A direct borohydride fuel cell with a polymer fiber membrane and non-noble metal catalysts.

Polymer electrolyte membranes (PEM) and Pt-based catalysts are two crucial components which determine the properties and price of fuel cells. Even though, PEM faces problem of fuel crossover in liquid fuel cells such as direct methanol fuel cell (DMFC) and direct borohydride fuel cell (DBFC), which lowers power output greatly. Here, we report a DBFC in which a polymer fiber membrane (PFM) was used, and metal oxides, such as LaNiO₃ and MnO₂, were used as cathode catalysts, meanwhile CoO was used as anode catalyst. Peak power density of 663 mW·cm⁻² has been achieved at 65°C, which increases by a factor of 1.7-3.7 compared with classic DBFCs. This fuel cell structure can also be extended to other liquid fuel cells, such as DMFC.

Fuel cells are promising power-generation technology for automotive applications, which convert chemical energy directly into electricity while causing little pollution. A direct borohydride fuel cell (DBFC) is a kind of liquid fuel cell, which has advantages of high open circuit voltage (1.64 V), high fuel energy density (9.3 Wh·g−1 for NaBH4 and 6.5 Wh·g−1 for KBH4), and fast borohydride oxidation reaction (BOR) kinetic1. In DBFC, the cell reaction principle is as follows:

Nafion membrane, polymer electrolyte membrane (PEM), is indispensable in fuel cells23, which provides electric insulator between anode and cathode and prevents reactant crossover from the anode to the cathode. However, crossover is still a serious problem due to the diffusion and osmotic drag that lower the power output by maximum up to 50% in liquid fuel cells4. Much research has been conducted on the details of the transport of protons or ions through the polymer matrix and on novel methods of improving its properties, but the crossover has not yet been solved as well as the cost of the PEM45.

The cost of noble metal catalyst is another factor limiting fuel cells commercialisation. According to United States Department of Energy's (DOE's) forecasts in 2007, platinum-based catalysts alone would account for 38–56% of the cost in a PEM fuel cell stack6. The cathode consumes around 90% of platinum catalyst used in both anode and cathode due to its sluggish oxygen reduction reaction (ORR) kinetics7. Therefore, non-Pt-based catalysts have been greatly studied. Recently, great progress has been achieved in this field. It was found that Co-N-C and Fe-N-C type complexes, which were made by pyrolyzing transition metal precursors with nitrogen-containing precursors supporting on conductive polymer8 or highly microporous carbon9 or metal-organic-framework10, have catalytic activity for the ORR comparable with state-of-the-art Pt-based catalyst. Although the performance and stability of Pt-based catalysts have been greatly improved in H2/O2 PEM fuel cells111213, its efficiency in DBFCs is still in a low level. The peak power densities ranged at 20–200 mW·cm−2 when Pt or Pt-based catalysts are used23, while they were in ca. 1,000 mW·cm−2 when in H2/O2 PEM fuel cells. Crossover is the main reason for this phenomenon. Pt-based catalysts promote ORR and BOR simultaneously when liquid fuel permeates through PEM and arrives in cathodes14, thus cathode efficiency is greatly reduced. It was found that some non-noble metal catalysts for ORR have excellent tolerance with respect to borohydride, including EuO215, MnO216, La2O317, CeO218, Fe/CoPc1920 and perovskite-type oxides (LaNiO3, LaCoO3)2122. However, their peak power densities were lower than 120 mW·cm−2 at ambient temperatures, which are much lower than that of PEMFCs. Therefore, improving the output of DBFCs is one of the most important targets as well as reducing costs.

Results

In this paper, we fabricated a DBFC with polymer fiber membrane (PFM) as a separator replacing of polymer electrolyte membrane (PEM). Figure 1a shows the structure of the DBFC with the PFM (DBFC-PFM). In the anode (2 in figure 1a), CoO was chosen as catalyst, which also had been used in our previous work23. It is a merit of DBFCs that anodic catalysts can also be some non-noble metals such as hydrogen storage alloys and some other metallic compounds242526.

