Performance Analysis Based on Sustainability Exergy Indicators of High-Temperature Proton Exchange Membrane Fuel Cell

Abstract

Based on finite-time thermodynamics, an irreversible high-temperature proton exchange membrane fuel cell (HT-PEMFC) model is developed, and the mathematical expressions of exergy efficiency, exergy destruction index ($EDI$), and exergy sustainability indicators ($ESI$) of HT-PEMFC are derived. According to HT-PEMFC model, the influences of thermodynamic irreversibility on exergy sustainability of HT-PEMFC are researched under different operating parameters that include operating temperatures, inlet pressure, and current density. The results show that the higher operating temperature and inlet pressure of HT-PEMFCs is beneficial to performance improvement. In addition, the single cell performance gradually decreases with increasing current density due to the presence of the irreversibility of HT-PEMFC.

1. Introduction

In recent years, proton exchange membrane fuel cells (PEMFCs) have been regarded as clean and promising energy conversion devices [1,2,3,4,5,6]. PEMFC has been widely applied in the vehicle and aerospace fields because of its low noise, zero-emission, fast start-up, and high reliability [7,8,9,10]. PEMFC can be divided into low-temperature PEMFC (LT-PEMFC, 60–80 °C) and HT-PEMFC (120–200 °C) according to the operating temperature. Compared with LT-PEMFC, HT-PEMFC has the advantage of accelerated reaction kinetic at the electrode and heat management system [11,12,13,14,15], higher CO tolerance [16,17,18], and higher quality waste heat [19,20].

The present research on HT-PEMFC mainly included material [21,22,23,24] improvement and methods of preparation [25,26,27,28,29]. Araya et al. [30] reviewed the current status of research on the operational aspects and performance of HT-PEMFCs. It focused on phosphoric acid-doped polybenzimidazole (PBI)-based HT-PEMFCs and reviewed their single-cell, stack, and system-level designs. Techniques for cell health status diagnosis, cell failure prevention, and cell life extension are also discussed. Gao et al. [31] proposed a numerical model of a HT-PEMFC stack waste heat recovery system and verified the model based on experiments to determine the main variables before optimizing the system configuration to recover heat from the exhaust gas. The results showed that model accuracy and system configuration optimization are crucial. Esfeh et al. [32] established the PEMFC model and conducted a parametric study. The results showed that the temperature increase reduced the concentration loss in all the temperature ranges, but reduced the activation overpotential below 80 °C. Miansari et al. [33] investigated the effects of parameters such as pressure, temperature, anode, and cathode channel depth on the performance of PEMFCs. The results showed that increasing the operating temperature and pressure can improve the cell performance, exergy efficiency and reduce the irreversibility of the cell. Li et al. [34] established a model of irreversible proton exchange membrane fuel cell including polarization loss and leakage current loss based on finite time thermodynamics. According to the model, the influence of the operating temperature, operating pressure, and water content of the proton exchange membrane on the optimal performance of the irreversible proton exchange membrane fuel cell is investigated. The results showed that when the operating temperature is increased, the optimized performance of the proton exchange membrane fuel cell in terms of output power, output efficiency, ecological objective function, and ecological coefficient of performance will be improved.

Guo et al. [35] researched the power, exergy, and ecological analysis of HT-PEMFC based on a phosphoric acid-doped polybenzimidazole membrane, and the experimental results showed that the operating temperature and doping level have a greater impact on improving the performance of HT-PEMFC than the operating pressure and relative humidity. Khan et al. [36] proposed a semi-empirical model of HT-PEMFC, taking into account hydrogen pressure, ambient temperature, pressure, and load resistance, and researched the influence of these parameters on cell performance. The results showed that when the ambient temperature increases and the pressure decreases, the output voltage of HT-PEMFC decreases. Nalbant et al. [37] researched the exergy performance evaluation of an integrated CHP system based on HT-PEMFC. The results showed that when the operating temperature of HT-PEMFC increases, the power and CHP efficiency of the system improved, and the stoichiometric ratio of the anode is the most influential parameter on system performance.

