] In this embodiment, the industrial alkaline electrolyzer uses an alkaline pump to force convection of the electrolyte; therefore, the gas movement is mainly affected by the flow of the alkaline solution. Thus, when performing two-phase flow calculations, a homogeneous flow assumption can be used to simplify the multiphysics model, assuming that the gas and liquid flow velocities are the same in the multiphysics model.

[0081] S104. Based on the running speed of the bubbles generated during the electrolysis process in the industrial alkaline electrolytic cell on the surface of the electrolytic cell electrode, the radial velocity in the running speed is ignored in the multiphysics finite element model.

[0082] In this embodiment, by statistically analyzing the running speed of bubbles generated during the electrolysis process in an industrial alkaline electrolyzer on the surface of the electrolyzer electrode, it is shown that the tangential velocity of the bubbles on the surface of the electrolyzer electrode is much greater than the radial velocity. Therefore, the radial velocity of the bubbles on the surface of the electrolyzer electrode can be ignored, and its impact on the accuracy of the evaluation is almost negligible. However, by ignoring the radial velocity, the radial calculation parameters of the multiphysics model and the coupling effect between the radial calculation parameters and other calculation parameters can be effectively reduced.

[0083] S105. Based on treating bubbles as particles and using homogeneous flow, the multiphysics finite element model sets up a single-phase flow model equation for each finite element mesh in the multiphysics finite element model to describe the electrolyte flow using single-phase flow, and a convection-diffusion equation to describe the bubble motion using convection-diffusion.

[0084] In this embodiment, a mathematical expression equation for a multiphysics model is constructed based on equating bubbles to particles and using homogeneous flow. As an optional embodiment, the mathematical expression equation includes, but is not limited to: a single-phase flow model equation that uses single-phase flow to describe the flow of electrolyte, and a convection-diffusion equation that uses convection-diffusion to describe the motion of gas (bubbles).

[0085] In this embodiment, the single-phase flow model equation, based on the homogeneous flow assumption, is essentially a solution to a set of Navier-Stokes equations. Therefore, using the single-phase flow model equation based on the single-phase flow model to describe the electrolyte flow is physically consistent. As an optional embodiment, the single-phase flow model equation includes the following equations (1) and (2):

[0086]

[0087] Among them, u l It is the velocity of the liquid (electrolyte), ρ l It is the liquid density, φ l It is the liquid volume fraction; p is the pressure; K is the viscous stress tensor; K m is the diffused stress; g is the gravitational acceleration.

[0088] The convection-diffusion equation is used to describe gas motion. As an alternative embodiment, the convection-diffusion equation is as follows:

[0089]

[0090] Where, ρ g =1-ρ l It is the volume fraction of bubbles, D eff R' is the equivalent diffusion coefficient of the gas, representing the effect of the bubble formation rate on the bubble volume fraction. Its value is proportional to the reaction current density and affected by the bubble volume fraction ρ. g Influence.

[0091] In this embodiment, the Pecklet number is 0 in the radial direction of the electrolyte streamline. Therefore, the gas distribution in the radial direction depends entirely on the gas's equivalent diffusion coefficient D. eff The value of is given. Therefore, the equivalent diffusion coefficient D of the gas can be determined by comparing it with the bubble volume fraction calculation results in the radial direction of the streamlines from the mixture model. eff The value of .

[0092] S106. Perform step-by-step iterative calculations on the multiphysics finite element model to obtain the multiphysics distribution results of the electrolytic cell electrode plate to be evaluated, and evaluate the structure of the electrolytic cell electrode plate to be evaluated based on the multiphysics distribution results.

[0093] In this embodiment, as an optional implementation, the multiphysics finite element model is iteratively calculated step by step to obtain the multiphysics distribution results of the electrolytic cell electrode plate to be evaluated, including:

[0094] A11, based on the single-phase flow model equation and convection-diffusion equation in the multiphysics finite element model, step-by-step iterative calculations are performed to obtain the bubble volume fraction distribution and liquid velocity distribution;

[0095] In this embodiment, the bubble volume fraction ρ of each finite element mesh in the multiphysics finite element model is calculated iteratively through step-by-step iterative calculation. g Liquid velocity u l The distribution value.

[0096] In this embodiment, an equivalent approximation is made based on the traditional mixture model. By adopting a step-by-step iterative method, the hardware requirements for computation can be greatly reduced compared to the traditional mixture model.