Figure 1

The structure of DBFC with PFM.

(a) schematic structure of DBFC with PFM, 1 end plate with fuel container; 2 anode; 3 polymer fiber membrane (PFM); 4 cathodic active layer; 5 gas diffusion layer; 6 end plate with oxygen flow field. The photograph (b) and SEM image (c) of the PFM are shown.

The fiber materials in the PFM (3 in figure 1a) can be polypropylene or polyamide or polyvinyl alcohol. The photograph and scanning electron microscopy (SEM) image of the PFM are shown in figure 1b and figure 1c, respectively. The PFM is a permeable membrane and it just keeps the cathode and anode non-contacted to prevent short-circuits. The fibers in the membrane are neutral and there are no polarity groups grafted on the main chains in fiber. The pores and gaps between fibers allow liquid fuel and ions transporting or moving through the PFM freely. It has a good wetting nature and is easy to be saturated by liquid solution. So the PFM in DBFCs acts as a very thin liquid electrolyte layer and allows the anions and cations, including BH4−, OH− and Na+/K+, to cross freely. In this situation, it is necessary for cathodic catalysts to have excellent tolerance to the poison of BH4− and good stability in alkaline solution. The cathodic catalysts (LaNiO3, MnO2, La2O3 and CeO2) used in this study have been proved stable enough in alkaline solution and do not react with BH4− 16171822.

In addition, a gas diffusion layer (5 in figure 1a) which was made by acetylene black and polytetrafluoroethylene (PTFE) was pressed with the cathodic active layer, which can efficiently prevent cathode-over-flood and have enough three phase area for ORR.

Figure 2a shows the performance of the DBFC-PFM. Classic DBFCs were fabricated with a PEM (Nafion NRE-211 or N-117) for a comparison. As shown in figure 2a, the highest peak power densities can be obtained when using PFM as a membrane. The peak power density of the DBFC-PFM with LaNiO3 as cathodic catalyst reached 368 mW·cm−2 at 25°C and it increased by a factor of ca. 1.5 and 3.1 compared with the DBFCs using NRE-211 and N-117, respectively. Similarly, the peak power density of the DBFC-PFM with MnO2 as cathodic catalyst reached 216 mW·cm−2 and it increased by a factor of ca. 1.5 and 2.1, respectively. Moreover, the other BH4−-tolerant cathodic catalysts (La2O3, CeO2) were also used in the DBFCs-PFM. And the performance increased by a factor of ca. 1.4–2.4 (Supplementary Figure 2S) compared to that of the DBFCs with Nafion membrane.

Figure 2

Comparisons of the membranes.

(a) Performances of the DBFCs with polymer fiber membrane (PFM) (, ), NRE-211 (, ) and N-117 membranes (, ), respectively. LaNiO3 (, , ) or MnO2 (, , ) was used as cathodic catalysts, respectively. The tests were performed at 25°C. (b) Polarisation curves and performances of the DBFCs with PFM (), NRE-211 () and N-117 membranes (), respectively, when LaNiO3 and CoO were used as cathodic and anodic catalysts, respectively, at 65°C. (c) Electrochemical impedance spectrum of the cells using PFM (), NRE-211 () and N-117 membranes () as separators, respectively. The high frequency part intercept on real-axis shows in the insert figure. LaNiO3 and CoO were used as cathodic and anodic catalysts, respectively. The tests were performed at 25°C. (d) IR-free polarisation curves obtained from the DBFCs are shown when PFM (), NRE-211 () and N-117 () is used, respectively. LaNiO3 and CoO was used as cathodic and anodic catalysts, respectively. The tests were performed at 25 °C.

