CN111090964B - Method for establishing full-area single-cell model by combining fluid and performance simulation - Google Patents

Method for establishing full-area single-cell model by combining fluid and performance simulation Download PDF

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CN111090964B
CN111090964B CN201911405270.XA CN201911405270A CN111090964B CN 111090964 B CN111090964 B CN 111090964B CN 201911405270 A CN201911405270 A CN 201911405270A CN 111090964 B CN111090964 B CN 111090964B
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cathode
anode
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water
exchange membrane
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CN111090964A (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

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Abstract

The application 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 serpentine flow channel full-area proton exchange membrane fuel cell model, and cutting a proton exchange membrane into two parts of an anode proton exchange membrane and a cathode proton exchange membrane from the center; cutting a proton exchange membrane, an anode catalytic 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 materials into a structure consistent with the anode fluid; the proton exchange membrane, the cathode catalytic layer, the cathode microporous layer, the cathode diffusion layer and the cathode plate at the cathode are cut by the cathode fluid and all processed into a structure consistent with the cathode fluid. The method does not cause errors to the calculation result, greatly reduces the calculation grid and greatly improves the calculation precision.

Description

Method for establishing full-area single-cell model by combining fluid and performance simulation
Technical Field
The application relates to the technical field of fuel cells, in particular to a method for establishing a full-area single-cell model of a complex asymmetric bidirectional serpentine flow channel by combining fluid and performance simulation.
Background
Fuel cells have been developed as a very promising energy technology due to their high efficiency and zero emissions. The proton exchange membrane fuel cell is used as a complex system with multiple physical fields, multiple dimensions and multiple phases, and the internal multiple physical fields are distributed as an indispensable part of analysis and research on the electrical performance of the fuel cell. In the prior art, the calculation method of the electric performance of the battery in the vehicle fuel cell is almost limited to the calculation process of the single-runner fuel cell, the influence of fluid distribution on the fuel cell is not considered, and the calculation result of the single runner often have certain error with the calculation result of the single runner because of the mutual influence among the fluid of the single-runner and the calculation boundary condition method of the single runner, so that the calculation result of the single runner and the calculation result of the single-runner are analyzed from the angles of modeling and calculation, and the whole-area proton exchange membrane fuel cell model is established, which is a challenging work in the analysis and research process of the fuel cell.
Disclosure of Invention
According to the problems existing in the prior art, the application discloses a method for establishing a full-area single-cell model by 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 two parts of an anode proton exchange membrane and a cathode proton exchange membrane from the center; cutting a proton exchange membrane, an anode catalytic 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 materials into a structure consistent with the anode fluid; the proton exchange membrane, the cathode catalytic layer, the cathode microporous layer, the cathode diffusion layer and the cathode plate at the cathode are cut by 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 asymmetric positions of the structure in the thickness direction, and data transmission is carried out between the two interfaces in an interpolation mode. Processing into structured grids increases the quality of the grids on the one hand and reduces the generation of large numbers of grids on the other hand.
Further, calculating anode fluid, cathode fluid and cooling liquid fluid of the bipolar plate fluid, and taking the calculation result of the three-cavity fluid as the calculation input condition of the complex bidirectional serpentine flow channel full-area proton exchange membrane fuel cell model.
Further, according to the oxygen reduction kinetics principle and the hydrogen oxidation kinetics principle, bipolar plates are adopted to test the exchange current density of the anode and the cathode respectively, and parameters such as temperature, pressure, catalyst and the like are corrected to obtain reference exchange current density values of the anode and the cathode respectively:
wherein J 0 (T) is the exchange current density [ A/m ] 2 ]；Exchange current density for reference [ A/m ] 2 ]；α c Is the specific surface area of the catalyst [ cm ] 2 /mg]；L c Is the catalyst loading [ mg/cm ] 2 ]，E c For activation energy [ kJ/mol ] -1 ]。