[0097] A12, based on the electrolytic cell plate voltage, the minimum voltage at which the electrolysis reaction occurs, the current of the catalytic electrode, and the single-phase flow model equation, calculate the current density distribution;

[0098] In this embodiment, the presence of gas bubbles affects the electrochemical reaction and the current density distribution. On one hand, during the electrolyte reaction, gaseous products are present near both catalytic electrodes. The cathode catalytic electrode produces hydrogen, and the anode catalytic electrode produces oxygen. As these gaseous products move from the catalyst layer to the fluid channel, the gas covering the surface of the electrolytic cell electrodes hinders the contact between the catalyst and the electrolyte, thereby reducing the effective reaction area and increasing the polarization overpotential. On the other hand, the presence of gas bubbles increases the length of the hydroxide ion transport path between the electrodes, leading to an increase in the ohmic overpotential. Therefore, the bubble covering effect leads to a decrease in the efficiency of the electrochemical reaction.

[0099] In this embodiment, as an optional embodiment, the current density distribution is calculated based on the electrolytic cell plate voltage, the minimum voltage at which the electrolysis reaction occurs, the current of the catalytic electrode, and the single-phase flow model equation, including:

[0100] A121. Under a given electrolytic cell plate voltage, the equivalent exchange current density of the catalytic electrode is obtained based on the current of the cathode catalytic electrode and the bubble volume fraction obtained from the single-phase flow model equation.

[0101] In this embodiment, as an optional embodiment, taking the catalytic electrode as the cathode catalytic electrode as an example, the equivalent exchange current density i of the cathode catalytic electrode eA The value is calculated by the following formula:

[0102] i eA =i 0A ·f1(φ g (4)

[0103] In the formula, i 0A The current φ is the cathode catalytic electrode current. g =1-φ l .

[0104] A122, based on the reaction current of the cathode catalytic electrode, the contact resistance between the cathode plate and the cathode catalytic electrode, the resistance of the cathode plate, the resistance of the diaphragm and the ohmic overpotential, a first function of current density distribution is constructed;

[0105] A123, based on the electrode voltage of the electrolytic cell, the minimum voltage at which the electrolytic reaction occurs, the ohmic overpotential, and the polarization overpotential of the cathode electrochemical reaction, a second function for current density distribution is constructed;

[0106] A124. Based on the equivalent exchange current density of the cathode catalytic electrode, the transfer coefficient of the cathode plate, the number of electrons transferred in the electrolysis reaction, the polarization overpotential of the electrochemical reaction of the cathode plate, the electrolyte temperature, and the reaction current of the cathode catalytic electrode, a third function of current density distribution is constructed.

[0107] A125, based on the first current density distribution function, the second current density distribution function, and the third current density distribution function, the current density distribution is obtained.

[0108] In this embodiment, the electrode voltage of the electrolytic cell, the minimum voltage at which the electrolytic reaction occurs, the ohmic overpotential, and the polarization overpotential satisfy the following equation (second function of current density distribution):

[0109]

[0110] The first function of current density distribution is as follows:

[0111] η ohm =i(r c +r p +r d (7)

[0112] The third function of current density distribution is as follows:

[0113]

[0114] Among them, E cell This refers to the voltage across the electrolytic cell electrodes. It is the reversible voltage, representing the minimum voltage at which the electrolytic reaction occurs, η. ohm It is an ohmic overpotential, representing the voltage drop caused by the resistance between the two electrodes, η. A and η c These are the polarization overpotentials of the cathode and anodic electrochemical reactions, respectively; ΔG is the Gibbs free energy change, which can be considered as 22.66 kJ / mol for alkaline water electrolysis (AWE); z is the number of electrons transferred in the electrolysis reaction; F = 96485.33 C / mol is the Faraday constant; i is the current density, r c It is the contact resistance between the bipolar plate and the catalytic electrode, r p It is the resistance of the electrodes (plates), r d It is the resistance of the diaphragm; i eA i eC It is the equivalent exchange current density of the cathode catalytic electrode and the anode catalytic electrode; α A is the transfer coefficient of the cathode plate, T is the electrolyte temperature, and R is the ideal gas constant.

[0115] In this embodiment, as an optional embodiment, the volume fraction of the bubbles can be obtained based on the conductivity of the electrolyte and the conductivity of the electrolyte in the bubble layer, and the volume fraction of the liquid phase can be obtained based on the volume fraction of the bubbles.

[0116] In this embodiment, based on the Bruggeman model, the electrolyte conductivity σ in the bubble layer is... e With bubble volume fraction φ g The relation is:

[0117] σ e =σ ek ·f2(φ g (10)

[0118] Where, σ ek It is the conductivity of potassium hydroxide solution (alkaline solution).

[0119] A13, based on the single-phase flow model equation, convection-diffusion equation, constant-pressure heat capacity of electrolyte, thermal conductivity of electrolyte and heat source quantity, calculate the temperature field distribution.

[0120] In this embodiment, the temperature field distribution of the small chamber is calculated based on the liquid phase velocity distribution, bubble volume distribution, and current density distribution obtained in the above steps.