Toghyanni et al. [38] conducted an economic analysis on the energy efficiency of HT-PEMFC by using a 3D non-isothermal model and researched the influences of operating temperature, cathode pressure, the thickness of gas diffusion layer, and membrane on the exergy efficiency and exergy cost. The research results showed that when the operating temperature and thickness of the membrane increased from 363 K to 393 K and 50 μm to 183 μm, respectively, the exergy cost of hydrogen decreased exergy efficiency is slightly improved and the higher operating pressure will reduce the exergy cost of hydrogen. Ye et al. [39] researched exergy analysis of the HT-PEMFC system. The research results showed that the increasing the inlet relative humidity and pressure effects on the improvement of the two kinds of system performance were indistinctive, further enhancing the efficiency of the energy exchange of the fuel cell and reducing the irreversibility of fuel cells is the key point of further improve the system efficiency.

In recent years, PEMFC had made some progress in exergy-related research. Ay et al. [40] researched the changes of exergy efficiency under different working conditions. The research results showed that the exergy efficiency of PEMFC decreased with the increase of thickness of the membrane and current density. In the case of the same thickness of the membrane, the exergy efficiency increased with the increase of cell operating pressure and the decrease of current density. Therefore, in order to improve the performance of PEMFC, the lower thickness of the membrane, lower current density, and higher cell operating pressure should be selected under the condition of constant cell temperature. Li et al. [41] researched exergy performance analysis and optimization of HT-PEMFC. The research results showed that increasing the inlet pressure and doping level can improve energy efficiency. Midilli et al. [42] proposed some new exergy-based indicators for PEMFC research through research, which are expected to quantify the sustainable concept of PEMFC.

In this paper, firstly, the irreversibility of the HT-PEMFC is analyzed according to finite time thermodynamics. A mathematical model that considers the irreversible polarization loss and leakage current loss is established. Secondly, exergy analysis is carried out on the HT-PEMFC operation process to research the exergy sustainability index of HT-PEMFC under different operating parameters. At the same time, the influences of different operating temperatures, the thickness of the membrane, and the current density on exergy sustainability index and cell operation process are researched. The results of the parametric study can provide directions for future improvements in the operating conditions and design of HT-PEMFC.

2. Results and Analysis

The relevant parameters in the HT-PEMFC model are shown in Table 1. The thermodynamic irreversibility and exergy sustainability of HT-PEMFC with different operating parameters are studied according to the input parameters.

Table 1.

Relevant data of HT-PEMFC.

Parameter	Value
$\mathrm{Current}\mathrm{Density}, I ({\mathrm{Am}}^{-2}$)	0–20,000 [35]
$\mathrm{Operating}\mathrm{Temperature}, T$ (K)	393–473 [35]
$\mathrm{Intake}\mathrm{Pressure},P_{H_2}, P_{O_2}\left(\mathrm{atm}\right)$	1–3 [35]
$\mathrm{Electronic}\mathrm{Number},n$	2
$\mathrm{Faraday}\mathrm{Constant},F \left({\mathrm{Cmol}}^{-1}\right)$	96,485
$\mathrm{Ambient}\mathrm{Temperature},T_0$(K)	298.15
$\mathrm{Transfer}\mathrm{Coefficient},\alpha$	0.25 [35]
$\mathrm{Gas}\mathrm{Constant},R$	8.3143

Figure 1a compared the predicted model potential and experimental data [43] of HT-PEMFC at 423 K and 448 K ($P$ = 1 atm; $RH=$ 0.38%; $DL$ = 5.6). As can be seen from Figure 1a, the error between the predicted and experimental data is about 6%. This shows that the model has a relatively good accuracy. Figure 1b shows the reversible potential, the polarization loss potential, and the output voltage versus the current density. It can be seen that the reversible potential is a constant that is unrelated to the current density. All three kinds of overpotentials increase with the increase of current density, where the concentration overpotential increases exponentially, the activation overpotential increases logarithmically, and the ohmic overpotential increases less. In the low current density section, the rapid growth of the activation overpotential leads to a decrease in the output voltage. In the higher current density section, the output voltage decreases mainly due to the rapid increase in the concentration overpotential.

Figure 1.

(a) Comparisons of the predicted model potential and the experimental data; (b) Curves of the potential and output voltage versus the current density.