Further, the catalytic layer polymer model is used for correcting the cathode exchange current density and the mass loss:
J cat exchange current density A/m for cathode 2 ，ζ cat The specific surface area of the cathode catalytic layer is 1/m, s is the saturation of liquid phase, K W For the solubility of oxygen in liquid water, D W For the diffusivity of oxygen in liquid water, r p In order to achieve a catalyst radius of the catalyst,ideal current transport for the cathode, +.>Is the ionic resistance of the cathode catalyst.
Further, the method comprises the steps of: pressure and porosity correction of the measured thermal conductivity coefficients during modeling, wherein the diffusion layer and microporous layer materials thermal conductivity coefficients are pressure corrected:
wherein ε 0 Initial porosity, delta 0 For initial thickness delta y For thickness after compression deformation ρ V Is the bulk density ρ s Is the density of carbon fiber; taking the anisotropism of porous materials of each layer of the MEA into consideration, carrying out porosity correction on the heat conductivity coefficient:
k eff ＝(1-ε) 1.5 k (5)
further, the dissolved phase model, the runner liquid phase model and the porous medium liquid phase model are combined to obtain a water generation and transportation model:
dissolved phase model:
wherein ε i Is the porosity of the porous medium, and the porous medium is the porous medium,lambda is the dissolved water content, n d In order to achieve a coefficient of osmotic resistance,is the diffusion coefficient of water content, S λ Generating a water rate for the cathode side reaction of the catalytic layer, S gd For its too water and dissolution water mass exchange rate, S ld The mass exchange rate of liquid water and dissolved water is adopted;
the porous medium liquid phase model is as follows:
wherein ρ is l Is liquid water density, mu l Is liquid hydrodynamic viscosity, K is absolute permeability, K r For relative permeability, p l Is hydraulic water pressure, S gl Mass exchange rates for gaseous water and liquid water;
the runner liquid phase model is:
wherein D is liq Is the diffusion coefficient of liquid water, and the water is mixed with the water,for the flow rate of liquid>Is the gas flow rate. By adopting the technical scheme, the method for establishing the full-area single cell model by combining the fluid and the performance simulation comprises the steps of firstly calculating the fluid of the anode fluid, the cathode fluid and the cooling liquid fluid of the bipolar plate fluid, and then taking the calculation result of the three-cavity fluid as the input condition of the full-area single Chi Duo physical field coupling calculation.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings that are required to be used in the embodiments or the description of the prior art will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments described in the present application, and other drawings may be obtained according to the drawings without inventive effort to those skilled in the art.
FIG. 1 is a general view of a full-area fuel cell of the present application;
FIG. 2 is a schematic view of a portion of an asymmetric bidirectional serpentine flow channel according to the present application;
FIG. 3 is a graph showing the comparison of the experimental and calculated results of the present application.
Wherein: 1 is empty in, 2 is water in, 3 is hydrogen out, 4 is hydrogen in, 5 is water out, 6 is empty out, 9 is bridge zone, 10 is distribution zone, 11 is reaction zone; 12 is a hydrogen flow path and 13 is an empty flow path.
Detailed Description
In order to make the technical scheme and advantages of the present application more clear, the technical scheme in the embodiment of the present application is clearly and completely described below with reference to the accompanying drawings in the embodiment of the present application:
the method for establishing the full-area single-cell model by combining fluid and performance simulation shown in fig. 1 specifically comprises the following steps:
a complex bidirectional winding flow channel full-area proton exchange membrane fuel cell model is established, a proton exchange membrane is cut into two parts of an anode proton exchange membrane and a cathode proton exchange membrane from the center, and then the proton exchange membrane, an anode catalytic layer, an anode microporous layer, an anode diffusion layer and an anode plate which are positioned at the anode are cut by anode fluid, and all are processed into a structure consistent with the anode fluid; the proton exchange membrane, the cathode catalytic layer, the cathode microporous layer, the cathode diffusion layer and the cathode polar 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 preferred mode, the complex bidirectional serpentine flow passage full-area proton exchange membrane fuel cell model is a complex asymmetric bidirectional serpentine flow passage full-area model, as shown in fig. 2, structured grids corresponding to grids one by one cannot be formed, quality and quantity of the grids cannot be guaranteed even if unstructured grids are generated, therefore, the model cuts other materials by anode fluid and cathode fluid respectively, interfaces can be added at the center of the proton exchange membrane, interfaces can be added at the center of cooling liquid, and the structured grids can be completely processed by adopting a self-adaption function.
