CN111090964A - Full-area single-pool model building method combining fluid and performance simulation - Google Patents

Full-area single-pool model building method combining fluid and performance simulation Download PDF

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CN111090964A
CN111090964A CN201911405270.XA CN201911405270A CN111090964A CN 111090964 A CN111090964 A CN 111090964A CN 201911405270 A CN201911405270 A CN 201911405270A CN 111090964 A CN111090964 A CN 111090964A
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cathode
anode
fluid
exchange membrane
proton exchange
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CN111090964B (en
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徐家慧
陈敏
赵洋洋
刘雪婷
邢丹敏
李光伟
姜炜
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Sunrise Power Co Ltd
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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04305—Modeling, demonstration models of fuel cells, e.g. for training purposes
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
    • H01M8/04537—Electric variables
    • H01M8/04634—Other electric variables, e.g. resistance or impedance
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Abstract

The invention discloses a method for establishing a full-area single-cell model by combining fluid and performance simulation, which comprises the steps of establishing a complex bidirectional meandering flow channel full-area proton exchange membrane fuel cell model, and cutting a proton exchange membrane into a cathode proton exchange membrane part and an anode proton exchange membrane part from the center; cutting a proton exchange membrane, an anode catalyst layer, an anode microporous layer, an anode diffusion layer and an anode plate which are positioned at an anode by adopting anode fluid, and processing all the components into a structure consistent with the anode fluid; the proton exchange membrane, cathode catalyst layer, cathode microporous layer, cathode diffusion layer and cathode plate at the cathode are cut with the cathode fluid and all processed into a structure consistent with the cathode fluid. The method can not cause errors to the calculation result, greatly reduces the calculation grids and greatly improves the calculation precision.

Description

Full-area single-pool model building method combining fluid and performance simulation
Technical Field
The invention relates to the technical field of fuel cells, in particular to a method for establishing a complex asymmetric bidirectional serpentine flow channel full-area single cell model by combining fluid and performance simulation.
Background
Fuel cells have now been developed as a very promising energy technology due to their advantages of high efficiency and zero emissions. The proton exchange membrane fuel cell is taken as a complex system with multiple physical fields, multiple scales and multiple phases, and the distribution of the multiple physical fields in the proton exchange membrane fuel cell becomes an indispensable part of analytical research on the electrical performance and the like of the fuel cell. In the prior art, the calculation method of the electrical performance of the battery in the vehicle fuel cell is almost limited to the calculation process of the single-channel fuel cell, and the influence of fluid distribution on the fuel cell is not considered, because the mutual influence exists among fluids of the full-area single cell, and the calculation boundary condition method of the single channel cannot well reflect the real process of the full-area fuel cell, the calculation result of the single channel often has a certain error with the calculation result of the full-area single cell, so that the full-area proton exchange membrane fuel cell model is established from the angle of modeling and calculation, and still is a challenging work in the analysis and research process of the fuel cell.
Disclosure of Invention
According to the problems in the prior art, the invention discloses a full-area single-pool model building method combining fluid and performance simulation, which specifically comprises the following steps:
establishing a complex bidirectional serpentine flow channel full-area proton exchange membrane fuel cell model, and cutting a proton exchange membrane into a cathode proton exchange membrane part and an anode proton exchange membrane part from the center; cutting the proton exchange membrane, the anode catalyst layer, the anode microporous layer, the anode diffusion layer and the anode plate which are positioned at the anode by adopting anode fluid, and processing the whole components into a structure consistent with the anode fluid; the proton exchange membrane, cathode catalyst layer, cathode microporous layer, cathode diffusion layer and cathode plate at the cathode are cut with the cathode fluid and all processed into a structure consistent with the cathode fluid.
Furthermore, interfaces are added at the center of the proton exchange membrane and the center of the cooling liquid at the structural asymmetry position in the thickness direction, and data are transmitted between the two interfaces in an interpolation mode. On the one hand, the structured grid can be processed to increase the quality of the grid, and on the other hand, the generation of a large number of grids can be reduced.
