Method and apparatus for optimizing operating conditions of a proton exchange membrane fuel cell

Abstract

The application relates to the technical field of fuel cells, and provides a method and device for optimizing operation conditions of a proton exchange membrane fuel cell. The method comprises the following steps: simulating the proton exchange membrane fuel cell according to a local dimension-reduced single-cell model of the proton exchange membrane fuel cell and initial operation conditions, to obtain initial effective output power; sequentially increasing each initial parameter value under the initial operation conditions to obtain target operation conditions; again simulating the proton exchange membrane fuel cell according to the target operation conditions and the local dimension-reduced single-cell model, to obtain a target saturation degree of liquid water in a cathode catalyst layer and target effective output power; and obtaining a performance evaluation value corresponding to the target operation conditions according to the initial effective output power, the target effective output power and the target saturation degree of liquid water in the cathode catalyst layer, so as to determine the target operation conditions corresponding to the performance evaluation value as optimal operation conditions. The method can improve the precision of the performance evaluation value, and further improve the optimization effect of the operation conditions.

Description

Technical Field

[0001] The present application relates to the field of fuel cell technology, and in particular to a method, apparatus, computer equipment, computer-readable storage medium, and computer program product for optimizing operating conditions of a proton exchange membrane fuel cell. Background Art

[0002] In terms of hydrogen energy applications, proton exchange membrane fuel cells are a key technology for utilizing hydrogen energy. As altitude increases, atmospheric pressure and temperature decrease, causing proton exchange membrane fuel cells to operate in a low-pressure, low-temperature environment, which reduces fuel cell performance. Pressurizing and preheating the reaction gases is typically used to increase the output voltage of the fuel cell, but this increases the fuel cell's pumping and gas preheating losses. Therefore, before proton exchange membrane fuel cells for power generation can be widely promoted, the issue of fuel cell adaptability to plateau environments is one of the technical challenges that needs to be addressed.

[0003] Currently, one-dimensional or three-dimensional models can be used to simulate PEM fuel cells for power generation in plateau regions, and operating conditions can be optimized based on performance evaluation values ​​that assess the overall performance of the PEM fuel cell. However, traditional PEM fuel cell operating condition optimization methods are limited to evaluating the overall performance of the PEM fuel cell based on output voltage, and fail to consider the additional losses caused by pressurizing and preheating the reactant gases, as well as fuel cell flooding. This results in low performance evaluation accuracy, which in turn affects the effectiveness of operating condition optimization. Summary of the Invention

[0004] Based on this, it is necessary to provide a method, device, computer equipment, computer-readable storage medium and computer program product for optimizing the operating conditions of a proton exchange membrane fuel cell in response to the above technical problems.

[0005] In a first aspect, the present application provides a method for optimizing operating conditions of a proton exchange membrane fuel cell, comprising:

[0006] Simulating the proton exchange membrane fuel cell according to a local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell to obtain an initial effective output power; the initial operating conditions including at least one of an initial altitude parameter, an initial inlet reactant gas temperature parameter, and an initial inlet pressure parameter;

[0007] The initial parameter values ​​under the initial operating conditions are increased in sequence to obtain the target operating conditions;

[0008] The proton exchange membrane fuel cell is simulated again according to the target operating conditions and the local dimensionality reduction single cell model to obtain the target saturation of liquid water in the cathode catalyst layer and the target effective output power;

[0009] Obtaining a performance evaluation value corresponding to a target operating condition according to the initial effective output power, the target effective output power, and the target saturation of liquid water in the cathode catalyst layer;

[0010] When the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value, the target operating condition corresponding to the performance evaluation value is determined to be the optimal operating condition.

[0011] In one embodiment, before simulating the proton exchange membrane fuel cell based on the local reduced-dimensionality single cell model and initial operating conditions of the proton exchange membrane fuel cell, the method further includes:

[0012] The gas channels, gas diffusion layers, and extended layers in the anode and cathode of the proton exchange membrane fuel cell are modeled as a three-dimensional computational domain.

[0013] The microporous layer, catalytic layer and proton exchange membrane in the proton exchange membrane fuel cell are modeled into a one-dimensional computational domain;

[0014] A local dimensionality reduction single cell model of a proton exchange membrane fuel cell is obtained according to the three-dimensional calculation domain and the one-dimensional calculation domain.

[0015] In one embodiment, simulating the proton exchange membrane fuel cell based on the local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell to obtain the initial effective output power includes:

[0016] Based on the local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell, the proton exchange membrane fuel cell is simulated to obtain the initial output power, initial pumping loss power and initial gas preheating loss power;

[0017] Obtaining an initial total power loss according to the initial pumping power loss and the initial gas preheating power loss;

[0018] An initial effective output power is obtained according to a difference between the initial output power and the initial total power loss.

[0019] In one embodiment, obtaining the initial pumping power loss includes:

[0020] Obtaining an initial anode pressure difference based on a simulated inlet gas pressure of the fuel cell flow channel anode and an initial inlet pressure parameter in the initial operating condition;

[0021] Obtaining an initial cathode pressure difference value based on a simulated inlet gas pressure of a cathode of a fuel cell flow channel and an initial inlet pressure parameter in an initial operating condition;

[0022] Obtaining an initial anode gas delivery power according to the simulated anode inlet gas mass flow rate and the initial anode pressure difference;

[0023] Obtaining an initial cathode gas delivery power according to the simulated cathode inlet gas mass flow rate and the initial cathode pressure difference;

[0024] Obtaining a total gas delivery power according to the initial anode gas delivery power and the initial cathode gas delivery power;

[0025] The initial pump gas loss power is obtained according to the total gas delivery power and the simulated pump efficiency.

[0026] In one embodiment, obtaining the initial gas preheating power loss includes:

[0027] Obtaining an initial anode temperature difference based on a simulated inlet gas temperature of the fuel cell flow channel anode and an initial inlet reaction gas temperature parameter in the initial operating condition;

[0028] Obtaining an initial cathode temperature difference based on a simulated inlet gas temperature of a fuel cell flow channel cathode and an initial inlet reaction gas temperature parameter in an initial operating condition;

[0029] Obtaining initial anode gas preheating power loss according to the initial anode temperature difference, the anode inlet simulated gas mass flow rate, and the simulated anode proportional constant;

[0030] Obtaining the initial cathode gas preheating loss power according to the initial cathode temperature difference, the cathode inlet simulated gas mass flow rate, and the simulated cathode proportional constant;

[0031] The initial gas preheating loss power is obtained according to the initial anode gas preheating loss power and the initial cathode gas preheating loss power.

[0032] In one embodiment, obtaining a performance evaluation value corresponding to a target operating condition according to the initial effective output power, the target effective output power, and the target saturation of liquid water in the cathode catalyst layer includes:

[0033] Obtaining a liquid water threshold saturation of the cathode catalyst layer and a weight index of the liquid water saturation of the cathode catalyst layer;

[0034] Obtaining a cathode catalyst layer liquid water saturation influence coefficient according to the cathode catalyst layer liquid water threshold saturation, the cathode catalyst layer liquid water saturation weight index, and the cathode catalyst layer liquid water target saturation;

[0035] According to the ratio of the initial effective output power to the target effective output power and the liquid water saturation influence coefficient of the cathode catalyst layer, a performance evaluation value corresponding to the target operating condition is obtained.

[0036] In a second aspect, the present application also provides a device for optimizing the operating conditions of a proton exchange membrane fuel cell, comprising:

[0037] an initial simulation module for simulating the proton exchange membrane fuel cell based on a local dimensionality reduction single cell model of the proton exchange membrane fuel cell and initial operating conditions to obtain an initial effective output power; the initial operating conditions including at least one of an initial altitude parameter, an initial inlet reactant gas temperature parameter, and an initial inlet pressure parameter;

[0038] A target operating condition acquisition module is used to sequentially increase the initial parameter values ​​under the initial operating conditions to obtain the target operating conditions;

[0039] a re-simulation module for re-simulating the proton exchange membrane fuel cell according to the target operating conditions and the local dimensionality reduction single cell model to obtain a target saturation of liquid water in the cathode catalyst layer and a target effective output power;

[0040] a performance evaluation value acquisition module, configured to obtain a performance evaluation value corresponding to a target operating condition according to the initial effective output power, the target effective output power, and the target saturation of liquid water in the cathode catalyst layer;

[0041] The optimal operating condition determination module is used to determine that the target operating condition corresponding to the performance evaluation value is the optimal operating condition when the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value.

[0042] In a third aspect, the present application further provides a computer device comprising a memory and a processor, wherein the memory stores a computer program and the processor executes the above method.

[0043] In a fourth aspect, the present application further provides a computer-readable storage medium having a computer program stored thereon, wherein the computer program is used by a processor to execute the above method.

[0044] In a fifth aspect, the present application further provides a computer program product, wherein the computer program product includes a computer program, and the computer program is executed by a processor to execute the above method.