As a preferred mode, the fluid calculation of anode fluid, cathode fluid and cooling liquid fluid is firstly carried out on the bipolar plate fluid, and then the calculation result of three-cavity fluid, namely the calculation result of the flow and the pressure of three-cavity fluid entering the inlet end of the reaction zone, namely the calculation result of the flow and the pressure of each section of cathode fluid and cooling liquid fluid with 7-7 sections in fig. 1, and the calculation result of the flow and the pressure of each section of anode fluid with 8-8 sections are used as the input condition of the physical field coupling calculation of the full area single Chi Duo.
As a preferable mode, because the cathode-anode exchange current density is greatly influenced by the catalytic layer and the fuel cell plate type, the cathode-anode exchange current density adopted in calculation needs to be obtained by experimental test firstly, and then parameter correction such as temperature, pressure and catalyst is carried out;
wherein the reference exchange current density value is obtained using the following formula:
wherein J 0 (T) is the exchange current density [ A/m ] 2 ]；Exchange current density for reference [ A/m ] 2 ]；α c Is the specific surface area of the catalyst [ cm ] 2 /mg]；L c Is the catalyst loading [ mg/cm ] 2 ]，E c For activation energy [ kJ/mol ] -1 ]。
Furthermore, in the method, the mass transfer loss is corrected in a related way, the cathode exchange current density is corrected by introducing a catalytic layer polymer model, and the mass transfer loss and the experimental mass transfer loss can be matched highly by introducing the polymer model, and the result is shown in figure 3.
J cat Exchange current density A/m for cathode 2 ，ζ cat The specific surface area of the cathode catalytic layer is 1/m, s is the saturation of liquid phase, K W For the solubility of oxygen in liquid water, D W For the diffusivity of oxygen in liquid water, r p In order to achieve a catalyst radius of the catalyst,ideal current transport for the cathode, +.>Is the ionic resistance of the cathode catalyst.
Furthermore, the anisotropy of the materials is considered in the diffusion layer and the microporous layer, and the thermal conductivity coefficient used for simulation is a normal pressure condition test result, so that the measured thermal conductivity coefficient needs to be subjected to pressure and porosity correction in the model, and the simulation calculation result is more consistent with the actual situation finally as shown in formulas (3), (4) and (5). The heat conductivity coefficients of the diffusion layer and the microporous layer material are subjected to pressure correction by adopting the following formula:
wherein ε 0 Initial porosity, delta 0 For initial thickness delta y For thickness after compression deformation ρ V Is the bulk density ρ s Is the density of carbon fiber;
taking the anisotropism of porous materials of each layer of the MEA into consideration, carrying out porosity correction on the heat conductivity coefficients of a diffusion layer, a microporous layer and a catalytic layer in the plane direction and the thickness direction:
k eff ＝(1-ε) 1.5 k (5)
in the method, the influence caused by the liquid water in the MEA and the liquid water in the flow channel is considered, the final calculated performance curves of formulas (6), (7) and (8) are very high in coincidence with experimental test results, and as shown in fig. 3, the dissolved phase model is as follows:
wherein ε i Is the porosity of the porous medium, and the porous medium is the porous medium,lambda is the dissolved water content, n d For osmotic resistance coefficient, ++>Is the diffusion coefficient of water content, S λ Generating a water rate for the cathode side reaction of the catalytic layer, S gd For its too water and dissolution water mass exchange rate, S ld The mass exchange rate of liquid water and dissolved water is adopted;
the porous medium liquid phase model is as follows:
wherein ρ is l Is liquid water density, mu l Is liquid hydrodynamic viscosity, K is absolute permeability, K r For relative permeability, p l Is hydraulic water pressure, S gl Mass exchange rates for gaseous water and liquid water;
the runner liquid phase model is:
wherein D is liq Is the diffusion coefficient of liquid water, and the water is mixed with the water,for the flow rate of liquid>Is the gas flow rate.
The foregoing is only a preferred embodiment of the present application, but the scope of the present application is not limited thereto, and any person skilled in the art, who is within the scope of the present application, should make equivalent substitutions or modifications according to the technical scheme of the present application and the inventive concept thereof, and should be covered by the scope of the present application.