Further, calculating anode fluid, cathode fluid and cooling fluid of the bipolar plate fluid, and taking the calculation result of the three-cavity fluid as the input condition of the calculation of the complex bidirectional winding flow passage full-area proton exchange membrane fuel cell model.
Further, the anode and cathode exchange current density is respectively tested by adopting a bipolar plate according to the oxygen reduction kinetic principle and the hydrogen oxidation kinetic principle, and parameters such as temperature, pressure, catalyst and the like are corrected to respectively obtain anode and cathode reference exchange current density values:
Figure BDA0002348457640000021
wherein J0(T) is exchange current density [ A/m ]2]；
Figure BDA0002348457640000022
Exchange current density [ A/m ] for reference2]；αcIs the specific surface area of the catalyst [ cm [)2/mg]；LcAs catalyst loading (mg/cm)2]，EcFor activation energy [ kJ/mol ]-1]。
Further, a catalytic layer polymer model is adopted to correct the cathode exchange current density and the mass transfer loss:
Figure BDA0002348457640000023
Jcatexchange the current density A/m for the cathode2，ζcatThe specific surface area of the cathode catalyst layer is 1/m, s is the liquid phase saturation, KWSolubility of oxygen in liquid water, DWThe diffusivity of oxygen in liquid water, rpIn order to be the radius of the catalyst,
Figure BDA0002348457640000024
the cathode is ideally designed to carry an electric current,
Figure BDA0002348457640000025
is the cathode catalyst ionic resistance.
Further, the method comprises the following steps: and correcting the measured heat conductivity coefficient by pressure and porosity in the model building process, wherein the heat conductivity coefficients of the diffusion layer and the microporous layer are corrected by pressure:
Figure BDA0002348457640000026
wherein epsilon0Initial porosity, δ0To an initial thickness, δyThickness after compression deformation, pVIs the bulk density, psIs the carbon fiber density; and (3) considering the anisotropy of porous materials of each layer of the MEA, and correcting the thermal conductivity coefficients by porosity:
keff＝(1-ε)1.5k (5)
further, combining the solution phase model, the flow channel liquid phase model and the porous medium liquid phase model to obtain a water generation and transportation model:
dissolved phase model:
Figure BDA0002348457640000031
wherein epsiloniIs the porosity of the porous medium, and the porous medium,
Figure BDA0002348457640000032
lambda is the dissolved water content, ndIn order to obtain a coefficient of osmotic resistance,
Figure BDA0002348457640000033
is the water content diffusion coefficient, SλFor the reaction on the cathode side of the catalyst layer to produce water rate, SgdFor its mass exchange rate of the seawater and the dissolved water, SldThe mass exchange rates of liquid water and dissolved water are adopted;
the porous medium liquid phase model is as follows:
Figure BDA0002348457640000034
where ρ islIs liquid water density, mulIs hydrodynamic viscosity in liquid state, K is absolute permeability, KrAs relative permeability, plIs hydraulic water pressure, SglThe mass exchange rates of the gaseous water and the liquid water are obtained;
the flow channel liquid phase model is as follows:
Figure BDA0002348457640000035
Figure BDA0002348457640000036
wherein DliqIs the diffusion coefficient of the liquid water,
Figure BDA0002348457640000037
in order to obtain the flow rate of the liquid,
Figure BDA0002348457640000038
is the gas flow rate. By adopting the technical scheme, the invention provides a full-area single cell model building method combining fluid and performance simulationFluid calculation of fluid and cooling liquid fluid, and then taking the calculation result of three-cavity fluid as the input condition of full-area single-cell multi-physical-field coupling calculation, the method does not cause error to the calculation result, and greatly reduces the calculation grid, so that the multi-physical-field coupling calculation of the full-area asymmetric bidirectional serpentine flow channel bipolar plate proton exchange membrane fuel cell becomes possible under the condition of the current computer resources, and the calculation is not simplified, thereby greatly improving the calculation precision.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments described in the present application, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a general view of a full-area fuel cell of the present invention;
FIG. 2 is a schematic view of a portion of an asymmetric bi-directional serpentine flow channel of the present invention;
FIG. 3 is a comparison of experimental and calculated results of the present invention.