[0045] The above-mentioned optimization method, device, computer equipment, computer-readable storage medium and computer program product for the operating conditions of the proton exchange membrane fuel cell simulate the proton exchange membrane fuel cell according to the local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell to obtain the initial effective output power; the initial operating conditions include at least one of the initial altitude parameter, the initial inlet reaction gas temperature parameter and the initial inlet pressure parameter; the values ​​of each initial parameter under the initial operating conditions are increased in sequence to obtain the target operating conditions; according to the target operating conditions and the local dimensionality reduction single cell model, the proton exchange membrane fuel cell is simulated again to obtain the target saturation of liquid water in the cathode catalyst layer and the target effective output power; according to the initial effective output power, the target effective output power and the target saturation of liquid water in the cathode catalyst layer, the performance evaluation value corresponding to the target operating condition is obtained; when the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value, the target operating condition corresponding to the performance evaluation value is determined to be the optimal operating condition. When evaluating the comprehensive performance of proton exchange membrane fuel cells, the present application fully considers the additional losses caused by pressurizing and preheating the reaction gas, thereby obtaining the initial effective output power and the target effective output power; based on the initial effective output power, the target effective output power and the target saturation of liquid water in the cathode catalyst layer, the performance evaluation value corresponding to the target operating conditions is obtained, and the problem of fuel cell flooding is further considered; in summary, the evaluation of the comprehensive performance of proton exchange membrane fuel cells in the present application is not limited to the output voltage. Taking into account the additional losses caused by pressurizing and preheating the reaction gas and the problem of fuel cell flooding, the accuracy of the performance evaluation value can be improved, thereby improving the optimization effect of the operating conditions. BRIEF DESCRIPTION OF THE DRAWINGS

[0046] In order to more clearly illustrate the technical solutions in the embodiments of the present application or related technologies, the following briefly introduces the drawings required for use in the embodiments of the present application or related technical descriptions. Obviously, the drawings described below are only some embodiments of the present application. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without paying any creative work.

[0047] Figure 1 A diagram illustrating an application environment of a method for optimizing operating conditions of a proton exchange membrane fuel cell according to an embodiment;

[0048] Figure 2 Schematic diagram of a process for optimizing operating conditions of a proton exchange membrane fuel cell in one embodiment;

[0049] Figure 3 In one embodiment, the activation area is 451.5 cm 2 Schematic diagram of the computational domain of a single proton exchange fuel cell for power generation;

[0050] Figure 4 Schematic diagram of a curve showing changes in atmospheric temperature and pressure with altitude in one embodiment;

[0051] Figure 5 Schematic diagram showing the change of output voltage with reaction gas inlet temperature in one embodiment;

[0052] Figure 6 Schematic diagram showing the change of output voltage with reaction gas inlet pressure in one embodiment;

[0053] Figure 7 Schematic diagram showing the change of performance evaluation value with reaction gas inlet temperature in one embodiment;

[0054] Figure 8 Schematic diagram showing the change of performance evaluation value with reaction gas inlet pressure in one embodiment;

[0055] Figure 9 A structural block diagram of a device for optimizing operating conditions of a proton exchange membrane fuel cell according to one embodiment;

[0056] Figure 10 FIG. 1 is a diagram showing the internal structure of a computer device in one embodiment. DETAILED DESCRIPTION

[0057] In order to make the purpose, technical solutions and advantages of this application more clear, the following further describes this application in detail with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain this application and are not intended to limit this application.

[0058] It should be noted that the terms "including" and "having" and any variations thereof used in this application are intended to cover non-exclusive inclusions. The term "plurality" used in this application refers to two or more. The term "and / or" used in this application refers to one or more solutions.

[0059] The method for optimizing the operating conditions of a proton exchange membrane fuel cell provided in the embodiments of the present application can be applied to Figure 1In the application environment shown, terminal 102 communicates with server 104 via a network. A data storage system can store data that server 104 needs to process. The data storage system can be integrated on server 104, or placed on a cloud or other network server. Terminal 102 can simulate a proton exchange membrane fuel cell based on a local dimensionality reduction single cell model of the proton exchange membrane fuel cell and initial operating conditions to obtain an initial effective output power. Initial parameter values ​​under the initial operating conditions can be sequentially increased to obtain target operating conditions. Based on the target operating conditions and the local dimensionality reduction single cell model, the proton exchange membrane fuel cell can be simulated again to obtain a target saturation of liquid water in the cathode catalyst layer and a target effective output power to obtain a performance evaluation value corresponding to the target operating condition. When the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value, the target operating condition corresponding to the performance evaluation value is determined to be the optimal operating condition. Terminal 102 can be, but is not limited to, various personal computers, laptops, smartphones, tablets, drones, low-altitude aircraft, Internet of Things devices, and portable wearable devices. The server 104 may be an independent physical server, a server cluster or a distributed system composed of multiple physical servers, or a cloud server that provides cloud computing services.

[0060] In an exemplary embodiment, Figure 2 As shown, a method for optimizing the operating conditions of a proton exchange membrane fuel cell is provided. Figure 1 The terminal 102 in the example is used as an example to illustrate the process, including the following steps S201 to S205.

[0061] Step S201 , simulating the proton exchange membrane fuel cell based on a local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell to obtain an initial effective output power; the initial operating conditions include at least one of an initial altitude parameter, an initial inlet reaction gas temperature parameter, and an initial inlet pressure parameter.

[0062] According to the modeling software, a local dimensionality reduction single cell model of a proton exchange membrane fuel cell can be established. The local dimensionality reduction single cell model of a proton exchange membrane fuel cell is suitable for power generation scenarios in plateau areas and can be used for activation areas exceeding 450cm 2 Efficient and accurate simulation of proton exchange membrane fuel cells for power generation in plateau areas.

[0063] The initial operating conditions can be set according to actual conditions. For example, the initial operating conditions can be set as an initial altitude parameter of 2000m, an initial inlet reaction gas temperature parameter of 285.15K, and an initial inlet pressure parameter of 80.3kPa.

[0064] The proton exchange membrane fuel cell can be simulated according to a local reduced dimension single cell model of the proton exchange membrane fuel cell and initial operation conditions to obtain initial output power, initial pumping loss power and initial gas preheating loss power of the proton exchange membrane fuel cell under the initial operation conditions; and the initial effective output power can be obtained according to the initial output power, the initial pumping loss power and the initial gas preheating loss power.

[0065] In step S202, each initial parameter value under the initial operation conditions is sequentially increased to obtain target operation conditions.

[0066] For example, when the initial operation conditions are that the initial altitude parameter is 2000 m, the initial inlet reaction gas temperature parameter is 285.15 K and the initial inlet pressure parameter is 80.3 kPa, the initial inlet reaction gas temperature parameter under the initial operation conditions is increased to obtain target operation conditions that the target altitude parameter is 2000 m, the target inlet reaction gas inlet temperature parameter is 305.15 K and the target inlet pressure parameter is 80.3 kPa.

[0067] After the target operation conditions are obtained, the target inlet pressure under the target operation conditions can be increased to obtain another target operation condition that the target altitude parameter is 2000 m, the target inlet reaction gas inlet temperature parameter is 305.15 K and the target inlet pressure parameter is 100.3 kPa. Similarly, a plurality of target operation conditions can be obtained.

[0068] In step S203, the proton exchange membrane fuel cell is simulated again according to the target operation conditions and the local reduced dimension single cell model to obtain a target saturation degree of liquid water in a cathode catalyst layer and a target effective output power.

[0069] For each target operation condition, the proton exchange membrane fuel cell can be simulated again according to the target operation conditions and the local reduced dimension single cell model to obtain a target saturation degree of liquid water in a cathode catalyst layer, a target output power, a target pumping loss power and a target gas preheating loss power of the proton exchange membrane fuel cell under the target operation conditions; and the target effective output power can be obtained according to the target output power, the target pumping loss power and the target gas preheating loss power.

[0070] In step S204, a performance evaluation value corresponding to the target operation conditions is obtained according to the initial effective output power, the target effective output power and the target saturation degree of liquid water in the cathode catalyst layer.

[0071] The saturation degree influence coefficient of liquid water in the cathode catalyst layer can be obtained according to the target saturation degree of liquid water in the cathode catalyst layer; and the performance evaluation value corresponding to the target operation conditions can be obtained according to a ratio of the initial effective output power to the target effective output power and the saturation degree influence coefficient of liquid water in the cathode catalyst layer.

[0072] Step S205 : When the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value, determining that the target operating condition corresponding to the performance evaluation value is the optimal operating condition.

[0073] When the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value, it indicates that the comprehensive performance of the proton exchange membrane fuel cell under the target operating condition corresponding to the performance evaluation value is the best. At this time, it can be determined that the target operating condition corresponding to the performance evaluation value is the optimal operating condition.

[0074] In the above-mentioned method for optimizing the operating conditions of the proton exchange membrane fuel cell, the additional losses caused by pressurizing and preheating the reaction gas are fully taken into account when evaluating the comprehensive performance of the proton exchange membrane fuel cell, thereby obtaining the initial effective output power and the target effective output power; based on the initial effective output power, the target effective output power and the target saturation of liquid water in the cathode catalyst layer, the performance evaluation value corresponding to the target operating condition is obtained, and the fuel cell flooding problem is further taken into account; in summary, the evaluation of the comprehensive performance of the proton exchange membrane fuel cell in this embodiment is not limited to the output voltage. Taking into account the additional losses caused by pressurizing and preheating the reaction gas and the fuel cell flooding problem, the accuracy of the performance evaluation value can be improved, thereby improving the optimization effect of the operating conditions.

[0075] In one embodiment, before simulating the proton exchange membrane fuel cell based on the local reduced-dimensionality single-cell model and initial operating conditions of the proton exchange membrane fuel cell, the method provided in the present application also includes: modeling the gas channel, gas diffusion layer, and extended layer in the anode and cathode in the proton exchange membrane fuel cell as a three-dimensional computational domain; modeling the microporous layer, catalytic layer, and proton exchange membrane in the proton exchange membrane fuel cell as a one-dimensional computational domain; and obtaining the local reduced-dimensionality single-cell model of the proton exchange membrane fuel cell based on the three-dimensional computational domain and the one-dimensional computational domain.

[0076] Using modeling software, the gas channels, gas diffusion layers, and extended layers in the anode and cathode of a proton exchange membrane fuel cell can be modeled as a three-dimensional computational domain. The microporous layer, catalyst layer, and proton exchange membrane in the proton exchange membrane fuel cell can be modeled as a one-dimensional computational domain, composed of internal surface nodes belonging to the anode and cathode. Based on the three-dimensional and one-dimensional computational domains, a localized, reduced-dimensional single-cell model of the proton exchange membrane fuel cell can be obtained. The extended layer can serve as a data storage layer in the one-dimensional computational domain, connecting the anode and cathode.