[0121] In this embodiment, as an optional implementation, the temperature field distribution is calculated based on the single-phase flow model equation, the convection-diffusion equation, the constant-pressure heat capacity of the electrolyte, the thermal conductivity of the electrolyte, and the heat source quantity, including:

[0122] A131, based on electrode potential, liquid volume fraction, equilibrium potential of electrolysis reaction, local reaction current density, and electrolyte temperature, obtains boundary heat source;

[0123] A132, based on the reaction current of the electrode, the electrode potential, the reaction current of the electrolyte, the electrode potential, and the electrode liquid potential, obtains the ohmic heat density in the chamber.

[0124] A133, based on the boundary heat source and ohmic heat density, obtains the amount of heat source provided by the electrolytic reaction;

[0125] A134 obtains the temperature field distribution based on liquid density, constant-pressure heat capacity of electrolyte, liquid velocity, thermal conductivity of electrolyte, and heat source provided by electrolysis reaction.

[0126] In this embodiment, within the small chamber, the temperature field distribution (of the electrolytic cell plates) is mainly affected by the electrolyte flow rate and the heat of electrochemical reaction. The formula for calculating the temperature field distribution is as follows:

[0127]

[0128] Q r =Q rH +Q m (12)

[0129]

[0130] Among them, c l This represents the constant-pressure heat capacity of the electrolyte, where T represents the temperature of the electrolyte, and kJ represents the constant-pressure heat capacity. l Q represents the thermal conductivity of the electrolyte. r Q represents the amount of heat provided by the electrolysis reaction. rH Q represents the ohmic heat density within the chamber. m Indicates the boundary heat source quantity. i s i l φ represents the reaction current in the electrode and electrolyte, respectively. s and φ l E represents the potential of the electrode and the electrode solution, respectively. eq i represents the equilibrium potential of the electrolytic reaction. loc This represents the local (boundary) reaction current density.

[0131] In this embodiment, as an optional embodiment, the structure of the electrolytic cell electrode plate to be evaluated is evaluated based on the multiphysics field distribution results, including:

[0132] Based on the bubble volume fraction distribution, current density distribution and temperature field distribution in the multiphysics field distribution results, the highest bubble volume fraction value, the highest current density value and the highest temperature within the set area are obtained respectively.

[0133] If the highest bubble volume fraction value is higher than the preset bubble volume fraction threshold, or the highest current density value is higher than the preset current density threshold, or the temperature difference between the highest temperature and the inlet temperature is higher than the preset temperature difference threshold, the structural evaluation result of the electrolytic cell electrode plate to be evaluated is determined to be unqualified.

[0134] In this embodiment, structural evaluation is performed based on the multiphysics distribution results (multiphysics calculation results) and judgment criteria. In this embodiment, for the reaction dead zone test, as an optional implementation, the bubble volume fraction threshold is set to 0.9, meaning the local bubble volume fraction value is set not to exceed 0.9; for the reaction current density exceeding the limit, the current density threshold is set to 20000 A / m². 2 That is, the local current density does not exceed 20000 A / m 2 For temperature limit testing, a temperature difference threshold of 15℃ is set, meaning the difference between the maximum temperature and the inlet temperature should not exceed 15℃. If any indicator value exceeds the corresponding threshold, the structural design of the electrolytic cell electrode plate is deemed unqualified and needs to be redesigned. Only when all indicator values ​​do not exceed the corresponding thresholds is the structural design of the electrolytic cell electrode plate deemed qualified, and production can proceed based on this design.

[0135] Figure 5 This is a schematic diagram of the electrolyte velocity distribution field and streamlines in a multiphysics finite element model provided in an embodiment of the present invention. Figure 5 As shown in this embodiment, the papillary structure enables the electrolyte to be evenly distributed inside the electrode, avoiding local eddies.

[0136] Figure 6 This is a schematic diagram of the bubble volume fraction distribution field in a multiphysics finite element model provided in an embodiment of the present invention. Figure 6 As shown in this embodiment, bubbles gradually accumulate along the fluid flow lines. In areas with high electrolyte flow rates and dense flow lines, the bubble volume fraction is relatively small. At the top of the electrode, where the flow lines are sparser and the flow rate is slower, the bubble volume fraction is greater than in other areas, indicating a larger bubble accumulation at the top of the chamber.

[0137] Figure 7 This is a schematic diagram of the current density distribution field in a multiphysics finite element model provided in an embodiment of the present invention. Figure 7 As shown, based on the bubble volume fraction values, the current on the electrolytic cell plates is concentrated at the papillae. In regions with smaller bubble volume fraction values, the current density at the papillae approaches 20000 A / m. 2 The current density is near the maximum specified value. Therefore, when designing the structure, the number of papillae can be appropriately increased to reduce the local current density of the papillae and reduce the pressure on individual papillae.