As shown in Figure 2a, exergy efficiency and power density increase slightly with the increase of operating temperature. From the perspective of electrode reaction kinetics, the increase of temperature is beneficial to increasing the proton conductivity and largely reduces the irreversible loss due to the polarization phenomenon. From the molecular viewpoint, the increase of temperature is beneficial to speed up the rate of proton motion and reaction, shorten the proton transport time, and thus improve the performance of HT-PEMFC. In the low current density section, the exergy efficiency stays at a high level and decreases when the current density increases to the higher section. In addition, the corresponding efficiency and power density do not reach the maximum value at the same moment when the power density or the exergy efficiency obtain the maximum value, respectively. In Figure 2b, both the power density and exergy efficiency increase significantly with the increase of the inlet pressure. When the inlet pressure increases, the gas concentration also increases, which improves the gas transport inside the fuel cell and makes the kinetic performance of the fuel cell improved. In the low current density interval, increasing the pressure is not obvious to improve the output performance of the fuel cell, but will cause an increase in the parasitic power due to the increase in the power of the air compressor, thus causing a decrease in system efficiency; in the medium current density interval, the effect of increasing the pressure on the output performance is gradually improved, gradually offsetting, or even higher than the parasitic power consumption that is brought by the air compressor; in the high current density interval, the higher the pressure, the higher the obstruction of protons through the membrane. The higher the pressure, the smaller the obstruction of protons through the membrane, and the mass transfer conditions are improved, leading to the reduction of ohmic loss, and the better the output performance of the fuel cell system.

Figure 2.

The effect of operating parameters on exergy efficiency and power density $(RH=0.038\%,$ $t_{mem}=0.002 \mathrm{cm},DL=10$). (a) different $T$; (b) different $P$.

2.1. Exergy Destruction Index ($EDI$)

Figure 3a,b show the effects of operating temperature and inlet pressure on $EDI$. In Figure 3a, the $EDI$ decreases with the increase of the operating temperature when the operating temperature increases. From the energy balance point of view, the increase in operating temperature improves the operating environment of the fuel cell and reduces the irreversible exergy loss due to polarization losses, which makes the HT-PEMFC have less impact on the environment and therefore the $EDI$ is reduced. In Figure 3b, the increase in the inlet pressure leads to an increase in the $EDI$. The increase in the inlet pressure leads to a subsequent increase in the gas concentration, which improves the gas transport conditions inside the fuel cell and reduces the hindrance of the fuel cell in the electrochemical reaction. In addition, the increase of $EDI$ with the temperature increase is relatively large. In the low current density section, the enhancement of $EDI$ with temperature and pressure is relatively small, while in the high current density section, $EDI$ is more affected by temperature. According to Equations (26), (28), (30), and (31), the HT-PEMFC at high current density is in the operation state of high output power and low assembly efficiency, which is a waste of energy and not environmentally friendly.

Figure 3.

The effect of operating parameters on exergy destruction index and power density $(RH=0.038\%,$ $t_{mem}=0.002 \mathrm{cm},DL=10$). (a) different $T$; (b) different $P$.

2.2. Exergy Sustainability Index ($ESI$)

In Figure 4a, $ESI$ decreases with increasing current density. When the temperature is low, the activation loss of the HT-PEMFC is higher, and the resulting exergy loss and exergy dissipation are higher. When the temperature increases, the catalyst activity in the HT-PEMFC increases, the activation loss decreases, the output voltage increases, and the output performance of the fuel cell is improved. In Figure 4b, as the inlet pressure increases, increasing the pressure causes a slight decrease in the $ESI$ at low current density, because the exergy loss and exergy dissipation due to parasitic power consumption from the air compressor are higher than the output performance improvement at this point. In the medium current density section and in the high current density section, increasing the inlet pressure and increasing the gas concentration, the output performance of the HT-PEMFC is improved at this time, and the $ESI$ increases with the increase in the inlet pressure.

Figure 4.

The effect of operating parameters on the exergy sustainability index and power density $(RH=0.038,$ $t_{mem}=0.002 \mathrm{cm},DL=10$). (a) different T; (b) different $P$.