[0077] Activation area 451.5cm 2 The computational domain of a proton exchange fuel cell for power generation is as follows: Figure 3 shown.

[0078] In the one-dimensional computational domain, conservation equations for components and energy are simplified to flux conservation equations. Flux conservation equations related to the catalyst layer and proton exchange membrane, such as electrochemical reactions and membrane water, are also solved in the one-dimensional sub-model. All equations within the one-dimensional computational domain are solved using user-defined functions. At each iteration, the scalar values ​​solved in the three-dimensional computational domain provide boundary conditions for the one-dimensional domain. Simultaneously, the solutions in the one-dimensional domain provide the required physical parameters and source terms for the three-dimensional domain, enabling data exchange between the two computational domains.

[0079] The specific steps for solving the local dimensionality reduction single cell model of the proton exchange membrane fuel cell are as follows:

[0080] 1. The fuel cell's internal conservation equations for mass, momentum, composition, energy, liquid pressure, liquid water saturation, and electron potential are solved in a three-dimensional computational domain. The mass, momentum, composition, and energy conservation equations are solved using the modeling software's built-in equations, while the liquid water and electron potential conservation equations are solved using user-defined functions.

[0081] 1.1. Solution of liquid water saturation equation:

[0082] In view of the small characteristic size of the fuel cell flow channel, the transmission of liquid water in the flow channel is regarded as occurring in the porous medium. The gas-liquid velocity ratio is derived with the help of Darcy's law of two phases as shown in Equation (1), and the liquid water saturation conservation equation as shown in Equation (2) is corrected.

[0083] (1)

[0084] in, Indicates the gas surface velocity in m / s (meters per second). Indicates the surface velocity of liquid water in m / s (meters per second), Indicates the kinematic viscosity of the gas, in m 2 / s (square meters / second), Indicates the kinematic viscosity of liquid water, in m 2 / s (square meters / second), represents the relative permeability of liquid water, represents the relative permeability of gas, Indicates liquid saturation, subscript g indicates gas, lw indicates liquid water, An empirical constant that quantifies the nonlinear relationship between relative permeability and saturation, used to describe the effect of porous media properties on gas-liquid two-phase flow. The common value range is 2.0~3.0.

[0085] (2)

[0086] in, represents the gradient, Indicates the density of liquid water in kg / m 3 (kg / m3), Indicates the kinematic viscosity of liquid water, in m / s (meters per second), Indicates the liquid saturation, represents the liquid water diffusion coefficient, in m 2 / s (square meters / second), represents the gradient of liquid saturation, Represents the hydraulic source term, unit is kg / (m 3 s)(kg / (m3 Second)).

[0087] 1.2. Solving the liquid pressure equation:

[0088] (3)

[0089] in, represents the gradient, Indicates the density of liquid water in kg / m 3 (kg / m3), K represents the absolute permeability, represents the relative permeability of liquid water, Indicates the kinematic viscosity of liquid water, in Pa s (Pascal Second), Represents the pressure source term, the unit is Pa (Pascal), Represents the hydraulic source term, unit is kg / (m 3 s)(kg / (m3 Second)), Represents the gradient of the pressure source term.

[0090] 1.3. Solving the electron potential equation:

[0091] (4)

[0092] in, represents the gradient, Indicates effective electronic conductivity, the unit is S / m (Siemens / meter), Represents the electron potential, the unit is V (volt), Represents the electron potential source term, in A / m 3 (ampere / cubic meter), the subscript ele represents electricity, and the superscript eff represents effective value.

[0093] The conservation equations above are partial differential equations, solved using the finite volume method. The finite volume method is first used to discretize the conservation equations, dividing the entire computational domain into several control volumes (grid cells). The corresponding conservation equations are then solved within each control volume. During the solution, the partial differential equations within the grid cells are converted into linear algebraic equations. These equations are then solved incrementally using an iterative method, with each iteration updating the conservation equations' variables, such as flow rate, pressure, temperature, and concentration, until convergence criteria are met.

[0094] 2. In the one-dimensional computational domain, the conservation equations for gas component concentration, temperature, and hydraulic pressure solved in step (1) are converted into flux equations for one-dimensional nodes. In addition, equations related to the catalyst layer and proton exchange membrane, such as electrochemical reactions and membrane water, are also described as flux equations. In the flux equation, only the diffusion effect along the thickness direction is considered.

[0095] 2.1. Solving the component equation:

[0096] (5)

[0097] 2.2 Solving the temperature equation:

[0098] (6)

[0099] 2.3. Solution of hydraulic equations:

[0100] (7)

[0101] 2.4. Solution of membrane water content equation:

[0102] (8)

[0103] 2.5. Solving the electron potential equation:

[0104] (9)

[0105] 2.6. Solving the ionic potential equation:

[0106] (10)

[0107] Where n = 0 and n = 1 represent two adjacent layers, respectively. When solving in the microporous layer, 0 represents the one-dimensional node at the interface between the gas diffusion layer and the microporous layer, and 1 represents the one-dimensional node at the interface between the microporous layer and the catalytic layer. When solving in the catalytic layer, 0 represents the one-dimensional node at the interface between the microporous layer and the catalytic layer, and 1 represents the one-dimensional node at the interface between the microporous layer and the proton exchange membrane. represents the effective diffusion coefficient length of component i in layer n, in m 2 / s (square meters / second), Indicates the thickness of the nth layer, in m (meters), It represents the gas molar concentration of component i in the n+1th layer, in mol / m 3 (mole / m3), It represents the gas molar concentration of component i in the nth layer, in mol / m 3 (mole / m3), represents the mass source term of component i in the nth layer, in mol / (m 3 s)(mol / (m3 Second)); represents the effective thermal conductivity of component i in the nth layer, in W / (m K)(W / (m Kelvin)), represents the temperature of the n+1th layer in K (Kelvin), represents the temperature of the nth layer in K (Kelvin), Represents the heat source term of the nth layer, in W / m 3 (watts per cubic meter); Indicates the density of liquid water in kg / m 3 (kg / m3), represents the absolute permeability of the nth layer, represents the relative permeability of liquid water in the nth layer, represents the kinematic viscosity of liquid water in the nth layer, in m / s (meters per second), Represents the pressure source term of the n+1th layer, in Pascals. Represents the pressure source term of the n+1th layer, with the unit being Pa (Pascal); Indicates the density of the ionomer in kg / m 3 (kg / m3), Represents the diffusion coefficient of membrane water, unit is m 2 / s (square meters / second), It represents the equivalent weight of dry ionomer in kg / mol (kilograms / mole). represents the membrane water content of the n+1th layer, represents the membrane water content of the nth layer, Represents the membrane water source term of the nth layer, in mol / (m 3 s)(mol / (volume time)); represents the effective electronic conductivity of the nth layer, in S / m (Siemens / meter), V (Volt), represents the electronic potential of the n+1th layer, V (Volt), represents the electronic potential of the n+1th layer, A / m, represents the electronic source term of the n+1th layer, 3 (Ampere / cubic meter), S / m, represents the effective ionic conductivity of the n+1th layer, V (Volt), represents the ionic potential of the n+1th layer, V (Volt), represents the ionic potential of the n+1th layer, A / m, represents the ionic source term of the n+1th layer, 3 (Ampere / cubic meter), subscript im represents ionomer, ion represents ion, mw represents membrane water, i represents gas species, including hydrogen, oxygen, water vapor.

[0108] The flux equation in the one-dimensional computational domain is also solved step by step in each iteration step by the iterative method. The scalar value solved by the three-dimensional computational domain provides the boundary conditions for the one-dimensional computational domain, while at the same time, the one-dimensional computational domain solution provides the required physical parameters and source terms for the three-dimensional computational domain. The data exchange between the two computational domains is realized in each iteration step.

[0109] 3. The electrochemical reaction rate is calculated by the Butler-Volmer equation corrected by the agglomeration model:

[0110] (11)

[0111] (12)

[0112] wherein, A / m, represents the electrochemical reaction rate of the anode, 2 (Ampere / square meter), A / m, represents the electrochemical reaction rate of the cathode, 2 (Ampere / square meter), A / m, represents the anode exchange current density under reference conditions, 2 (Ampere / square meter), A / m, represents the cathode exchange current density under reference conditions, 2 (Ampere / square meter), m² / m³, (square meter / cubic meter), represents the specific area, represents the temperature correction coefficient of the anode, represents the temperature correction coefficient of the cathode, represents the universal gas constant, T represents absolute temperature, Indicates the hydrogen concentration in mol / m 3 (mole / m3), Indicates the hydrogen concentration under reference conditions, in mol / m 3 (mole / m3), Indicates the oxygen concentration under reference conditions, in mol / m 3 (mole / m3), Henry's constant for hydrogen, in Pa m³ / mol (Pascal cubic meters / mole), Indicates oxygen concentration in mol / m 3 (mole / m3), Henry's constant for oxygen, in Pa m³ / mol (Pascal cubic meters / mole), Indicates Henry's coefficient, unit is Pa m³ / mol (Pascal cubic meters / mole), Represents the Faraday constant, with the unit of C / mol (coulomb / mole), represents the anode transfer coefficient, Indicates the overpotential gas transport resistance of the anode, the unit is V (volt), represents the cathode transfer coefficient, Indicates the overpotential gas transport resistance of the cathode, in V (volts), Represents the local gas transport resistance, in Ω m² (Ohm square meters), It represents the interfacial area between the ionomer and the catalyst, with the unit of m² / m³ (square meters / cubic meter). The superscript ref represents the reference value, the subscript a represents the anode, c represents the cathode, pt represents the platinum loading, H2 represents hydrogen, and O2 represents oxygen.

[0113] In this example, , , , , , , , , the remaining relevant parameters are obtained in each iterative step of step (1) and step (2), so as to calculate the electrochemical reaction rate of the one-dimensional node.