[0138] Figure 8 This is a schematic diagram of the temperature distribution field of a multiphysics finite element model provided in an embodiment of the present invention. Figure 8 As shown in the diagram, the calculation results reveal two main regions with higher temperatures: the area near the nipples and the top region of the electrolytic cell plates. Near the nipples, the higher current density generates more heat, leading to a greater temperature rise in the electrolyte. The higher temperature at the top region is due to the accumulation of heat along the streamlines of the fluid.

[0139] In this embodiment, as an optional embodiment, the method further includes:

[0140] The results of the evaluation of the structure of the electrolytic cell electrode plate under evaluation based on the multi-physics field distribution results indicate that the structural design of the electrolytic cell electrode plate under evaluation is unqualified.

[0141] If the highest current density value is higher than the preset current density threshold, or the temperature difference between the highest temperature and the inlet temperature is higher than the preset temperature difference threshold, the number of protrusions on the electrode plate of the electrolytic cell to be evaluated is increased.

[0142] In this embodiment, if the current density and temperature rise are close to or exceed the limit values, it is recommended to increase the number of papillae.

[0143] In this embodiment, a multiphysics model is constructed based on the geometry of an industrial electrolyzer. Single-phase flow is used to simplify the coupling of the multiphysics model, thereby reducing its nonlinearity, effectively reducing the computational scale, and improving its convergence. This allows for rapid tracking of the impact of changes in the electrolyzer electrode structure on the multiphysics, enabling the rationality assessment of different electrolyzer electrode structure designs and improving the evaluation efficiency of the electrolyzer electrode structure. Furthermore, due to the low computational resource requirements, local computation can be achieved, reducing the risk of leakage of structural design schemes. Moreover, with the same computational resources, the evaluation of electrolyzer electrode structures with more complex geometries can be applied, improving engineering applicability.

[0144] Based on the same inventive concept, such as Figure 9 As shown, this embodiment of the invention also provides an apparatus for evaluating the structure of an electrolytic cell electrode plate, the apparatus comprising:

[0145] The finite element model construction module 901 is used to construct a multiphysics model based on an alkaline electrolytic cell including the electrode plates of the electrolytic cell to be evaluated, and to perform finite element meshing on the multiphysics model to obtain a multiphysics finite element model.

[0146] In this embodiment, as an optional embodiment, for the electrolytic cell electrode area to be evaluated with a large number of covered bubbles as determined by experimental statistics, a smaller finite element mesh is set. For example, for the nipple structure, the finite element mesh density is larger, and the mesh parameters of the finite element mesh are set.

[0147] The first simplification module 902 is used to, based on the statistics of the diameter of bubbles generated during the electrolysis process of industrial alkaline electrolyzers, set the bubbles to be equivalent to particles when calculating the volume distribution of bubbles in a small chamber using the multiphysics finite element model.

[0148] In this embodiment, the bubble is equivalent to a particle in the case where a woven nickel mesh is used as the substrate for the catalytic electrode.

[0149] The second simplification module 903 is used to set homogeneous flow in the multiphysics finite element model based on the characteristic that the industrial alkaline electrolyzer uses an alkaline pump to force convection of the electrolyte and the gas movement is affected by the alkaline flow.

[0150] In this embodiment, the flow velocities of gas and liquid are set to be the same in the multiphysics finite element model.

[0151] The third simplification module 904 is used to set the radial velocity in the running speed to be ignored in the multiphysics finite element model based on the running speed of the bubbles generated during the electrolysis process of the industrial alkaline electrolyzer on the surface of the electrolyzer electrode.

[0152] In this embodiment, since the tangential velocity of the bubbles on the surface of the electrolytic cell electrode is much greater than the radial velocity, the radial velocity of the bubbles on the surface of the electrolytic cell electrode can be ignored.

[0153] The model parameter setting module 905 is used to set the single-phase flow model equations for describing the electrolyte flow using single-phase flow for each finite element mesh in the multiphysics finite element model, based on equating bubbles to particles and using homogeneous flow, and the convection-diffusion equations for describing bubble motion using convection-diffusion.

[0154] In this embodiment, a mathematical expression equation for a multiphysics model is constructed based on equating bubbles to particles and using homogeneous flow. As an optional embodiment, the mathematical expression equation includes, but is not limited to: a single-phase flow model equation that uses single-phase flow to describe the flow of electrolyte, and a convection-diffusion equation that uses convection-diffusion to describe the motion of gas (bubbles).