2.3. Exergy Sustainability Indicators

Figure 5a,b show the curves of $ESI,EDI$, ${\eta }_{ex}^{fc}$ and net output power at the thickness of membrane of 0.002 cm, operating pressure of 3.039 × 10⁵ Pa, the operating temperature of 413 K and current density of 0–2 × 10⁴ A/m². As the exergy efficiency increases, the $EDI$ gradually decreases and the $ESI$ increases. This indicates that the damage to the environment of the cell is gradually reduced when the HT-PEMFC continued to operate and the operating temperature is increasing until it is stable and also verifies the sustainability of the HT-PEMFC. As can be seen in Figure 5b, when the exergy efficiency and $ESI$ increase, the output power density does not keep increasing continuously, which indicates that the best performance of HT-PEMFC requires us to further balance the indicators and perform multi-objective optimization of each indicator to obtain the optimal output power.

Figure 5.

(a) Relationship between $ESI$ and $EDI$ at different exergy efficiency; (b) Relationship between $ESI$ and $P$ at different exergy efficiency.

3. Thermodynamic Model

3.1. Working Principle of HT-PEMFC

The reaction principle of PEMFC is as follows: the hydrogen tank supplies hydrogen to the anode, and the air compressor supplies oxygen to the cathode. Then, the hydrogen is converted to hydrogen ions and electrons in the anode, the hydrogen ions pass through the proton exchange membrane, and the electrons flow through the external load to the cathode, where the hydrogen ions and oxygen atoms and electrons combine to form H₂0 [44]. The electrochemical reaction formula of PEMFC is as follows:

$$\mathrm{anode}\mathrm{reaction}:{\mathrm{H}}_2\to 2{\mathrm{H}}^{+}+2{\mathrm{e}}^{-}$$ (1)

$$\mathrm{Cathodic}\mathrm{reaction}:2{\mathrm{H}}^{+}+\frac{1}{2}{\mathrm{O}}_2+2{\mathrm{e}}^{-}\to {\mathrm{H}}_2\mathrm{O}+\mathrm{heat}$$ (2)

$$\mathrm{Total}\mathrm{reaction}:{\mathrm{H}}_2+\frac{1}{2}{\mathrm{O}}_2\to {\mathrm{H}}_2\mathrm{O}+\mathrm{heat}+\mathrm{electricity}$$ (3)

In HT-PEMFC, phosphoric acid is usually used instead of water for humidification. The principle of mass transfer in the anode, cathode, and membrane can be expressed as:

$$\mathrm{anode}\mathrm{reaction}:{\mathrm{H}}_2{\mathrm{PO}}_4^{-}+{\mathrm{H}}^{+}={\mathrm{H}}_3{\mathrm{PO}}_4$$ (4)

$$\mathrm{membrane}:{\mathrm{H}}_3{\mathrm{PO}}_4+\mathrm{PBI}={\mathrm{H}}_2{\mathrm{PO}}_4^{-}+\mathrm{PBI}·{\mathrm{H}}^{+}$$ (5)

$$\mathrm{Cathodic}\mathrm{reaction}:\mathrm{PBI}·{\mathrm{H}}^{+}=\mathrm{PBI}+{\mathrm{H}}^{+}$$ (6)

3.2. Reversible Potential of HT-PEMFC

For exergy analysis and research, the changes of exergy sustainability indexes under different working conditions, the following assumptions should be considered for HT-PEMFC:

1. The fuel cell operates in a steady state.

2. The reactants are ideally compressible gases and there are no reactants left after the full reaction.

3. The operating pressure and relative humidity are constant during the reaction.

4. The effect of the generated water on the relative humidity is not considered.

5. Only physical and chemical exergy is considered, no potential exergy and kinetic exergy are considered.

6. Leakage current loss and polarization loss are considered.

In a HT-PEMFC thermodynamic system, the potential of an electrochemical reaction depends on the Gibbs free energy of fuel [44]. The operating temperature, pressure, and concentration of the reaction gas affect the Gibbs free energy. For HT-PEMFC, the reversible output voltage is as follows:

$$V_{rev}=E_r^0+\frac{-18.449-0.01283T}{F}\left(T-T_0\right)+\frac{RT}{nF}\ln (\frac{p_{H_2}{p}_{O_2}^{0.5}}{p_w})$$ (7)

where $E_r^0=1.185$ is the reversible potential, $T$ is the operating temperature of HT-PEMFC, $T_0$ is the ambient temperature, $R$ is the gas constant, $p_{H_2}$ is the inlet pressure of hydrogen, $p_{O_2}$ is the inlet pressure of oxygen, and $p_w$ is the pressure of water vapor discharge.