[0114] Furthermore, the reversible voltage is obtained from the Nernst equation and expressed as:

[0115] (13)

[0116] in, Represents the reversible voltage, the unit is V (volt), It represents the entropy change of electrochemical reaction, with the unit of J / (mol K) (Joules / mole Kelvin), represents the universal gas constant, in J / (mol K) (Joules / mole Kelvin), Represents the Faraday constant, with the unit of C / mol (coulomb / mole), Indicates the inlet hydrogen pressure in Pa (Pascal), represents oxygen pressure in Pa (Pascal), T represents absolute temperature in K (Kelvin), Indicates the reference temperature in K (Kelvin), Indicates the reference pressure in Pa (Pascal). In this example, , , the remaining parameters are obtained in each iterative step of step (1) and step (2), so as to calculate the reversible voltage of the one-dimensional node of the fuel cell.

[0117] In this embodiment, a local dimensionality reduction single cell model of a proton exchange membrane fuel cell is established, which consists of a three-dimensional computational domain and a one-dimensional computational domain. Compared with the traditional one-dimensional model, the local dimensionality reduction model can truly reflect the actual physical processes inside the proton exchange membrane fuel cell, and reflect the impact of environmental changes in plateau areas on the internal reactions and mass transfer characteristics of the proton exchange membrane fuel cell. Compared with the traditional three-dimensional model, the local dimensionality reduction model has a reduced mesh size, which can improve computational efficiency and can perform efficient and accurate simulation of large-scale fuel cells for power generation.

[0118] In one embodiment, a proton exchange membrane fuel cell is simulated based on a local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell to obtain an initial effective output power. The specific steps are as follows: based on a local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell, the proton exchange membrane fuel cell is simulated to obtain an initial output power, an initial pumping loss power, and an initial gas preheating loss power; based on the initial pumping loss power and the initial gas preheating loss power, an initial total loss power is obtained; and based on the difference between the initial output power and the initial total loss power, an initial effective output power is obtained.

[0119] According to the local reduced dimension single cell model of the proton exchange membrane fuel cell and the initial operating condition, the proton exchange membrane fuel cell is simulated to obtain the simulation average current density, the simulation output voltage, the simulation active area, the simulation inlet gas pressure of the flow channel anode, the simulation inlet gas pressure of the flow channel cathode, the simulation inlet gas temperature of the flow channel anode and the simulation inlet gas temperature of the flow channel cathode of the proton exchange membrane fuel cell under the initial operating condition.

[0120] The initial output power of the proton exchange membrane fuel cell under the initial operating condition can be obtained according to the simulation average current density, the simulation output voltage and the simulation active area of the proton exchange membrane fuel cell under the initial operating condition, as shown in formula (14).

[0121] (14)

[0122] wherein, the initial output power is represented by P0, with the unit of W (watt), the simulation average current density is represented by I0, with the unit of A / m2 (ampere per square meter), the simulation output voltage is represented by U0, with the unit of V (volt), the simulation active area is represented by S0, with the unit of m2 (square meter). .

[0123] The initial pump loss power of the proton exchange membrane fuel cell under the initial operating condition can be obtained according to the simulation inlet gas pressure of the flow channel anode and the simulation inlet gas pressure of the flow channel cathode of the fuel cell flow channel.

[0124] The initial gas preheating loss power of the proton exchange membrane fuel cell under the initial operating condition can be obtained according to the simulation inlet gas temperature of the flow channel anode and the simulation inlet gas temperature of the flow channel cathode of the fuel cell flow channel.

[0125] The initial total loss power can be obtained according to the addition of the initial pump loss power and the initial gas preheating loss power; the initial effective output power can be obtained according to the result of subtracting the initial total loss power from the initial output power.

[0126] In this embodiment, the proton exchange membrane fuel cell is simulated according to the local reduced dimension single cell model of the proton exchange membrane fuel cell and the initial operating condition to obtain the initial output power, the initial pump loss power and the initial gas preheating loss power, so as to obtain the initial effective output power and prepare data for obtaining the performance evaluation value corresponding to the target operating condition.

[0127] ​​​In one embodiment, the initial pumping gas loss power is obtained, and the specific steps are as follows: an initial anode pressure difference is obtained based on the simulated inlet gas pressure of the anode of the fuel cell flow channel and the initial inlet pressure parameter in the initial operating conditions; an initial cathode pressure difference is obtained based on the simulated inlet gas pressure of the cathode of the fuel cell flow channel and the initial inlet pressure parameter in the initial operating conditions; an initial anode gas delivery power is obtained based on the simulated inlet gas mass flow rate of the anode and the initial anode pressure difference; an initial cathode gas delivery power is obtained based on the simulated inlet gas mass flow rate of the cathode and the initial cathode pressure difference; a total gas delivery power is obtained based on the initial anode gas delivery power and the initial cathode gas delivery power; and an initial pumping gas loss power is obtained based on the total gas delivery power and the simulated pump efficiency.

[0128] According to the simulated inlet gas pressure of the fuel cell flow channel anode and the initial inlet pressure parameter in the initial operating conditions , get the initial anode pressure difference ; According to the simulated inlet gas pressure of the fuel cell flow channel cathode and the initial inlet pressure parameter in the initial operating conditions , get the initial cathode pressure difference .

[0129] According to the simulated inlet gas mass flow rate of the anode and the initial anode pressure difference , and the initial anode gas delivery power is obtained ; According to the simulated cathode inlet gas mass flow and the initial cathode pressure difference , the initial cathode gas delivery power is obtained ; According to the initial anode gas delivery power and initial cathode gas delivery power The total gas delivery power is obtained by adding ; According to the total gas delivery power and simulated pump efficiency The ratio of is used to obtain the initial pump gas loss power, as shown in formula (15).

[0130] (15)

[0131] in, Indicates the initial pumping power loss, in W (watt), Indicates the simulated inlet gas pressure of the fuel cell flow channel anode, in Pa (Pascal), Indicates the initial inlet pressure parameter, the unit is Pa (Pascal), Indicates the simulated inlet gas pressure of the fuel cell flow channel cathode, in Pa (Pascal), represents the simulated inlet gas mass flow rate of the anode in kg / s (kilograms per second), represents the simulated cathode inlet gas mass flow rate in kg / s (kilograms per second), represents the pump efficiency, which is assumed to be 70%, and the subscripts a and c represent the anode and cathode, respectively.

[0132] In this embodiment, the initial anode pressure difference and the initial cathode pressure difference are obtained based on the simulated inlet gas pressure of the fuel cell flow channel anode, the simulated inlet gas pressure of the flow channel cathode and the initial inlet pressure parameters in the initial operating conditions; the initial anode gas delivery power and the initial cathode gas delivery power are obtained based on the simulated inlet gas mass flow rate of the anode, the simulated inlet gas mass flow rate of the cathode and the initial anode pressure difference to obtain the total gas delivery power; the initial pump gas loss power is obtained based on the total gas delivery power and the simulated pump efficiency, so as to quickly and accurately obtain the loss caused by pressurizing the reaction gas.

[0133] In one of the embodiments, the initial gas preheating loss power is obtained, and the specific steps are as follows: an initial anode temperature difference is obtained based on the simulated inlet gas temperature of the anode of the fuel cell flow channel and the initial inlet reaction gas temperature parameters in the initial operating conditions; an initial cathode temperature difference is obtained based on the simulated inlet gas temperature of the cathode of the fuel cell flow channel and the initial inlet reaction gas temperature parameters in the initial operating conditions; an initial anode gas preheating loss power is obtained based on the initial anode temperature difference, the simulated gas mass flow rate at the anode inlet and the simulated anode proportional constant; an initial cathode gas preheating loss power is obtained based on the initial cathode temperature difference, the simulated gas mass flow rate at the cathode inlet and the simulated cathode proportional constant; an initial gas preheating loss power is obtained based on the initial anode gas preheating loss power and the initial cathode gas preheating loss power.

[0134] According to the simulated inlet gas temperature of the fuel cell flow channel anode and the initial inlet reaction gas temperature parameter in the initial operating conditions , get the initial anode temperature difference ; According to the simulated inlet gas temperature of the fuel cell channel cathode and the initial inlet reaction gas temperature parameter in the initial operating conditions , get the initial cathode temperature difference ; According to the initial anode temperature difference , simulated gas mass flow rate at the anode inlet and simulated anode proportional constant , get the initial anode gas preheating power loss ; According to the initial cathode temperature difference , simulated gas mass flow rate at cathode inlet and simulated cathode proportional constant , get the initial cathode gas preheating loss power ; According to the sum of the initial anode gas preheating loss power and the initial cathode gas preheating loss power, the initial gas preheating loss power is obtained, as shown in formula (16).

[0135] (16)

[0136] in, Indicates the initial gas preheating power loss, in W (watt), represents the simulated inlet gas temperature of the fuel cell flow channel anode, in K (Kelvin), represents the initial inlet reaction gas temperature parameter, in K (Kelvin), represents the simulated inlet gas temperature of the fuel cell flow channel cathode, in K (Kelvin), represents the simulated anode proportional constant, Represents the simulated cathode proportional constant, and the subscripts H2 and O2 represent hydrogen and oxygen, respectively.

[0137] In this embodiment, the initial anode temperature difference and the initial cathode temperature difference are obtained based on the simulated inlet gas temperature of the fuel cell flow channel anode, the simulated inlet gas temperature of the flow channel cathode and the initial inlet reaction gas temperature parameters in the initial operating conditions; the initial anode gas preheating loss power is obtained based on the initial anode temperature difference, the simulated gas mass flow rate at the anode inlet and the simulated anode proportional constant; the initial cathode gas preheating loss power is obtained based on the initial cathode temperature difference, the simulated gas mass flow rate at the cathode inlet and the simulated cathode proportional constant, so as to obtain the initial gas preheating loss power, which can quickly and accurately obtain the loss caused by preheating the reaction gas.