As the application temperature of DBFCs is in the range of 60–80°C, we measured the performance of the DBFCs at 65°C with LaNiO3 (figure 2b), which has the best performance among the cathodic catalysts mentioned above. The peak power density of the DBFC-PFM is 663 mW·cm−2, which is increased by a factor of ca. 1.7 and 3.7 compared with that of the DBFCs employing NRE-211 and N-117. At 0.6 V, which is a meaningful voltage as suggested10, the power density of the DBFC-PFM with LaNiO3 is 640 mW·cm−2 at 65°C. It is highly improved compared with the highest power density as reported27, the power density of 370 mW·cm−2 for DBFCs with Co(OH)2-PPY-C was obtained at 0.6 V at 60°C. And it increases to a level comparable with the power density of H2/O2 PEMFC with the most promising non-noble metal catalyst (750 mW·cm−2 at 0.6 V, 80°C)10.

Discussion

To explain the different performances of DBFCs with different membranes, electrochemical impedance spectroscopy was measured and the results are shown in figure 2c. Ohm resistance, which is represented by the intercept on real-axis28, is lower when PFM is used. And it is 0.08663, 0.2738 and 0.7432 Ω·cm−2 for PFM, NRE-211 and N-117, respectively. The reaction resistance of the DBFCs-PFM presented by the arc at low frequencies29, including charge transfer and mass transport resistances, is lower than that of the DBFCs with NRE-211 and N-117. The DBFCs-PFM having lower ohm and reaction resistance can be explained by following reasons.

Firstly, ions transfer is more difficult in the solid electrolyte (NRE-211 and N-117) than in the liquid electrolyte. Secondly, only preferential ions (anions or cations) are allowed to transfer through polymer electrolyte membrane (PEM), but both anions and cations can be used as carriers to transfer through polymer fiber membrane (PFM). Thirdly, in classic DBFCs, the cathode is of somehow deficiency with water as a necessary reactant for ORR. However, plenty of water is provided and mass transport resistance is lower when PFM is used.

In addition, N-117 (183 μm) is much thicker than NRE-211 (25.4 μm). So, ions have longer pathway in N-117 than in NRE-211. Thus, as figure 2c shows, the resistance of N-117 is higher than that of NRE-211.

Careful inspection of IR-free polarisation curves in figure 2d, which derived from polarisation curves compensated with ohm losses, revealed that the absolute value of slope of the DBFCs-PFM is the lowest no matter in low or high over potential region (Supplementary Table 1S). The lower absolute value of slope represents the lower polarisation, and the lower reaction resistance. Therefore, it can be concluded that the DBFCs-PFM has the lowest reaction resistances, which confirms the results of figure 2c.

Excellent performance of the DBFCs-PFM should owe to their low resistances as well as cathodic catalysts, especially LaNiO3. Because sluggish ORR of cathodic catalyst is an important factor determining the property of fuel cells30. We adopted Pt/C as cathodic catalyst in the classic DBFCs as a comparison. Table 1 shows the peak power densities of the DBFCs. In the DBFCs with NRE-211 (the third column in table 1), the LaNiO3 cathode has the best performance at the same condition among the three catalysts. While rotating disk electrode (RDE) measurement indicates that Pt/C has the highest transferred electron number (n) than that of LaNiO3 and MnO2 (last column in table 1) in the ORR. It seems a contradiction that Pt/C has the highest electron transfer number, but it has a lower power density in battery system than LaNiO3 at the same conditions. This can be explained by the crossover of fuel through the Nafion membrane. Pt/C has catalytic nature for both borohydride oxidation reaction (BOR) and oxygen reduction reaction (ORR), borohydride ions can be decomposed by Pt/C when they permeate to the cathode, and the reaction electrons do not pass into circuit but have been consumed in situ by OH− produced in the ORR in the cathode. Thus, the catalytic efficiency of Pt/C becomes lower in the cathode. Because LaNiO3 and MnO2 do not react with BH4−, the crossover does not affect the ORR in cathodic performances. We carefully conclude that Pt/C is not suitable as cathodic catalyst for DBFCs, unless crossover can be limited in a negligible level by more advanced ion exchange membrane.