3.3. Overpotential of HT-PEMFC

The HT-PEMFC shows polarization phenomena due to its electrochemical reactions and internal resistance. The polarization phenomenon means that during the electrochemical process of HT-PEMFC, energy must be consumed to overcome the resistance, such as the diffusion of anode and cathode gases and the dissolution of active gases, such as proton adsorption reactions. This energy consumption will reduce the actual output voltage and the electrode potential will be lower than the ideal reversible potential. Polarization phenomena cause three types of polarization overpotentials: activation overpotential, ohmic overpotential and concentration overpotential.

The electrochemical reaction rate of HT-PEMFC affects the activation over potential. The slower the reaction rate, the more severe the polarization loss and the greater the activation overpotential. In addition, the catalysts used at the cathode and anode poles are also related to the activated overpotential. The better the catalyst activity, the lower the activation overpotential. The activation overpotential $V_{act}$ can be expressed as followed [45]:

$$V_{act}=\frac{RT}{2\alpha F}\ln (\frac{I+I_{leak}}{I_0})$$ (8)

where $I_{leak}$ is the leakage current density, $I_0$ is the exchange current density, and α is the transfer coefficient. The expression of $I_0$ is as follows:

$$\ln (I_0)=2.2266\times \frac{1000}{T}-0.4959$$ (9)

For HT-PEMFC, the loss due to resistance between cell components is called ohmic overpotential. Ohmic resistance consists of two main parts: resistance that is caused by the ion flow through the proton exchange membrane in the electrolyte and resistance that is caused by the flow of electrons through the electrode ends.

The ohmic potential $V_{ohm}$ can be expressed as follows [46]:

$$V_{ohm}=I\left(\frac{l_m}{K_m}+\frac{2l_d}{{\sigma }_d}\right)$$ (10)

where $l_m$ is the thickness of the membrane, $K_m$ is proton conductivity, $l_d$ is the thickness of the diffusion layer, and ${\sigma }_d$ is the electron conductivity.

Proton conductivity $K_m$ needs to consider the influence of cell operating temperature, phosphoric acid doping level of the membrane, and the relative humidity, and its expression is as follows [47]:

$$K_m=\frac{a\times b}{T}\times ex{p}^{\frac{-c}{RT}}$$ (11)

$$a=68D{L}^3-6324D{L}^2+65750\mathrm{DL}+8460$$ (12)

$$b=\{\begin{array}{c}1+\left(0.01704T-4.767\right)RH, 373.15K\le T\le 413.15K\\ 1+\left(0.1432T-56.89\right)RH, 413.15K<T\le 453.15K\\ 1+\left(0.7T-309.2\right)RH, 453.15K<T\le 473.15K\end{array}$$ (13)

$$c=-619.6DL+21750$$ (14)

where $DL$ is the doping level of phosphoric acid in the proton exchange membrane and $RH$ is the relative humidity of the reaction gas [48].

During the operation of HT-PEMFC, when the reaction gas is not provided in time, the electrode reaction surface cannot maintain the concentration of the reaction gas and concentration polarization will occur.

The expression of concentration overpotential $V_{conc}$ is as follows [49]:

$$V_{conc}=\left(1+\frac{1}{\alpha }\right)\frac{RT}{nF}\ln \frac{I_L}{I_L-I}$$ (15)

where $I_L$ is the limiting current density [46].