Wherein: 1 is empty, 2 is water in, 3 is hydrogen out, 4 is hydrogen in, 5 is water out, 6 is empty, 9 is a bridge plate area, 10 is a distribution area, and 11 is a reaction area; the reference numeral 12 denotes a hydrogen flow path, and 13 denotes an empty flow path.
Detailed Description
In order to make the technical solutions and advantages of the present invention clearer, the following describes the technical solutions in the embodiments of the present invention clearly and completely with reference to the drawings in the embodiments of the present invention:
as shown in fig. 1, a method for establishing a full-area single-pool model by combining fluid and performance simulation specifically includes the following steps:
establishing a complex bidirectional meandering flow passage full-area proton exchange membrane fuel cell model, cutting a proton exchange membrane into a cathode proton exchange membrane part and an anode proton exchange membrane part from the center, then cutting the proton exchange membrane, an anode catalyst layer, an anode microporous layer, an anode diffusion layer and an anode plate which are positioned at an anode by using anode fluid, and processing the two parts into a structure consistent with the anode fluid; the proton exchange membrane, the cathode catalyst layer, the cathode microporous layer, the cathode diffusion layer and the cathode plate which are positioned at the cathode are cut by cathode fluid and are all processed into a structure consistent with the cathode fluid, so that a mathematical model of the full-area asymmetric bidirectional serpentine flow channel bipolar plate proton exchange membrane fuel cell can be established.
As a preferable mode, since the complex bidirectional serpentine flow channel full-area proton exchange membrane fuel cell model is a complex asymmetric bidirectional serpentine flow channel full-area model as shown in fig. 2, structured grids corresponding to grids one to one cannot be formed, and even if an unstructured grid is generated, the quality and the number of the grids cannot be guaranteed, the model cuts other materials by using anode fluid and cathode fluid respectively, an interface can be added at the center of the proton exchange membrane, an interface is added at the center of the cooling liquid, and the complex asymmetric bidirectional serpentine flow channel full-area proton exchange membrane fuel cell model can be completely processed into the structured grids by adopting a self-adaptive function.
Preferably, the fluid calculation of the anode fluid, the cathode fluid and the cooling fluid is firstly carried out on the bipolar plate fluid, and then the calculation results of the three-cavity fluids, namely the calculation results of the flow rate and the pressure of the three-cavity fluids entering the inlet end of the reaction region, namely the calculation results of the flow rate and the pressure of each section of the cathode fluid and the cooling fluid in the sections 7-7 in fig. 1, and the calculation results of the flow rate and the pressure of each section of the anode fluid in the sections 8-8 are used as input conditions for the coupling calculation of the full-area single-cell multi-physical field.
As a preferred mode, because the cathode and anode exchange current density is greatly influenced by the catalytic layer and the fuel cell plate type, aiming at the cathode and anode reference exchange current density adopted in the calculation, experimental tests are firstly carried out to obtain the cathode and anode exchange current density, and then parameters such as temperature, pressure, catalyst and the like are corrected, so that the cathode and anode exchange current density is respectively tested by using the bipolar plate according to the oxygen reduction kinetic principle and the hydrogen oxidation kinetic principle, and then the temperature, pressure, catalyst condition and the like are corrected according to the following formula to obtain the cathode and anode reference exchange current density value;
the reference exchange current density value is obtained by adopting the following formula:
Figure BDA0002348457640000041
wherein J0(T) is exchange current density [ A/m ]2]；
Figure BDA0002348457640000051
Exchange current density [ A/m ] for reference2]；αcIs the specific surface area of the catalyst [ cm [)2/mg]；LcAs catalyst loading (mg/cm)2]，EcFor activation energy [ kJ/mol ]-1]。
Furthermore, in the method, the mass transfer loss is relatively corrected, a catalytic layer polymer model is introduced to correct the cathode exchange current density, and the polymer model is introduced to ensure that the mass transfer loss and the experimental mass transfer loss have high goodness of fit, and the result is shown in fig. 3.