Table 1

The peak power densities of the DBFCs and electron transfer number at 25°C. The data obtained from Figure 2a, Supplementary Figure 3S and Figure 4S (n means transferred electron number per oxygen molecule in the ORR)

Catalysts in cathode	PFM/mW·cm−2	NRE-211/mW·cm−2	N-117/mW·cm−2	n
LaNiO3	368	248	119	2.9
MnO2	216	146	100	2.8
Pt/C		188	217	3.5

LaNiO3 and MnO2 have similar n values (2.9 and 2.8, respectively), which indicates that these catalysts have similar catalytic property for ORR, but the difference in fuel cell performances (table 1), especially in DBFCs-PFM, implies that the n value cannot fully explain the electrochemical property of such metal oxides catalysts. In further research, we found that this difference is due to the resistivity of these two catalysts. The measurement of the resistivity of these two catalyst powders show that it is 1.07×10−1 and 1.77×102 Ω·cm for LaNiO3 and MnO2, respectively (see Supplementary Information). The resistivity of catalysts greatly influences the reaction electron exchange rate between catalysts and support. Therefore, the resistivity of catalyst should be taken enough notice in non-precious metal catalyst developing.

The stability of fuel cells is another factor determining its application. Figure 3 shows the durability tests of the DBFCs-PFM for 40 hours. DBFCs with NRE-211 have also been tested in the same conditions as a reference. Cell voltage was recorded at a constant current of 200 mA·cm2. The fluctuating point was due to the addition and consumption of fuel solution. The potential of DBFCs-PFM is much higher and without degradation throughout the 40-hours tests. While DBFCs with NRE-211 degrades continually in initial 10 hours, then tends to stable.

Figure 3

Comparison of fuel cell durability.

Polymer fiber membrane (PFM) and NRE-211 were used in DBFCs, respectively. LaNiO3 and CoO were used as cathode and anode catalyst, respectively, in all cells. The current density held at 200 mA·cm2.

In DBFCs, there are three obstacles limiting their commercialisation: borohydride hydrolysis, liquid fuel crossover and battery cost14. In our research, the last two of them have been solved in this structured fuel cell. The PFM is much cheaper and it is widely used in Ni-MH battery as a separator, meanwhile inexpensive catalysts can be used in both anode and cathode in the DBFC-PFM. In conventional research, crossover is a serious problem which must be resisted by increasing the thickness of the PEM or developing new PEM. However, increasing the thickness of PEM will increase ohm loss. We solve the problem by a different way that the crossover is allowed. A similar idea of allowing crossover has also been adopted in a swiss-roll liquid-gas mixed-reactant fuel cell31. In the situation of allowing crossover, it requires cathodic catalysts decompose O2 only and are inert to all other ions and reactants. It has been proved that the catalysts used in this work have this ability. This principle could be extended to other liquid fuel cells, such as direct methanol fuel cell (DMFC). A tentative test has been shown in Supplementary Figure 5S. A peak power density of 64 mW·cm−2 has been obtained at 60°C. It is the highest value in DMFCs concerning non-Pt-based catalysts to the best of our knowledge323334. This test provides us a clue that all liquid fuel cells can be studied in the way that crossover is no need to be considered and we just seek cathodic catalysts with selective catalysis for ORR, especially inexpensive metal oxide catalysts.

Concerning borohydride hydrolysis, there are has two ways to solve it: allowing hydrolysis and prohibiting hydrolysis. If hydrolysis is serious, we can collect hydrogen gas, which is the only by-product of the hydrolysis and feed the H2 for a H2/O2 PEMFC. We can develop a system in which, two fuel cells stacks work together, one is DBFE-PFM and the other is PEMFC. H2 comes from hydrolysis as a by-product in DBFC-PFM. It can omit hydrogen making and storage problem and is probably a new hydrogen energy system. For prohibiting hydrolysis, some researches indicated that Nafion film coated on anode35, and some metal catalysts could depress hydrogen evolution36. There are few researches concerning this problem and related researches need to be carried out in future.