The irreversible output voltage $V$ of HT-PEMFC can be expressed as [50]:

$$\begin{gathered} V=V_{rev}-V_{act}-V_{ohm}-V_{conc} \\ =1.185-\left(1.91\times {10}^{-4}+1.33\times {10}^{-7}T\right)\left(T-298.15\right)+4.13 \\ \times {10}^{-5}T\ln \frac{P_{H_2}{P_{O_2}}^{0.5}}{0.0243}-1.72\times {10}^{-5}\times \\ T\ln \frac{I+88458.17·ex{p}^{\frac{-2342.9}{T}}}{3.95\times {10}^{-6}{T}^3-0.00424T^2+1.523T-183} \\ -I\left(\frac{l_{m}T}{a·b·ex{p}^{\frac{74.5\mathrm{DL}-2616}{T}}}+9.8\times {10}^{-6}\right) \end{gathered}$$ (16)

3.4. Exergy Balance Model

Considering the above assumptions, the exergy equilibrium model of HT-PEMFC is shown in Figure 6. The exergy balance expression of HT-PEMFC can be obtained by [51,52,53]:

$$E{x}_{in}^{fc}=E{x}_{d,out}^{fc}+E{x}_{w,out}^{fc}+E{x}_d^{fc}$$ (17)

Figure 6.

Exergy balance of proton exchange membrane fuel cell.

In the proton exchange membrane fuel cell system, the total exergy input is:

$$E{x}_{in}^{fc}=E{x}_{H_2,in}+E{x}_{O_2,in}$$ (18)

In this paper, exergy waste that is generated by hydrogen, oxygen, water, and heat that is discharged from the system can be divided into two categories: recoverable exergy waste and unrecoverable exergy waste [54].

$$E{x}_{w,out}^{fc}=E{x}_{rw}^{fc}+E{x}_{uw}^{fc}$$ (19)

The recoverable exergy waste is:

$$E{x}_{rw}^{fc}=n_{O_2,out}\times {\left(ex\right)}_{O_2}^{ch}+n_{O_2,out}\times {\left(ex\right)}_{O_2}^{ch}$$ (20)

The unrecoverable exergy waste is:

$$\begin{gathered} E{x}_{uw}^{fc}=\left(n_{H_2,out}\times {\left(ex\right)}_{H_2}^{ph}+n_{O_2,out}\times {\left(ex\right)}_{O_2}^{ph}+n_{H_{2}O,out}\times e{x}_{H_{2}O}^{ph}\right) \\ +Q_{w,out}^{fc}\times \left(1-\frac{T_0}{T}\right)\times r_{hl} \end{gathered}$$ (21)

Physical exergy and chemical exergy are expressed as followed [55]:

$${\left(ex\right)}^{ph}=C_p{T}_0[\frac{T}{T_0}-1-\ln (\frac{T}{T_0})+\ln (\frac{p}{p_0}{)}^{\frac{k-1}{k}}]$$ (22)

$${\left(ex\right)}^{ch}={\displaystyle \sum }{x}_n·e_n^{ch}+R{T}_0{\displaystyle \sum }{x}_n·\ln x_n$$ (23)

where $C_p$ is the constant specific heat of the gas, $T_0$ is the ambient temperature, $p_0$ is the pressure, $K$ is the specific heat rate, $x_n$ is the mole fraction of the component, and $e_n^{ch}$ is the chemical exergy of each composition.

The total exergy of the desired output is:

$$E{x}_{d,out}^{fc}=W_{fc}$$ (24)

$$W_{fc}=Vi=(V_{rev}-V_{act}-V_{ohm}-V_{conc})i$$ (25)

Exergy dissipation can be obtained from the equilibrium equation of PEMFC exergy

$$E{x}_d^{fc}=E{x}_{in}^{fc}-E{x}_{d,out}^{fc}-E{x}_{w,out}^{fc}$$ (26)

3.5. HT-PEMFC Exergy Sustainability Index Derivation Process

The exergy efficiency of HT-PEMFC is defined as the ratio of effective exergy output to total exergy output, as follows [56]:

$${\eta }_{ex}^{fc}=\frac{E{x}_{d,out}^{fc}}{E{x}_{in}^{fc}}$$ (27)

Exergy dissipation will occur during HT-PEMFC operation due to heat transfer and polarization. The waste exergy ratio expression is as follows:

$$\begin{gathered} r_{we}^{fc}=r_{rw}^{fc}+r_{uw}^{fc} \\ {r}_{rw}^{fc}=\frac{E{x}_{rw}^{fc}}{E{x}_{in}^{fc}} \end{gathered}$$ (28)

$$r_{uw}^{fc}=\frac{E{x}_{uw}^{fc}}{E{x}_{in}^{fc}}$$ (29)