Figure BDA0002348457640000052
JcatExchange the current density A/m for the cathode2，ζcatThe specific surface area of the cathode catalyst layer is 1/m, s is the liquid phase saturation, KWSolubility of oxygen in liquid water, DWThe diffusivity of oxygen in liquid water, rpIn order to be the radius of the catalyst,
Figure BDA0002348457640000053
the cathode is ideally designed to carry an electric current,
Figure BDA0002348457640000054
is the cathode catalyst ionic resistance.
Furthermore, the anisotropy of the material is considered in the diffusion layer and the microporous layer, and because the thermal conductivity coefficient used in the simulation is a test result under the normal pressure condition, the measured thermal conductivity coefficient needs to be subjected to pressure and porosity correction in the model, see the formulas (3), (4) and (5), and finally, the simulation calculation result is more consistent with the actual situation. Wherein the heat conductivity coefficients of the diffusion layer and the microporous layer are corrected by adopting the following formula:
Figure BDA0002348457640000055
Figure BDA0002348457640000056
wherein epsilon0Initial porosity, δ0To an initial thickness, δyThickness after compression deformation, pVIs the bulk density, psIs the carbon fiber density;
considering the anisotropy of the porous materials of each layer of the MEA, the thermal conductivity coefficients of the diffusion layer, the microporous layer and the catalytic layer are subjected to porosity correction in the plane direction and the thickness direction:
keff＝(1-ε)1.5k (5)
the method considers the influence of liquid water in MEA and liquid water in the flow channel, the performance curve finally calculated by the formulas (6), (7) and (8) is highly consistent with the experimental test result, as shown in FIG. 3, the dissolved phase model is as follows:
Figure BDA0002348457640000061
wherein epsiloniIs the porosity of the porous medium, and the porous medium,
Figure BDA0002348457640000062
lambda is the dissolved water content, ndIn order to obtain a coefficient of osmotic resistance,
Figure BDA0002348457640000063
is the water content diffusion coefficient, SλFor the reaction on the cathode side of the catalyst layer to produce water rate, SgdFor its mass exchange rate of the seawater and the dissolved water, SldThe mass exchange rates of liquid water and dissolved water are adopted;
the porous medium liquid phase model is as follows:
Figure BDA0002348457640000064
where ρ islIs liquid water density, mulIs hydrodynamic viscosity in liquid state, K is absolute permeability, KrAs relative permeability, plIs hydraulic water pressure, SglThe mass exchange rates of the gaseous water and the liquid water are obtained;
the flow channel liquid phase model is as follows:
Figure BDA0002348457640000065
Figure BDA0002348457640000066
wherein DliqIs the diffusion coefficient of the liquid water,
Figure BDA0002348457640000067
in order to obtain the flow rate of the liquid,
Figure BDA0002348457640000068
is the gas flow rate.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.

Claims (7)

1. A full-area single pool model building method combining fluid and performance simulation is characterized by comprising the following steps:
establishing a complex bidirectional serpentine flow channel full-area proton exchange membrane fuel cell model, and cutting a proton exchange membrane into a cathode proton exchange membrane part and an anode proton exchange membrane part from the center; cutting the proton exchange membrane, the anode catalyst layer, the anode microporous layer, the anode diffusion layer and the anode plate which are positioned at the anode by adopting anode fluid, and processing the whole components into a structure consistent with the anode fluid; the proton exchange membrane, cathode catalyst layer, cathode microporous layer, cathode diffusion layer and cathode plate at the cathode are cut with the cathode fluid and all processed into a structure consistent with the cathode fluid.
2. The method of claim 1, wherein: adding interfaces at the center of the proton exchange membrane and the center of the cooling liquid at the structural asymmetry position in the thickness direction, and transmitting data between the two interfaces in an interpolation mode.
3. The method of claim 1, wherein: and calculating the anode fluid, the cathode fluid and the cooling liquid fluid of the bipolar plate fluid, and taking the calculation result of the three-cavity fluid as the input condition of the calculation of the complex bidirectional winding flow passage full-area proton exchange membrane fuel cell model.