[0138] In one of the embodiments, a performance evaluation value corresponding to the target operating condition is obtained based on the initial effective output power, the target effective output power and the target saturation of liquid water in the cathode catalyst layer. The specific steps are as follows: obtaining the threshold saturation of liquid water in the cathode catalyst layer and the weight index of the liquid water saturation of the cathode catalyst layer; obtaining the influence coefficient of liquid water saturation in the cathode catalyst layer based on the threshold saturation of liquid water in the cathode catalyst layer, the weight index of the liquid water saturation in the cathode catalyst layer and the target saturation of liquid water in the cathode catalyst layer; obtaining the performance evaluation value corresponding to the target operating condition based on the ratio of the initial effective output power to the target effective output power and the influence coefficient of the liquid water saturation in the cathode catalyst layer.

[0139] The liquid water threshold saturation of the cathode catalyst layer can be obtained and the weight index of liquid water saturation in the cathode catalyst layer ; According to the liquid water threshold saturation of the cathode catalyst layer , the weight index of liquid water saturation in the cathode catalyst layer and the target saturation of liquid water in the cathode catalyst layer , the influence coefficient of liquid water saturation in the cathode catalyst layer is obtained ; According to the initial effective output power and target effective output power The ratio of the cathode catalyst layer liquid water saturation coefficient , and obtain the performance evaluation value corresponding to the target operating conditions , as shown in formula (17).

[0140] (17)

[0141] in, Indicates the liquid water saturation of the fuel cell catalyst layer, is the weight index of liquid water saturation in the catalyst layer, which is assumed to be 2. The larger the value, the greater the risk of flooding the fuel cell is considered to face. The more significant the impact is, the When it is close to 1, the evaluation criteria It decreases rapidly to 0. The superscript 0 represents the initial parameter, and 1 represents the corresponding parameter when the fuel cell operating conditions change; represents the initial output power, Indicates the initial pumping power loss, represents the initial gas preheating power loss, Indicates the output power of the fuel cell when the operating conditions change, Indicates the pumping power loss when the fuel cell operating conditions change, Indicates the gas preheating power loss when the fuel cell operating conditions change.

[0142] In this embodiment, the additional losses caused by pressurizing and preheating the reaction gas are fully taken into account when evaluating the comprehensive performance of the proton exchange membrane fuel cell, thereby obtaining the initial effective output power and the target effective output power; based on the initial effective output power, the target effective output power and the target saturation of liquid water in the cathode catalyst layer, the performance evaluation value corresponding to the target operating conditions is obtained, and the problem of fuel cell flooding is further taken into account; in summary, the evaluation of the comprehensive performance of the proton exchange membrane fuel cell in this embodiment is not limited to the output voltage. Taking into account the additional losses caused by pressurizing and preheating the reaction gas and the problem of fuel cell flooding, the accuracy of the performance evaluation value can be improved, thereby improving the optimization effect of the operating conditions.

[0143] In order to better understand the above method, an application example of the method for optimizing the operating conditions of a proton exchange membrane fuel cell of the present application is described in detail below.

[0144] The application of hydrogen energy offers an effective solution to current energy challenges. Fuel cells are considered the most suitable power generation device for hydrogen utilization and have been a research hotspot for decades. Proton exchange membrane fuel cells (PEMFCs) are a key technology for hydrogen energy utilization, offering advantages such as high power density, silent operation, rapid dynamic response, zero emissions, and low operating temperatures. In addition to plains, plateaus also occupy large swathes of the Earth, such as the Qinghai-Tibet Plateau and the Pamir Plateau. With increasing altitude, atmospheric pressure and temperature decrease, resulting in PEMFCs operating in a low-pressure, low-temperature environment, which degrades fuel cell performance. Pressurizing and preheating the reactant gases is commonly used to increase the fuel cell's output voltage, but this incurs additional pumping and preheating losses. Therefore, before PEMFCs can be widely deployed for power generation, the adaptability of fuel cells to plateau environments remains a pressing technical challenge.

[0145] Currently, one-dimensional or three-dimensional models can be used to simulate PEM fuel cells used for power generation in plateau regions, thereby optimizing operating conditions. However, one-dimensional models cannot truly reflect the actual physical processes within PEM fuel cells, nor can they truly reflect the impact of environmental changes in plateau regions on the internal reactions and mass transfer characteristics of PEM fuel cells. Three-dimensional models have large mesh sizes and low computational efficiency, making them inefficient for efficient and accurate simulation of large-scale PEM fuel cells used for power generation. Furthermore, evaluation of the comprehensive performance of PEM fuel cells is limited to output voltage, without considering the additional losses caused by pressurizing and preheating the reactant gases, or the problem of fuel cell flooding. This results in low-precision performance evaluation values, which in turn affects the optimization of operating conditions.

[0146] In response to the above problems, this embodiment proposes a method for optimizing the operating conditions of proton exchange membrane fuel cells, which is suitable for power generation scenarios in plateau areas. A local dimensionality reduction single cell model of proton exchange membrane fuel cells for power generation in plateau areas can be established, which can be used for the optimization of the operating conditions of proton exchange membrane fuel cells with an activation area of ​​more than 450cm 2 Efficient and accurate simulation of fuel cells for power generation in high-altitude areas. By varying the operating conditions of PEMFCs for power generation in plateau regions, the effects of factors such as reactant gas inlet temperature and pressure on fuel cell output voltage, mass transfer characteristics, and hydrothermal management can be determined. A method for calculating the performance evaluation value of PEMFCs for power generation in plateau regions is provided. This method measures how the performance evaluation value changes with reactant gas inlet temperature and pressure, thereby enabling adaptive optimization of PEMFC operating conditions in plateau regions.

[0147] The embodiment provides a method for optimizing operation conditions of a proton exchange membrane fuel cell, and the specific implementation process is as follows.

[0148] I. Establishing a highland environment model. The environmental temperature and pressure of a highland region change with the altitude, and according to an international standard atmospheric model, a model for the change of temperature with the altitude is established as shown in formula (18).

[0149] (18)

[0150] A model for the change of pressure with the altitude is established as shown in formula (19).

[0151] (19)

[0152] wherein, Tin represents an inlet reaction gas temperature parameter, in the unit of K (Kelvin), Tin,0 represents an inlet reaction gas reference temperature parameter, in the unit of K (Kelvin), H represents an altitude, in the unit of m (meter), Pin represents an inlet pressure parameter, in the unit of Pa (Pascal), Pin,0 represents an inlet reference pressure parameter, in the unit of Pa (Pascal), , The change curves of the atmospheric temperature and pressure with the altitude in the example are shown in FIG. 1. Figure 4

[0153] II. According to a modeling software, the gas channel, the gas diffusion layer, the extended layer in the anode and the cathode in the proton exchange membrane fuel cell can be modeled as a three-dimensional calculation domain; the microporous layer, the catalytic layer and the proton exchange membrane in the proton exchange membrane fuel cell can be modeled as a one-dimensional calculation domain, which is composed of internal surface nodes belonging to the anode and the cathode; according to the three-dimensional calculation domain and the one-dimensional calculation domain, a local dimension-reduced single cell model of the proton exchange membrane fuel cell is obtained. The extended layer can be used as a data storage layer of the one-dimensional calculation domain, and plays a role in connecting the anode and the cathode.

[0154] The activation area of the power generation proton exchange fuel cell single cell calculation domain is 451.5 cm 2 . Figure 3

[0155] ​​In the one-dimensional computational domain, conservation equations for components and energy are simplified to flux conservation equations. Flux conservation equations related to the catalyst layer and proton exchange membrane, such as electrochemical reactions and membrane water, are also solved in the one-dimensional sub-model. All equations within the one-dimensional computational domain are solved using user-defined functions. At each iteration, the scalar values ​​solved in the three-dimensional computational domain provide boundary conditions for the one-dimensional domain. Simultaneously, the solutions in the one-dimensional domain provide the required physical parameters and source terms for the three-dimensional domain, enabling data exchange between the two computational domains.

[0156] The specific steps for solving the local dimensionality reduction single cell model of the proton exchange membrane fuel cell are as follows:

[0157] 1. The fuel cell's internal conservation equations for mass, momentum, composition, energy, liquid pressure, liquid water saturation, and electron potential are solved in a three-dimensional computational domain. The mass, momentum, composition, and energy conservation equations are solved using the modeling software's built-in equations, while the liquid water and electron potential conservation equations are solved using user-defined functions.

[0158] 1.1. Solution of liquid water saturation equation:

[0159] In view of the small characteristic size of the fuel cell flow channel, the transmission of liquid water in the flow channel is regarded as occurring in the porous medium. The gas-liquid velocity ratio is derived with the help of Darcy's law of two phases as shown in Equation (1), and the liquid water saturation conservation equation as shown in Equation (2) is corrected.

[0160] (1)

[0161] in, Indicates the gas surface velocity in m / s (meters per second). Indicates the surface velocity of liquid water in m / s (meters per second), Indicates the kinematic viscosity of the gas, in m 2 / s (square meters / second), Indicates the kinematic viscosity of liquid water, in m 2 / s (square meters / second), represents the relative permeability of liquid water, represents the relative permeability of gas, Indicates liquid saturation, the subscript g indicates gas, and lw indicates liquid water.

[0162] (2)

[0163] in, represents the gradient, Indicates the density of liquid water in kg / m 3(kg / m3), denotes the liquid water kinematic viscosity, in m / s (meter per second), denotes the liquid water saturation, denotes the liquid water diffusion coefficient, in m / s (meter per second), 2 denotes the gradient of the liquid water saturation, denotes the hydraulic source term, in kg / (m 3 s) (kilogram per (cubic meter second).