[0155] The structural design evaluation module 906 is used to perform step-by-step iterative calculations on the multiphysics finite element model, obtain the multiphysics distribution results of the electrolytic cell electrode plate to be evaluated, and evaluate the structure of the electrolytic cell electrode plate to be evaluated based on the multiphysics distribution results.

[0156] In this embodiment, as an optional embodiment, the structural design evaluation module 906 is specifically used for:

[0157] Based on the single-phase flow model equation and convection-diffusion equation in the multiphysics finite element model, step-by-step iterative calculations are performed to obtain the bubble volume fraction distribution and liquid velocity distribution.

[0158] The current density distribution is calculated based on the electrolytic cell plate voltage, the minimum voltage at which the electrolysis reaction occurs, the current of the catalytic electrode, and the single-phase flow model equation.

[0159] The temperature field distribution is calculated based on the single-phase flow model equation, the convection-diffusion equation, the constant-pressure heat capacity of the electrolyte, the thermal conductivity of the electrolyte, and the heat source quantity.

[0160] In this embodiment, as an optional embodiment, the current density distribution is calculated based on the electrolytic cell plate voltage, the minimum voltage at which the electrolysis reaction occurs, the current of the catalytic electrode, and the single-phase flow model equation, including:

[0161] Given the electrode voltage of the electrolyzer, the equivalent exchange current density of the catalytic electrode is obtained based on the current of the cathode catalytic electrode and the bubble volume fraction obtained from the single-phase flow model equation.

[0162] Based on the reaction current of the cathode catalytic electrode, the contact resistance between the cathode plate and the cathode catalytic electrode, the resistance of the cathode plate, the resistance of the diaphragm, and the ohmic overpotential, a first function for the current density distribution is constructed.

[0163] Based on the electrode voltage of the electrolytic cell, the minimum voltage at which the electrolytic reaction occurs, the ohmic overpotential, and the polarization overpotential of the cathode electrochemical reaction, a second function for the current density distribution is constructed.

[0164] Based on the equivalent exchange current density of the cathode catalytic electrode, the transfer coefficient of the cathode plate, the number of electrons transferred in the electrolysis reaction, the polarization overpotential of the electrochemical reaction of the cathode plate, the electrolyte temperature, and the reaction current of the cathode catalytic electrode, a third function of current density distribution is constructed.

[0165] The current density distribution is obtained based on the first current density distribution function, the second current density distribution function, and the third current density distribution function.

[0166] In this embodiment, as an optional embodiment, the current density distribution is obtained based on the first current density distribution function, the second current density distribution function, and the third current density distribution function, including:

[0167] The boundary heat source is obtained based on electrode potential, liquid volume fraction, equilibrium potential of electrolysis reaction, local reaction current density, and electrolyte temperature.

[0168] The ohmic heat density in the chamber is obtained based on the reaction current of the electrode, the electrode potential, the reaction current of the electrolyte, the electrode potential, and the electrode liquid potential.

[0169] Based on the boundary heat source and ohmic heat density, the amount of heat source provided by the electrolytic reaction is obtained.

[0170] The temperature field distribution is obtained based on the liquid density, the constant-pressure heat capacity of the electrolyte, the liquid velocity, the thermal conductivity of the electrolyte, and the heat source provided by the electrolysis reaction.

[0171] In this embodiment, as another optional embodiment, the structural design evaluation module 906 is further used for:

[0172] Based on the bubble volume fraction distribution, current density distribution and temperature field distribution in the multiphysics field distribution results, the highest bubble volume fraction value, the highest current density value and the highest temperature within the set area are obtained respectively.

[0173] If the highest bubble volume fraction value is higher than the preset bubble volume fraction threshold, or the highest current density value is higher than the preset current density threshold, or the temperature difference between the highest temperature and the inlet temperature is higher than the preset temperature difference threshold, the structural evaluation result of the electrolytic cell electrode plate to be evaluated is determined to be unqualified.

[0174] In this embodiment, as an optional embodiment, the device further includes:

[0175] The structural design optimization module (not shown in the figure) is used to determine the structural design of the electrolytic cell electrode plate to be evaluated based on the results of the multi-physics field distribution.

[0176] If the highest current density value is higher than the preset current density threshold, or the temperature difference between the highest temperature and the inlet temperature is higher than the preset temperature difference threshold, the number of protrusions on the electrode plate of the electrolytic cell to be evaluated is increased.

[0177] Based on the same inventive concept, embodiments of the present invention also provide a storage medium storing a computer program thereon, which, when executed by a processor, implements the steps of the method for evaluating the electrode structure of an electrolytic cell in any of the above possible implementations.

[0178] Alternatively, the storage medium may be a non-transitory computer-readable storage medium, such as a ROM, random access memory (RAM), CD-ROM, magnetic tape, floppy disk, and optical data storage device.