The irreversibility of HT-PEMFC during operation will lead to the increase of exergy dissipation. Exergy dissipation is used to describe the irreversibility of the operation process and the exergy dissipation rate is defined as:

$$f_{exd}^{fc}=\frac{E{x}_d^{fc}}{E{x}_{in}^{fc}}$$ (30)

The exergy destruction index ($EDI$) can reflect the impact of unrecoverable exergy loss and exergy dissipation on the environment. Its expression is as follows:

$$EDI=(r_{uw}^{fc}+f_{exd}^{fc}) \frac{1}{{\eta }_{ex}^{fc}}$$ (31)

According to the reaction equation of PEMFC, the reaction products are only water, heat, and electric energy. In practical application, due to the irreversibility of cells, some ${\mathrm{H}}_2$ and ${\mathrm{O}}_2$ will not be used, which reduces the exergy stability of PEMFC, which is the main reason for exergy dissipation. In addition, power output also affects exergy stability. Therefore, the exergy stability coefficient of PEMFC is defined as:

$$f_{est}^{fc}=\frac{E{x}_{d,out}^{fc}}{\left(E{x}_{d,out}^{fc}+E{x}_{w,out}^{H_2}+E{x}_{w,out}^{O_2}+E{x}_d^{fc}\right)}$$ (32)

The Environmental Benign Index ($EBI$) indicates the environmental suitability of HT-PEMFC. The higher the EBI of HT-PEMFC, the better it is for the environment. The environmental adaptability of HT-PEMFC can generally be improved by reducing $EDI$. Its expression is as follows:

$$EBI=\frac{{\eta }_{ex}^{fc}}{(r_{uw}^{fc}+f_{exd}^{fc}) }$$ (33)

The exergy sustainability index ($ESI$) is as follows:

$$ESI=\frac{{\eta }_{ex}^{fc}}{(r_{uw}^{fc}+f_{exd}^{fc})}\times \frac{E{x}_{d,out}^{fc}}{\left(E{x}_{d,out}^{fc}+E{x}_{w,out}^{H_2}+E{x}_{w,out}^{O_2}+E{x}_d^{fc}\right)}$$ (34)

4. Conclusions

In this paper, a HT-PEMFC model is established based on finite time thermodynamics, which takes into account polarization losses and leakage current loss. In order to improve the sustainability of HT-PEMFC and reduce the negative impact on the environment, the exergy sustainability index of HT-PEMFC is studied to provide improvement directions for PEMFC in engineering applications. Some main conclusions are drawn through graphical and theoretical analysis as follows:

1. The reliability of the HT-PEMFC model is proved by comparing the model with the experimental data. Through the parameterization studies, the suitable increase of temperature is beneficial to the improvement of HT-PEMFC output performance. With the decrease of the plasmonic membrane thickness, the output performance is improved.

2. At low exergy efficiency, the output power of HT-PEMFC takes the maximum value and starts to decrease when the exergy efficiency exceeds 0.27.

3. The operating conditions of HT-PEMFC can be improved by increasing the inlet pressure, changing the diffusion rate of the gas, appropriately increasing the operating temperature, and using thin proton exchange membranes.

The obtainable conclusion may provide some directions and references for future research that is related to the influence of parameters on HT-PEMFC performance. In the future, the optimization method for output performance of HT-PEMFC can be further researched.

Author Contributions

The collection of materials and summarization of this article is done by X.G., Y.L. and D.L. The simulation and analysis are done by Y.L., B.X. and Z.M. The conceptual ideas, methodology, and guidance for the research are provided by Z.M. All authors have read and agreed to the published version of the manuscript.

Institutional Review Board Statement

Not applicable.

Informed Consent Statement

Not applicable.

Data Availability Statement

Not applicable.

Conflicts of Interest

The authors declare no conflict of interest.

Funding Statement

We gratefully acknowledge the financial support of the National Natural Science Foundation of China (No. 51306079 and 51176069), the Jiangsu Provincial Key Research and Development Program (No. BE2017008), and Scientific Research Foundation of Nanjing Forestry University (No. GXL2018004).