4. The method of claim 2, wherein: according to the oxygen reduction kinetics principle and the hydrogen oxidation kinetics principle, the bipolar plates are adopted to respectively test the exchange current density of the cathode and the anode, and parameters such as temperature, pressure, catalyst and the like are corrected to respectively obtain the reference exchange current density value of the cathode and the anode:
Figure FDA0002348457630000011
wherein J0(T) is exchange current density [ A/m ]2]；
Figure FDA0002348457630000012
Exchange current density [ A/m ] for reference2]；αcIs the specific surface area of the catalyst [ cm [)2/mg]；LcAs catalyst loading (mg/cm)2]，EcFor activation energy [ kJ/mol ]-1]。
5. The method of claim 4, wherein: and (3) correcting the cathode exchange current density and correcting the mass transfer loss by adopting a catalyst layer polymer model:
Figure FDA0002348457630000021
Jcatexchange the current density A/m for the cathode2，ζcatThe specific surface area of the cathode catalyst layer is 1/m, s is the liquid phase saturation, KWSolubility of oxygen in liquid water, DWThe diffusivity of oxygen in liquid water, rpIn order to be the radius of the catalyst,
Figure FDA0002348457630000022
the cathode is ideally designed to carry an electric current,
Figure FDA0002348457630000023
is the cathode catalyst ionic resistance.
6. The method of claim 5, wherein: and correcting the measured heat conductivity coefficient by pressure and porosity in the model building process, wherein the heat conductivity coefficients of the diffusion layer and the microporous layer are corrected by pressure:
Figure FDA0002348457630000024
wherein epsilon0Initial porosity, δ0To an initial thickness, δyThickness after compression deformation, pVIs the bulk density, psIs the carbon fiber density; and (3) considering the anisotropy of porous materials of each layer of the MEA, and correcting the thermal conductivity coefficients by porosity:
keff＝(1-ε)1.5k (5)。
7. the method of claim 6, wherein: combining the solution phase model, the flow channel liquid phase model and the porous medium liquid phase model to obtain a water generation and transportation model:
dissolved phase model:
Figure FDA0002348457630000025
wherein epsiloniIs the porosity of the porous medium, and the porous medium,
Figure FDA0002348457630000026
lambda is the dissolved water content, ndIn order to obtain a coefficient of osmotic resistance,
Figure FDA0002348457630000027
is the water content diffusion coefficient, SλFor the reaction on the cathode side of the catalyst layer to produce water rate, SgdFor its mass exchange rate of the seawater and the dissolved water, SldThe mass exchange rates of liquid water and dissolved water are adopted;
the porous medium liquid phase model is as follows:
Figure FDA0002348457630000031
where ρ islIs liquid water density, mulIs hydrodynamic viscosity in liquid state, K is absolute permeability, KrAs relative permeability, plIs hydraulic water pressure, SglThe mass exchange rates of the gaseous water and the liquid water are obtained;
the flow channel liquid phase model is as follows:
Figure FDA0002348457630000032
Figure FDA0002348457630000033
wherein DliqIs the diffusion coefficient of the liquid water,
Figure FDA0002348457630000034
in order to obtain the flow rate of the liquid,
Figure FDA0002348457630000035
is the gas flow rate.
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CN111653321A (en) * 2020-06-17 2020-09-11 上海汽车集团股份有限公司 Device and method for calculating activity of fuel cell catalyst, and electronic apparatus
CN112417677A (en) * 2020-11-19 2021-02-26 上海电气集团股份有限公司 Distribution area adjusting method, device, equipment and storage medium
CN112800643A (en) * 2020-12-30 2021-05-14 新源动力股份有限公司 Multi-physical-field coupling calculation simplification method for corrugated-runner fuel cell
CN112800643B (en) * 2020-12-30 2024-03-08 新源动力股份有限公司 Multi-physical field coupling calculation simplifying method for corrugated flow passage fuel cell
CN113921847A (en) * 2021-08-23 2022-01-11 东风汽车集团股份有限公司 Fuel cell stack fluid flow analysis modeling method and device
CN114976099A (en) * 2022-04-27 2022-08-30 同济大学 Fuel cell bipolar plate flow channel optimization design method
CN116029179A (en) * 2023-03-29 2023-04-28 上海治臻新能源股份有限公司 Numerical simulation method and device for fuel cell flow channel structure and computer equipment

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