[0179] Based on the same inventive concept, see [link to inventive concept] Figure 10This invention also provides an electronic device, including a memory 101 (e.g., non-volatile memory), a processor 102, and a computer program stored in the memory 101 and executable on the processor 102. When the processor 102 executes the program, it implements the steps of the method for evaluating the electrode structure of an electrolytic cell in any of the above possible implementations, which can be equivalent to the aforementioned device for evaluating the electrode structure of an electrolytic cell. Of course, the processor can also be used to process other data or perform calculations. This electronic device can be a PC, server, terminal, or other similar device.

[0180] like Figure 10 As shown, the electronic device may also include: memory 103, network interface 104, and internal bus 105. In addition to these components, other hardware may also be included, which will not be described in detail here.

[0181] It should be noted that the above-mentioned device for evaluating the electrode structure of the electrolytic cell can be implemented by software. As a device in a logical sense, it is formed by the processor 102 of the electronic device in which it is located reading the computer program instructions stored in the non-volatile memory into the memory 103 for execution.

[0182] The embodiments of the subject matter and functional operation described in this specification can be implemented in the following ways: digital electronic circuits, tangibly embodied computer software or firmware, computer hardware including the structures disclosed in this specification and their structural equivalents, or combinations thereof. Embodiments of the subject matter described in this specification can be implemented as one or more computer programs, i.e., one or more modules of computer program instructions encoded on a tangible, non-transitory program carrier for execution by a data processing apparatus or for controlling the operation of a data processing apparatus. Alternatively or additionally, the program instructions may be encoded on artificially generated propagation signals, such as machine-generated electrical, optical, or electromagnetic signals, which are generated to encode information and transmit it to a suitable receiving device for execution by the data processing apparatus. The computer storage medium may be a machine-readable storage device, a machine-readable storage substrate, a random or serial access memory device, or combinations thereof.

[0183] The processing and logic flow described in this specification can be executed by one or more programmable computers that execute one or more computer programs to perform corresponding functions by operating on input data and generating output. The processing and logic flow can also be executed by special-purpose logic circuitry—such as FPGAs (Field-Programmable Gate Arrays) or ASICs (Application-Specific Integrated Circuits), and the device can also be implemented as special-purpose logic circuitry.

[0184] Suitable computers for executing computer programs include, for example, general-purpose and / or special-purpose microprocessors, or any other type of central processing unit. Typically, the central processing unit receives instructions and data from read-only memory and / or random access memory. The basic components of a computer include a central processing unit for implementing or executing instructions and one or more memory devices for storing instructions and data. Typically, a computer will also include one or more mass storage devices for storing data, such as disks, magneto-optical disks, or optical disks, or the computer will be operatively coupled to such mass storage devices to receive data from or transfer data to them, or both. However, a computer is not required to have such devices. Furthermore, a computer can be embedded in another device, such as a mobile phone, a personal digital assistant (PDA), a mobile audio or video player, a game console, a global positioning system (GPS) receiver, or a portable storage device such as a universal serial bus (USB) flash drive, to name a few.

[0185] Computer-readable media suitable for storing computer program instructions and data include all forms of non-volatile memory, media, and memory devices, such as semiconductor memory devices (e.g., EPROM, EEPROM, and flash memory devices), magnetic disks (e.g., internal hard disks or removable disks), magneto-optical disks, and CD-ROM and DVD-ROM disks. Processors and memory may be supplemented by or incorporated into dedicated logic circuitry.

[0186] While this specification contains numerous specific implementation details, these should not be construed as limiting the scope of any invention or the scope of the claims, but rather are primarily used to describe features of specific embodiments of a particular invention. Certain features described in the various embodiments herein may also be implemented in combination in a single embodiment. Conversely, various features described in a single embodiment may also be implemented separately in various embodiments or in any suitable sub-combination. Furthermore, while features may function in certain combinations as described above and even initially claimed in this way, one or more features from a claimed combination may be removed from that combination in some cases, and a claimed combination may refer to a sub-combination or a variation thereof.

[0187] Similarly, although the operations are depicted in a specific order in the accompanying drawings, this should not be construed as requiring these operations to be performed in the specific order shown or sequentially, or requiring all illustrated operations to be performed to achieve the desired result. In some cases, multitasking and parallel processing may be advantageous. Furthermore, the separation of various system modules and components in the above embodiments should not be construed as requiring such separation in all embodiments, and it should be understood that the described program components and systems can generally be integrated together in a single software product or packaged into multiple software products.

[0188] Thus, specific embodiments of the subject matter have been described. Other embodiments are within the scope of the appended claims. In some cases, the actions recited in the claims may be performed in a different order and still achieve the desired result. Furthermore, the processes depicted in the drawings are not necessarily shown in a specific order or sequence to achieve the desired result. In some implementations, multitasking and parallel processing may be advantageous.