[0164] 1.2. Solution of the liquid pressure equation:

[0165] (3)

[0166] where, denotes the gradient, denotes the liquid water density, in kg / m 3 (kilogram per cubic meter), K denotes the absolute permeability, denotes the liquid water relative permeability, denotes the liquid water kinematic viscosity, in Pa s (pascal second), denotes the pressure source term, in Pa (pascal), denotes the hydraulic source term, in kg / (m 3 s) (kilogram per (cubic meter second), denotes the gradient of the pressure source term.

[0167] 1.3. Solution of the electronic potential equation:

[0168] (4)

[0169] where, denotes the gradient, denotes the electronic conductivity, in S / m (siemens per meter), denotes the electronic potential, in V (volt), denotes the electronic potential source term, in A / m 3 (ampere per cubic meter), subscript ele denotes electric, superscript eff denotes effective value.

[0170] ​The conservation equations above are partial differential equations, solved using the finite volume method. The finite volume method is first used to discretize the conservation equations, dividing the entire computational domain into several control volumes (grid cells). The corresponding conservation equations are then solved within each control volume. During the solution, the partial differential equations within the grid cells are converted into linear algebraic equations. These equations are then solved incrementally using an iterative method, with each iteration updating the conservation equations' variables, such as flow rate, pressure, temperature, and concentration, until convergence criteria are met.

[0171] 2. In the one-dimensional computational domain, the conservation equations for gas component concentration, temperature, and hydraulic pressure solved in step (1) are converted into flux equations for one-dimensional nodes. In addition, equations related to the catalyst layer and proton exchange membrane, such as electrochemical reactions and membrane water, are also described as flux equations. In the flux equation, only the diffusion effect along the thickness direction is considered.

[0172] 2.1. Solving the component equation:

[0173] (5)

[0174] 2.2 Solving the temperature equation:

[0175] (6)

[0176] 2.3. Solution of hydraulic equations:

[0177] (7)

[0178] 2.4. Solution of membrane water content equation:

[0179] (8)

[0180] 2.5. Solving the electron potential equation:

[0181] (9)

[0182] 2.6. Solving the ionic potential equation:

[0183] (10)

[0184] The flux equation in the one-dimensional computational domain is also solved incrementally at each iteration step using an iterative method. The scalar values ​​obtained in the three-dimensional computational domain provide boundary conditions for the one-dimensional domain. Simultaneously, the results from the one-dimensional domain provide the required physical parameters and source terms for the three-dimensional domain. Each iteration allows for data exchange between the two computational domains.

[0185] 3. The electrochemical reaction rate is calculated using the Butler–Volmer equation modified by the agglomeration model:

[0186] (11)

[0187] (12)

[0188] in, Indicates the electrochemical reaction rate of the anode, the unit is A / m 2 (amperes per square meter), Indicates the electrochemical reaction rate of the cathode, in A / m 2 (amperes per square meter), It represents the anodic exchange current density under reference conditions, in A / m 2 (amperes per square meter), Indicates the cathode exchange current density under reference conditions, in A / m 2 (amperes per square meter), Indicates specific area, the unit is m² / m³ (square meters / cubic meter). represents the temperature correction coefficient of the anode, represents the temperature correction coefficient of the cathode, represents the universal gas constant, T represents the absolute temperature, Indicates the hydrogen concentration in mol / m 3 (mole / m3), Indicates the hydrogen concentration under reference conditions, in mol / m 3 (mole / m3), Henry's constant for hydrogen, in Pa m³ / mol (Pascal cubic meters / mole), Indicates oxygen concentration in mol / m 3 (mole / m3), Henry's constant for oxygen, in Pa m³ / mol (Pascal cubic meters / mole), Indicates Henry's coefficient, unit is Pa m³ / mol (Pascal cubic meters / mole), Represents the Faraday constant, with the unit of C / mol (coulomb / mole), represents the transfer coefficient, Indicates the overpotential gas transport resistance, the unit is V (volt), Represents the local gas transport resistance, in Ω m² (Ohm square meters), It represents the interfacial area between the ionomer and the catalyst, with the unit of m² / m³ (square meters / cubic meter). The superscript ref represents the reference value, the subscript a represents the anode, c represents the cathode, pt represents the platinum loading, H2 represents hydrogen, and O2 represents oxygen.

[0189] In this example, , , , , , , , , the remaining relevant parameters are obtained in each iterative step of step (1) and step (2), so as to calculate the electrochemical reaction rate of the one-dimensional node.

[0190] Furthermore, the reversible voltage is obtained from the Nernst equation and expressed as:

[0191] (13)

[0192] in, Represents the reversible voltage, the unit is V (volt), It represents the entropy change of electrochemical reaction, with the unit of J / (mol K) (Joules / mole Kelvin), represents the universal gas constant, in J / (mol K) (Joules / mole Kelvin), Represents the Faraday constant, with the unit of C / mol (coulomb / mole), Indicates the inlet hydrogen pressure in Pa (Pascal), represents oxygen pressure in Pa (Pascal), T represents absolute temperature in K (Kelvin), Indicates the reference temperature in K (Kelvin), Indicates the reference pressure in Pa (Pascal). In this example, , , the remaining parameters are obtained in each iterative step of step (1) and step (2), so as to calculate the reversible voltage of the one-dimensional node of the fuel cell.

[0193] 3. Using the above-mentioned local dimensionality reduction single cell model of proton exchange membrane fuel cells for power generation in plateau areas, by changing the operating conditions, the effects of reaction gas inlet temperature and inlet pressure on the fuel cell output voltage, mass transfer characteristics and hydrothermal management are obtained.

[0194] As an example, the operating conditions are selected as follows: an altitude of 2000m, a reaction gas inlet pressure of 80.3kPa, and reaction gas inlet temperatures of 285.15K, 305.15K, 325.15K, and 345.15K. Figure 5 The results show that as the reactant gas inlet temperature increases, the fuel cell output voltage increases. This is because higher reactant gas inlet temperatures increase the catalyst layer temperature, increasing the reaction rate and reducing activation losses. However, the increasing trend slows down at higher reactant gas inlet temperatures.

[0195] Furthermore, the operating conditions of an altitude of 2000m and a reaction gas inlet temperature of 285.15K were selected, and the reaction gas inlet pressures were selected as 80.3kPa, 100.3kPa, 120.3kPa, 140.3kPa, and 160.3kPa, respectively. Figure 6 The results show that as the reactant gas inlet pressure increases, the fuel cell output voltage increases. This is because higher reactant gas inlet pressure promotes the transfer of oxygen to the catalyst layer, increasing the oxygen concentration in the catalyst layer and reducing mass transfer losses. However, the increasing trend slows down at higher reactant gas inlet pressures.

[0196] Fourth, a performance evaluation method for proton exchange membrane fuel cells used for power generation in plateau areas is provided. Comprehensive evaluation of proton exchange membrane fuel cells cannot be limited to output voltage alone; additional losses caused by pressurizing and preheating the reactant gases, as well as fuel cell flooding, must also be considered. Therefore, a performance evaluation method is proposed that combines output power, pumping losses, gas preheating losses, and liquid water saturation in the cathode catalyst layer.

[0197] The initial output power of the proton exchange membrane fuel cell under initial operating conditions is calculated as shown in formula (14).

[0198] (14)

[0199] in, Indicates the initial output power in W (watt). Represents the average current density of the simulation, in units of (amperes per square meter), Indicates the simulated output voltage in V (volts). Represents the simulated activation area in units of (square meters). , .

[0200] The initial pumping loss power of the proton exchange membrane fuel cell under initial operating conditions (additional energy consumption caused by air compressor pumping loss) is calculated as shown in formula (15).

[0201] (15)

[0202] in, Indicates the initial pumping power loss, in W (watt), Indicates the simulated inlet gas pressure of the fuel cell flow channel anode, in Pa (Pascal), Indicates the initial inlet pressure parameter, the unit is Pa (Pascal), Indicates the simulated inlet gas pressure of the fuel cell flow channel cathode, in Pa (Pascal), represents the simulated inlet gas mass flow rate of the anode in kg / s (kilograms per second), represents the simulated cathode inlet gas mass flow rate in kg / s (kilograms per second), represents the pump efficiency, which is assumed to be 70%, and the subscripts a and c represent the anode and cathode, respectively.

[0203] The initial gas preheating loss power (additional energy consumption caused by preheating of reaction gas) of the proton exchange membrane fuel cell under initial operating conditions is shown in Equation (16).

[0204] (16)

[0205] in, Indicates the initial gas preheating power loss, in W (watt), represents the simulated inlet gas temperature of the fuel cell flow channel anode, in K (Kelvin), represents the initial inlet reaction gas temperature parameter, in K (Kelvin), represents the simulated inlet gas temperature of the fuel cell flow channel cathode, in K (Kelvin), represents the simulated anode proportional constant, Represents the simulated cathode proportional constant, and the subscripts H2 and O2 represent hydrogen and oxygen, respectively.

[0206] Performance evaluation value corresponding to target operating conditions , as shown in formula (17).

[0207] (17)

[0208] in, Indicates the liquid water saturation of the catalyst layer of the fuel cell, is the weight index of liquid water saturation in the catalyst layer, which is assumed to be 2. The larger the value, the greater the risk of flooding the fuel cell is considered to face. The more significant the impact is, the When it is close to 1, the evaluation criteria It decreases rapidly to 0. The superscript 0 represents the initial parameter, and 1 represents the corresponding parameter when the fuel cell operating conditions change.

[0209] In this example, the initial operating conditions are as follows: the altitude parameter is 2000m, the initial inlet reaction gas temperature parameter is 285.15K, and the initial inlet pressure parameter is 80.3kPa. , , Furthermore, under the target operating conditions of target altitude parameter of 2000m, target inlet reaction gas inlet temperature parameter of 305.15K, and target inlet pressure parameter of 80.3kPa, the above steps are used to calculate , , The fuel cell performance evaluation value calculated under the target operating conditions is .

