Numerical Simulation of Full-Scale Cell and Stack at Very High Current Density: Influence of Heat and Liquid Water Saturation
Authors: Tsukamoto Takayuki , Aoki Tsutomu , Kanesaka Hiroyuki , Komiyama Keisuke , Takayama Tsutomu , Motegi Haruki , Takayama Ryo , Tanaka Shoichi , Yoneda Masakazu 
Published: December 2020

In order to further improve power density of PEFC stack, the operations at high current density and high voltage are required in addition to downsizing. To achieve 6.0kW/L around 2030 formulated by NEDO in Japan, the extreme targets such as 0.7V@3.0A/cm2 and 0.66V@3.8A/cm2 being proposed. However, such operations cannot be achieved by the currently common MEA and GDL, and it is difficult to experimentally investigate the issues of internal states at such very high current density. In the present study, we carried out simulation of fuel cell performance by our originally developed software P-Stack. The results indicated that improving GDL properties is very important in addition to enhance performances of PEM and catalyst layer.
The most important feature of this software is the employed macroscopic model comprehensively dealing with all the relevant transport phenomena coupled with electrochemical reactions. In anode and cathode channels and GDLs, mass transport of gas and liquid phase are solved by considering the two-phase fluid dynamics with taking into account the effects of phase changing. Here mass transport is coupled with heat and chemical species transport equations. Those all transport phenomena are coupled with electrochemical reactions in the MEA. Electrochemical reactions are modeled by Butler-Volmer equation. The parameters in the equation and other models need to be fitted to reproduce the fuel cell performance with target MEA and GDL for different operating conditions.
First, we assembled 1cm2 cell with a typical MEA (PEM: Nafion NR211, Ca/An CL: TKK TEC10E50E 0.3mgPt/cm2, Ca/An GDL: SGL28BC), and then measured I-V and I-R curves under various operating conditions and transient behavior when current density is rapidly increased assuming GDL flooding. These experiments were carried out with massive flow rate and constant temperature, and therefore it can be assumed the in-plane distributions are uniform. In order to reproduce the measured results of the 1cm2 cell by simulation, we second fitted the various simulation parameters including electrochemical parameters and mass transport resistance of cathode catalyst layer and the parameters related to GDL flooding. As a validation of the fitted parameters, we compared measured and calculated I-V and I-R curves for 25cm2 dual serpentine cell with the reference MEA. These calculated results are in good agreement with the measured values.
300cm2 cell with reference MEA were calculated under the conditions: anode RH is 80 %, cathode RH is 40%, cathode stoichiometry is 2.5, back pressure is 150kPa(g) and coolant flow rate is 1.0L/min/cell. The results indicated that the cell voltage decreases more than 200mV at 3.0A/cm2 due to the influence of GDL flooding. We also calculated 300cm2 cell with hypothetically modified MEA in which proton conductivity, catalyst activity, less mass transport resistance, through-plane electric/thermal conductivity of GDL and gas diffusivity of GDL are highly enhanced to achieve 0.7V@3.0A/cm2. Although the details will be discussed in the presentation, it was indicated that the further improvement of gas diffusivity and through-plane thermal conductivity are very important to reduce the GDL flooding, respectively. In addition, short stacks with 30 cells were also calculated to discuss distributions along the stack direction.

References

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