[0189] It should be noted that, in this document, relational terms such as "first" and "second" are used merely to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such a process, method, article, or apparatus. Unless otherwise specified, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the process, method, article, or apparatus that includes the element.

[0190] The above are merely specific embodiments of the present invention, enabling those skilled in the art to understand or implement the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. Therefore, the present invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features claimed herein.

Claims

1. A method for evaluating the structure of electrolytic cell electrode plates, characterized in that, include: Based on an alkaline electrolyzer including the electrode plates of the electrolyzer to be evaluated, a multiphysics model is constructed, and the multiphysics model is meshed into a finite element model to obtain a multiphysics finite element model. Based on statistics of the diameter of bubbles generated during the electrolysis process of industrial alkaline electrolyzers, it is set that when using the multiphysics finite element model to calculate the volume distribution of bubbles in a small chamber, bubbles are equivalent to particles. Based on the characteristics of the industrial alkaline electrolyzer using an alkaline pump to force convection of the electrolyte and the gas movement being affected by the alkaline flow, homogeneous flow is adopted in the multiphysics finite element model. Based on the running speed of bubbles generated during the electrolysis process in an industrial alkaline electrolyzer on the surface of the electrolyzer electrode, the radial velocity in the running speed is ignored in the multiphysics finite element model. Based on treating bubbles as particles and using homogeneous flow, the multiphysics finite element model sets up a single-phase flow model equation for each finite element mesh in the model to describe the electrolyte flow using single-phase flow, and a convection-diffusion equation to describe the bubble motion using convection-diffusion. The multiphysics finite element model is iteratively calculated step by step to obtain the multiphysics distribution results of the electrode plate of the electrolytic cell to be evaluated, and the structure of the electrode plate of the electrolytic cell to be evaluated is evaluated based on the multiphysics distribution results.

2. The method for evaluating the electrode structure of an electrolytic cell according to claim 1, characterized in that, The step-by-step iterative calculation of the multiphysics finite element model to obtain the multiphysics distribution results of the electrolytic cell electrode plate to be evaluated includes: Based on the single-phase flow model equation and convection-diffusion equation in the multiphysics finite element model, step-by-step iterative calculations are performed to obtain the bubble volume fraction distribution and liquid velocity distribution. The current density distribution is calculated based on the electrolytic cell plate voltage, the minimum voltage at which the electrolysis reaction occurs, the current of the catalytic electrode, and the single-phase flow model equation. The temperature field distribution is calculated based on the single-phase flow model equation, the convection-diffusion equation, the constant-pressure heat capacity of the electrolyte, the thermal conductivity of the electrolyte, and the heat source quantity.

3. The method for evaluating the electrode structure of an electrolytic cell according to claim 2, characterized in that, The equations for the single-phase flow model are as follows: Among them, u l It is the electrolyte velocity, ρ l It is the liquid density, φ l It is the liquid volume fraction; p is the pressure; K is the viscous stress tensor; K m Where is the diffusion stress; g is the gravitational acceleration; the convection-diffusion equation is as follows: Where, ρ g =1-ρ l It is the volume fraction of bubbles, D eff R' is the equivalent diffusion coefficient of the gas, and R' represents the effect of the bubble generation rate on the bubble volume fraction.

4. The method for evaluating the electrode structure of an electrolytic cell according to claim 3, characterized in that, The calculation of current density distribution based on the electrolytic cell electrode voltage, the minimum voltage at which the electrolysis reaction occurs, the current at the catalytic electrode, and the single-phase flow model equation includes: Given the electrode voltage of the electrolyzer, the equivalent exchange current density of the catalytic electrode is obtained based on the current of the cathode catalytic electrode and the bubble volume fraction obtained from the single-phase flow model equation. Based on the reaction current of the cathode catalytic electrode, the contact resistance between the cathode plate and the cathode catalytic electrode, the resistance of the cathode plate, the resistance of the diaphragm, and the ohmic overpotential, a first function for the current density distribution is constructed. Based on the electrode voltage of the electrolytic cell, the minimum voltage at which the electrolytic reaction occurs, the ohmic overpotential, and the polarization overpotential of the cathode electrochemical reaction, a second function for the current density distribution is constructed. Based on the equivalent exchange current density of the cathode catalytic electrode, the transfer coefficient of the cathode plate, the number of electrons transferred in the electrolysis reaction, the polarization overpotential of the electrochemical reaction of the cathode plate, the electrolyte temperature, and the reaction current of the cathode catalytic electrode, a third function of current density distribution is constructed. The current density distribution is obtained based on the first current density distribution function, the second current density distribution function, and the third current density distribution function.