[0210] Further, according to the calculation results of the fuel cell at different reaction gas inlet temperatures and inlet pressures obtained in step 3, the fuel cell performance evaluation value is obtained. Changes with the fuel cell reaction gas inlet temperature and inlet pressure.

[0211] Performance evaluation of proton exchange membrane fuel cells for power generation in plateau areas As the reaction gas inlet temperature changes Figure 7 The results show that as the reaction gas inlet temperature increases, the performance evaluation value First it increases and then decreases. Although the fuel cell output voltage gradually increases with the increase of the reaction gas inlet temperature, it will bring additional inlet gas preheating loss, resulting in the performance evaluation value at a higher reaction gas inlet temperature. When the reaction gas inlet temperature is 325.15 K, the evaluation criterion reaches the maximum value of 1.027.

[0212] Performance evaluation of proton exchange membrane fuel cells for power generation in plateau areas As the reaction gas inlet pressure changes Figure 8 The results show that as the reaction gas inlet pressure increases, the performance evaluation value Although the fuel cell output voltage gradually increases with the increase of the reaction gas inlet pressure, it will bring additional pumping loss, resulting in a higher performance evaluation value at a higher reaction gas inlet pressure. When the reaction gas inlet pressure is 140.3 kPa, the evaluation standard reaches the maximum value of 1.128.

[0213] Based on the changes in the performance evaluation values ​​for power generation fuel cells in plateau areas, the optimal gas inlet temperature and pressure for the power generation PEMFC in this example are determined to be 325.15K and 140.3kPa, respectively. While this example only discusses the impact of reactant gas inlet temperature and pressure on the evaluation criteria for power generation PEMFCs at an altitude of 2000m, the proposed performance evaluation values ​​are generally applicable and are still effective for optimizing operating conditions at other altitudes.

[0214] The optimization method for the operating conditions of the proton exchange membrane fuel cell provided in this embodiment establishes a plateau environment model to obtain the changes in atmospheric temperature and pressure with altitude. A local dimensionality reduction single cell model of the proton exchange membrane fuel cell is established to optimize the operating conditions of the proton exchange membrane fuel cell with an activation area of ​​more than 450 cm 2 Efficient and accurate simulation of power generation fuel cells. Using a locally reduced-dimensional single-cell model of a proton exchange membrane fuel cell, the effects of varying fuel cell operating conditions, including reactant gas inlet temperature and pressure, on fuel cell output voltage, mass transfer characteristics, and hydrothermal management are analyzed. A performance evaluation method for proton exchange membrane fuel cells used in plateau regions is provided. The performance evaluation value is calculated as a function of reactant gas inlet temperature and pressure, enabling adaptive optimization of operating conditions for proton exchange membrane fuel cells used in plateau regions.

[0215] Compared to traditional one-dimensional models, the method for optimizing the operating conditions of proton exchange membrane fuel cells provided in this embodiment uses a local dimensionality reduction model that can truly reflect the actual physical processes within the proton exchange membrane fuel cell and demonstrate the impact of environmental changes in plateau regions on the internal reactions and mass transfer characteristics of the proton exchange membrane fuel cell. Compared to traditional three-dimensional models, the local dimensionality reduction model reduces the mesh size, which can improve computational efficiency and enable efficient and accurate simulation of large-scale power generation fuel cells. Compared to traditional methods for optimizing the operating conditions of proton exchange membrane fuel cells, the performance evaluation value calculation method proposed in this embodiment fully accounts for the additional losses caused by pressurizing and preheating the reactant gases, as well as the problem of fuel cell flooding, and can adaptively optimize the operating conditions of power generation proton exchange membrane fuel cells in plateau regions.

[0216] It should be understood that, although the various steps in the flowcharts involved in the various embodiments described above are displayed in sequence according to the instructions of the arrows, these steps are not necessarily performed in sequence in the order indicated by the arrows. Unless clearly stated herein, the execution of these steps is not strictly limited in order, and these steps can be performed in other orders. Moreover, at least a portion of the steps in the flowcharts involved in the various embodiments described above may include multiple steps or multiple stages, and these steps or stages are not necessarily performed at the same time, but can be performed at different times, and the execution order of these steps or stages is not necessarily performed in sequence, but can be performed in turn or alternately with at least a portion of the steps or stages in other steps or other steps. It is understandable that the various steps in different embodiments can be freely combined as needed, and the various non-contradictory schemes formed by the combination all fall within the scope of protection of this application.

[0217] Based on the same inventive concept, embodiments of the present application also provide a device for optimizing the operating conditions of a proton exchange membrane fuel cell, which is used to implement the aforementioned method for optimizing the operating conditions of a proton exchange membrane fuel cell. The solution provided by this device is similar to the solution described in the aforementioned method. Therefore, the specific limitations of one or more embodiments of the device for optimizing the operating conditions of a proton exchange membrane fuel cell provided below can be found in the aforementioned definition of the method for optimizing the operating conditions of a proton exchange membrane fuel cell, and will not be repeated here.

[0218] In an exemplary embodiment, Figure 9 As shown, a device for optimizing the operating conditions of a proton exchange membrane fuel cell is provided, wherein:

[0219] An initial simulation module 901 is configured to simulate the proton exchange membrane fuel cell based on a local dimensionality reduction single cell model of the proton exchange membrane fuel cell and initial operating conditions to obtain an initial effective output power; the initial operating conditions include at least one of an initial altitude parameter, an initial inlet reactant gas temperature parameter, and an initial inlet pressure parameter;

[0220] The target operating condition acquisition module 902 is used to sequentially increase the initial parameter values ​​under the initial operating conditions to obtain the target operating conditions;

[0221] A re-simulation module 903 is configured to re-simulate the proton exchange membrane fuel cell according to the target operating conditions and the local dimensionality reduction single cell model to obtain a target saturation of liquid water in the cathode catalyst layer and a target effective output power;

[0222] a performance evaluation value acquisition module 904 for obtaining a performance evaluation value corresponding to a target operating condition according to the initial effective output power, the target effective output power, and the target saturation of liquid water in the cathode catalyst layer;

[0223] The optimal operating condition determination module 905 is configured to determine that the target operating condition corresponding to the performance evaluation value is the optimal operating condition when the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value.

[0224] In one embodiment, the device also includes a model building module, which is used to: model the gas channels, gas diffusion layers, and extended layers in the anode and cathode in the proton exchange membrane fuel cell as a three-dimensional calculation domain; model the microporous layer, catalytic layer and proton exchange membrane in the proton exchange membrane fuel cell as a one-dimensional calculation domain; and obtain a local dimensionality reduction single cell model of the proton exchange membrane fuel cell based on the three-dimensional calculation domain and the one-dimensional calculation domain.

[0225] In one embodiment, the initial simulation module 901 is further used to: simulate the proton exchange membrane fuel cell based on the local reduced-dimensional single-cell model and initial operating conditions of the proton exchange membrane fuel cell to obtain the initial output power, initial pumping loss power and initial gas preheating loss power; obtain the initial total loss power based on the initial pumping loss power and the initial gas preheating loss power; and obtain the initial effective output power based on the difference between the initial output power and the initial total loss power.

[0226] In one embodiment, the initial simulation module 901 is also used to: obtain an initial anode pressure difference based on the simulated inlet gas pressure of the anode of the fuel cell flow channel and the initial inlet pressure parameter in the initial operating conditions; obtain an initial cathode pressure difference based on the simulated inlet gas pressure of the cathode of the fuel cell flow channel and the initial inlet pressure parameter in the initial operating conditions; obtain an initial anode gas delivery power based on the simulated inlet gas mass flow rate of the anode and the initial anode pressure difference; obtain an initial cathode gas delivery power based on the simulated inlet gas mass flow rate of the cathode and the initial cathode pressure difference; obtain a total gas delivery power based on the initial anode gas delivery power and the initial cathode gas delivery power; and obtain an initial pump gas loss power based on the total gas delivery power and the simulated pump efficiency.

[0227] In one embodiment, the initial simulation module 901 is also used to: obtain an initial anode temperature difference based on the simulated inlet gas temperature of the anode of the fuel cell flow channel and the initial inlet reaction gas temperature parameters in the initial operating conditions; obtain an initial cathode temperature difference based on the simulated inlet gas temperature of the cathode of the fuel cell flow channel and the initial inlet reaction gas temperature parameters in the initial operating conditions; obtain an initial anode gas preheating loss power based on the initial anode temperature difference, the simulated gas mass flow rate at the anode inlet and the simulated anode proportional constant; obtain an initial cathode gas preheating loss power based on the initial cathode temperature difference, the simulated gas mass flow rate at the cathode inlet and the simulated cathode proportional constant; obtain an initial gas preheating loss power based on the initial anode gas preheating loss power and the initial cathode gas preheating loss power.

[0228] In one embodiment, the performance evaluation value acquisition module 904 is also used to: obtain the cathode catalyst layer liquid water threshold saturation and the cathode catalyst layer liquid water saturation weight index; obtain the cathode catalyst layer liquid water saturation influence coefficient based on the cathode catalyst layer liquid water threshold saturation, the cathode catalyst layer liquid water saturation weight index and the cathode catalyst layer liquid water target saturation; obtain the performance evaluation value corresponding to the target operating conditions based on the ratio of the initial effective output power to the target effective output power, and the cathode catalyst layer liquid water saturation influence coefficient.

[0229] Each module in the aforementioned apparatus for optimizing proton exchange membrane fuel cell operating conditions may be implemented in whole or in part through software, hardware, or a combination thereof. Each module may be embedded in or independent of a processor within a computer device in the form of hardware, or may be stored in a computer device memory in the form of software, so that the processor can call and execute the corresponding operations of each module.