Claims (6)

1. A method for establishing a full-area single cell model by 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 two parts of an anode proton exchange membrane and a cathode proton exchange membrane from the center; cutting a proton exchange membrane, an anode catalytic 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 materials into a structure consistent with the anode fluid; cutting a proton exchange membrane, a cathode catalytic layer, a cathode microporous layer, a cathode diffusion layer and a cathode polar plate which are positioned at a cathode by adopting cathode fluid, and processing all the materials into a structure consistent with the cathode fluid;
according to the oxygen reduction kinetics principle and the hydrogen oxidation kinetics principle, bipolar plates are adopted to test the exchange current density of the anode and the cathode respectively, and parameters such as temperature, pressure, catalyst and the like are corrected to obtain reference exchange current density values of the anode and the cathode respectively:
wherein J 0 (T) is the exchange current density [ A/m ] 2 ]；Exchange current density for reference [ A/m ] 2 ]；α c Is the specific surface area of the catalyst [ cm ] 2 /mg]；L c Is the catalyst loading [ mg/cm ] 2 ]，E c For activation energy [ kJ/mol ] -1 ]。
2. The method according to claim 1, characterized in that: and adding an interface between the proton exchange membrane center and the cooling liquid center at the asymmetric position of the structure in the thickness direction, and carrying out data transmission between the two interfaces in an interpolation mode.
3. The method according to claim 1, characterized in that: calculating anode fluid, cathode fluid and cooling liquid fluid of the bipolar plate fluid, and taking the calculation result of the three-cavity fluid as the input condition of calculation of the complex bidirectional serpentine flow channel full-area proton exchange membrane fuel cell model.
4. A method according to claim 3, characterized in that: correcting the cathode exchange current density and the transmission loss by adopting a catalytic layer polymer model:
J cat exchange current density A/m for cathode 2 ，ζ cat The specific surface area of the cathode catalytic layer is 1/m, s is the saturation of liquid phase, K W For the solubility of oxygen in liquid water, D W For diffusion of oxygen in liquid waterRate, r p In order to achieve a catalyst radius of the catalyst,ideal current transport for the cathode, +.>Is the ionic resistance of the cathode catalyst.
5. The method according to claim 4, wherein: pressure and porosity correction of the measured thermal conductivity coefficients during modeling, wherein the diffusion layer and microporous layer materials thermal conductivity coefficients are pressure corrected:
wherein ε 0 Initial porosity, delta 0 For initial thickness delta y For thickness after compression deformation ρ V Is the bulk density ρ s Is the density of carbon fiber; taking the anisotropism of porous materials of each layer of the MEA into consideration, carrying out porosity correction on the heat conductivity coefficient:
k eff ＝(1-ε) 1.5 k (5)。
6. the method according to claim 5, wherein: combining the dissolved phase model, the runner liquid phase model and the porous medium liquid phase model to obtain a water generation and transportation model:
dissolved phase model:
wherein ε i Is the porosity of the porous medium, and the porous medium is the porous medium,lambda is the dissolved water content, n d For osmotic resistance coefficient, ++>Is the diffusion coefficient of water content, S λ Generating a water rate for the cathode side reaction of the catalytic layer, S gd For its too water and dissolution water mass exchange rate, S ld The mass exchange rate of liquid water and dissolved water is adopted;
the porous medium liquid phase model is as follows:
wherein ρ is l Is liquid water density, mu l Is liquid hydrodynamic viscosity, K is absolute permeability, K r For relative permeability, p l Is hydraulic water pressure, S gl Mass exchange rates for gaseous water and liquid water;
the runner liquid phase model is:
wherein D is liq Is the diffusion coefficient of liquid water, and the water is mixed with the water,for the flow rate of liquid>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
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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
CN113921847B (en) * 2021-08-23 2023-03-31 东风汽车集团股份有限公司 Fuel cell stack fluid flow analysis modeling method and device
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