5. The method for evaluating the electrode structure of an electrolytic cell according to claim 4, characterized in that, The second function of the current density distribution is as follows: The first function of current density distribution is as follows: η ohm =i(r c +r p +r d ) The third function of current density distribution is as follows: Among them, E cell This refers to the voltage across the electrolytic cell electrodes. It is the minimum voltage at which the electrolysis reaction occurs, η phm It is an ohmic overpotential, η A and η c These are the polarization overpotentials of the cathode and anodic electrochemical reactions, respectively; ΔG is the Gibbs free energy change; z is the number of electrons transferred in the electrolysis reaction; F is the Faraday constant; i is the current density, r c It is the contact resistance between the bipolar plate and the catalytic electrode, r p It is the resistance of the electrode, r d It is the resistance of the diaphragm; i eA i eC It is the equivalent exchange current density of the cathode catalytic electrode and the anode catalytic electrode; α A is the transfer coefficient of the cathode plate, T is the electrolyte temperature, and R is the ideal gas constant.

6. The method for evaluating the structure of electrolytic cell electrodes according to claim 4, characterized in that, The process of obtaining the current density distribution based on the first current density distribution function, the second current density distribution function, and the third current density distribution function includes: The boundary heat source is obtained based on electrode potential, liquid volume fraction, equilibrium potential of electrolysis reaction, local reaction current density, and electrolyte temperature. The ohmic heat density in the chamber is obtained based on the reaction current of the electrode, the electrode potential, the reaction current of the electrolyte, the electrode potential, and the electrode liquid potential. Based on the boundary heat source and ohmic heat density, the amount of heat source provided by the electrolytic reaction is obtained. The temperature field distribution is obtained based on the liquid density, the constant-pressure heat capacity of the electrolyte, the liquid velocity, the thermal conductivity of the electrolyte, and the heat source provided by the electrolysis reaction.

7. The method for evaluating the structure of electrolytic cell plates according to any one of claims 1 to 6, characterized in that, The evaluation of the structure of the electrolytic cell electrode plate based on the multiphysics field distribution results includes: Based on the bubble volume fraction distribution, current density distribution and temperature field distribution in the multiphysics field distribution results, the highest bubble volume fraction value, the highest current density value and the highest temperature within the set area are obtained respectively. If the highest bubble volume fraction value is higher than the preset bubble volume fraction threshold, or the highest current density value is higher than the preset current density threshold, or the temperature difference between the highest temperature and the inlet temperature is higher than the preset temperature difference threshold, the structural evaluation result of the electrolytic cell electrode plate to be evaluated is determined to be unqualified.

8. An apparatus for evaluating the structure of electrode plates in an electrolytic cell, characterized in that, The apparatus for evaluating the electrode structure of the electrolytic cell includes: The finite element model construction module is used to construct a multiphysics model based on an alkaline electrolyzer including the electrode plates of the electrolyzer to be evaluated, and to perform finite element meshing on the multiphysics model to obtain a multiphysics finite element model. The first simplification module is used to, based on statistics of the diameter of bubbles generated during the electrolysis process of industrial alkaline electrolyzers, set up to treat bubbles as particles when calculating the volume distribution of bubbles in a small chamber using the multiphysics finite element model. The second simplification module is used to set homogeneous flow in the multiphysics finite element model based on the characteristic that the industrial alkaline electrolyzer uses an alkaline pump to force convection of the electrolyte and the gas movement is affected by the alkaline flow. The third simplification module is used to set the radial velocity in the running speed of the bubbles generated during the electrolysis process of the industrial alkaline electrolyzer on the surface of the electrolyzer electrode to be ignored in the multiphysics finite element model. The model parameter setting module is used to set the single-phase flow model equations for describing the electrolyte flow using single-phase flow for each finite element mesh in the multiphysics finite element model, based on equating bubbles to particles and using homogeneous flow, and the convection-diffusion equations for describing bubble motion using convection-diffusion. The structural design evaluation module is used to perform step-by-step iterative calculations on the multiphysics finite element model, obtain the multiphysics distribution results of the electrolytic cell electrode plate to be evaluated, and evaluate the structure of the electrolytic cell electrode plate to be evaluated based on the multiphysics distribution results.

9. A storage medium, characterized in that, A program or instruction is stored on a storage medium, and the program or instruction is executed by a processor to implement the steps of the method for evaluating the electrode structure of an electrolytic cell as described in any one of claims 1 to 7.

10. An electronic device comprising a memory, a processor, and a computer program stored in the memory and executable on the processor, characterized in that, When the processor executes the program, it implements the steps of the method for evaluating the electrode structure of an electrolytic cell as described in any one of claims 1 to 7.

Images