[0230] In an exemplary embodiment, a computer device is provided. The computer device may be a server, and its internal structure diagram may be as shown in FIG. Figure 10As shown. The computer device includes a processor, a memory, an input / output interface (Input / Output, abbreviated as I / O) and a communication interface. The processor, memory and input / output interface are connected through a system bus, and the communication interface is connected to the system bus through the input / output interface. The processor of the computer device is used to provide computing and control capabilities. The memory of the computer device includes a non-volatile storage medium and an internal memory. The non-volatile storage medium stores an operating system, a computer program and a database. The internal memory provides an environment for the operation of the operating system and computer program in the non-volatile storage medium. The database of the computer device is used to store data of an embodiment of a method for optimizing the operating conditions of a proton exchange membrane fuel cell. The input / output interface of the computer device is used to exchange information between the processor and an external device. The communication interface of the computer device is used to communicate with an external terminal through a network connection. When the computer program is executed by the processor, a method for optimizing the operating conditions of a proton exchange membrane fuel cell is implemented.

[0231] Those skilled in the art will understand that Figure 10 The structure shown in the figure is only a block diagram of a part of the structure related to the solution of the present application, and does not constitute a limitation on the computer device to which the solution of the present application is applied. The specific computer device may include more or fewer components than shown in the figure, or combine certain components, or have a different component arrangement.

[0232] In one embodiment, a computer device is further provided, including a memory and a processor. The memory stores a computer program, and the processor implements the steps in the above method embodiments when executing the computer program.

[0233] In one embodiment, a computer-readable storage medium is provided, on which a computer program is stored. When the computer program is executed by a processor, the steps in the above-mentioned method embodiments are implemented.

[0234] In one embodiment, a computer program product is provided, including a computer program, which implements the steps in the above method embodiments when executed by a processor.

[0235] It should be noted that the user information (including but not limited to user device information, user personal information, etc.) and data (including but not limited to data used for analysis, stored data, displayed data, etc.) involved in this application are all information and data authorized by the user or fully authorized by all parties, and the collection, use and processing of relevant data must comply with relevant regulations.

[0236] Those skilled in the art can understand that all or part of the processes in the above-mentioned embodiment methods can be completed by instructing the relevant hardware through a computer program. The computer program can be stored in a non-volatile computer readable storage medium, and when executed, can include the processes of the above-mentioned embodiment methods. Any reference to memory, database or other medium used in the embodiments provided in the present application can include at least one of non-volatile memory and volatile memory. The non-volatile memory can include read-only memory (ROM), magnetic tape, floppy disk, flash memory, optical storage, high-density embedded non-volatile memory, resistive random access memory (ReRAM), magnetoresistive random access memory (MRAM), ferroelectric random access memory (FRAM), phase change memory (PCM), graphene memory, etc. The volatile memory can include random access memory (RAM) or external cache memory, etc. As an illustration but not limitation, the RAM can be in various forms, such as static random access memory (SRAM) or dynamic random access memory (DRAM), etc. The database involved in the embodiments provided in the present application can include at least one of a relational database and a non-relational database. The non-relational database can include a distributed database based on a block chain, etc., without being limited thereto. The processor involved in the embodiments provided in the present application can be a general-purpose processor, a central processing unit, a graphics processing unit, a digital signal processor, a programmable logic device, a data processing logic device based on quantum computing, an artificial intelligence (AI) processor, etc., without being limited thereto.

[0237] The technical features of the above embodiments can be combined in any manner. To make the description concise, not all possible combinations of the technical features in the above embodiments are described, but as long as the combinations of the technical features do not exist contradictions, they should be considered as the scope of the present application.

[0238] The above-described embodiments merely represent several implementation methods of the present application. While the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the present application. It should be noted that a person of ordinary skill in the art may make various modifications and improvements without departing from the spirit of the present application, and these modifications and improvements fall within the scope of protection of the present application. Therefore, the scope of protection of the present application shall be determined by the appended claims.

Claims

1. A method for optimizing operating conditions of a proton exchange membrane fuel cell, characterized in that: The method comprises: Simulating the proton exchange membrane fuel cell according to a local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell to obtain an initial effective output power; the initial operating conditions including at least one of an initial altitude parameter, an initial inlet reactant gas temperature parameter, and an initial inlet pressure parameter; The initial parameter values ​​under the initial operating conditions are increased in sequence to obtain the target operating conditions; The proton exchange membrane fuel cell is simulated again according to the target operating conditions and the local dimensionality reduction single cell model to obtain the target saturation of liquid water in the cathode catalyst layer and the target effective output power; Obtaining a performance evaluation value corresponding to a target operating condition according to the initial effective output power, the target effective output power, and the target saturation of liquid water in the cathode catalyst layer; When the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value, the target operating condition corresponding to the performance evaluation value is determined to be the optimal operating condition.

2. The method according to claim 1, characterized in that Before simulating the proton exchange membrane fuel cell based on the local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell, the method further includes: The gas channels, gas diffusion layers, and extended layers in the anode and cathode of the proton exchange membrane fuel cell are modeled as a three-dimensional computational domain. The microporous layer, catalytic layer and proton exchange membrane in the proton exchange membrane fuel cell are modeled into a one-dimensional computational domain; A local dimensionality reduction single cell model of a proton exchange membrane fuel cell is obtained according to the three-dimensional calculation domain and the one-dimensional calculation domain.

3. The method according to claim 1, characterized in that The method of simulating the proton exchange membrane fuel cell based on the local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell to obtain the initial effective output power includes: Based on the local dimensionality reduction single cell model and initial operating conditions of the proton exchange membrane fuel cell, the proton exchange membrane fuel cell is simulated to obtain the initial output power, initial pumping loss power and initial gas preheating loss power; Obtaining an initial total power loss according to the initial pumping power loss and the initial gas preheating power loss; An initial effective output power is obtained according to a difference between the initial output power and the initial total power loss.

4. The method according to claim 3, characterized in that Get the initial pumping power loss, including: Obtaining an initial anode pressure difference based on a simulated inlet gas pressure of the fuel cell flow channel anode and an initial inlet pressure parameter in the initial operating condition; Obtaining an initial cathode pressure difference value based on a simulated inlet gas pressure of a cathode of a fuel cell flow channel and an initial inlet pressure parameter in an initial operating condition; Obtaining an initial anode gas delivery power according to the simulated anode inlet gas mass flow rate and the initial anode pressure difference; Obtaining an initial cathode gas delivery power according to the simulated cathode inlet gas mass flow rate and the initial cathode pressure difference; Obtaining a total gas delivery power according to the initial anode gas delivery power and the initial cathode gas delivery power; The initial pump gas loss power is obtained according to the total gas delivery power and the simulated pump efficiency.

5. The method according to claim 3, characterized in that The initial gas preheating power loss is obtained, including: Obtaining an initial anode temperature difference based on a simulated inlet gas temperature of the fuel cell flow channel anode and an initial inlet reaction gas temperature parameter in the initial operating condition; Obtaining an initial cathode temperature difference based on a simulated inlet gas temperature of a fuel cell flow channel cathode and an initial inlet reaction gas temperature parameter in an initial operating condition; Obtaining initial anode gas preheating power loss according to the initial anode temperature difference, the anode inlet simulated gas mass flow rate, and the simulated anode proportional constant; Obtaining the initial cathode gas preheating loss power according to the initial cathode temperature difference, the cathode inlet simulated gas mass flow rate, and the simulated cathode proportional constant; The initial gas preheating loss power is obtained according to the initial anode gas preheating loss power and the initial cathode gas preheating loss power.

6. The method according to claim 1, characterized in that Obtaining a performance evaluation value corresponding to a target operating condition according to the initial effective output power, the target effective output power, and the target saturation of liquid water in the cathode catalyst layer includes: Obtaining a liquid water threshold saturation of the cathode catalyst layer and a weight index of the liquid water saturation of the cathode catalyst layer; Obtaining a cathode catalyst layer liquid water saturation influence coefficient according to the cathode catalyst layer liquid water threshold saturation, the cathode catalyst layer liquid water saturation weight index, and the cathode catalyst layer liquid water target saturation; According to the ratio of the initial effective output power to the target effective output power and the liquid water saturation influence coefficient of the cathode catalyst layer, a performance evaluation value corresponding to the target operating condition is obtained.

7. A device for optimizing the operating conditions of a proton exchange membrane fuel cell, characterized in that: The device comprises: an initial simulation module for simulating the proton exchange membrane fuel cell based on a local dimensionality reduction single cell model of the proton exchange membrane fuel cell and initial operating conditions to obtain an initial effective output power; the initial operating conditions including at least one of an initial altitude parameter, an initial inlet reactant gas temperature parameter, and an initial inlet pressure parameter; A target operating condition acquisition module is used to sequentially increase the initial parameter values ​​under the initial operating conditions to obtain the target operating conditions; a re-simulation module for re-simulating the proton exchange membrane fuel cell according to the target operating conditions and the local dimensionality reduction single cell model to obtain a target saturation of liquid water in the cathode catalyst layer and a target effective output power; a performance evaluation value acquisition module, configured to obtain a performance evaluation value corresponding to a target operating condition according to the initial effective output power, the target effective output power, and the target saturation of liquid water in the cathode catalyst layer; The optimal operating condition determination module is used to determine that the target operating condition corresponding to the performance evaluation value is the optimal operating condition when the performance evaluation value corresponding to the target operating condition is the maximum performance evaluation value.

8. A computer device comprising a memory and a processor, wherein the memory stores a computer program, wherein: When the processor executes the computer program, the steps of the method according to any one of claims 1 to 6 are implemented.

9. A computer-readable storage medium having a computer program stored thereon, characterized in that: When the computer program is executed by a processor, the steps of the method according to any one of claims 1 to 6 are implemented.

10. A computer program product comprising a computer program, characterized in that When the computer program is executed by a processor, the steps of the method according to any one of claims 1 to 6 are implemented.

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