Methods

Electrochemical characterisation

Electrochemical characterisation was performed using a rotate disk electrode (RDE, Pine Research Instrumentation) connected to a Pine AFCBP1 Bipotentiostat (Pine Research Instrumentation) assembled with a AFMSRCE rotator (Pine Research Instrumentation). A Hg/HgO (1 M KOH) electrode and Pt wire were used as reference and counter electrode, respectively. The work electrode, RDE, was modified with catalysts. The modified RDE electrode was fabricated as follows: a catalyst ink was prepared by ultrasonically mixing 3 mg catalyst, 0.5 ml ethanol and 15 μl Nafion (5 wt.%) into a slurry, then spreading 10 μl of the slurry onto the surface of the glass carbon electrode. The oxygen was saturated by bubbling oxygen gas into the electrolyte solution (1 M KOH) for 20 minutes before the tests.

The working electrode was scanned cathodically at a rate of 5 mV·s−1 at RDE experiment with varying rotating speed from 400 rpm to 2,500 rpm at −0.5 V, −0.6 V and −0.7 V (vs. Hg/HgO), respectively. The apparent number of electrons transferred (n) during the ORR calculated by the slopes of Koutecky–Levich (K-L) plots. The K-L equation is37:

where J is kinetic current, J is diffusion-limiting current, n is the overall number of transferred electrons during O2 reduction, F is Faraday constant (96,500 C·mol−1), A is the geometric area of the electrode (cm2), k is rate constant for oxygen reduction, C is the saturated O2 concentration in the electrolyte, D is the diffusion coefficient of O2 in the electrolyte, ν is the kinetic viscosity of the solution, and ω is the angular frequency of the rotation in terms of rad·s−1.

Preparation of cathodes and anodes

The cathode for DBFCs-PFM consisted of a gas diffusion layer, a current collector and an active layer. To prepare gas diffusion layer, 60 wt.% acetylene black and 40 wt.% polytetrafluoroethylene (PTFE) (60 wt.% PTFE solution) were mixed into slurry, then pressing the slurry into a 0.3 mm membrane and heating at 340°C for 1 hour. A non-noble metal catalyst ink was prepared by mixing 30 wt.% catalyst, 45 wt.% carbon nanotubes and 25 wt.% PTFE (60 wt.% PTFE solution). Then smeared the ink onto a current collector (nickel foam) and dried at 80°C for 2 hours under vacuum. The cathode electrode was finished by pressing the gas diffusion layer and the prepared current collector under 2 MPa.

The cathode for classic DBFCs was prepared by smeared the catalyst ink onto a hydrophobic treated carbon cloth and dried at 80°C for 2 hours under vacuum. Finally, the cathode was pressed under 2 MPa. The loading of non-noble metal cathodic catalyst was ca. 7.5 mg·cm−2. In addition, the Pt/C catalyst ink was prepared by mixing 50 wt.% Pt/C and 50 wt. % Nafion (5 wt.% Nafion solution) together. The Pt loading was 2 mg·cm−2.

The anode used in DBFCs-PFM and classic DBFCs was prepared in the same way. The anode was prepared by mixing 97 wt.% cobalt (II) oxide and 3 wt.% PTFE together. Then the mixture was pasted onto the nickel foam, and dried at 80°C for 2 hours under vacuum. Finally, the anode electrode was pressed under a pressure of 3 MPa. The anodic catalyst loading was ca. 70 mg·cm−2. In DMFCs, PtRu/C and Nafion solution was used as anodic catalyst and binder, respectively. The loading of PtRu/C was ca. 6 mg·cm−2.

Fuel cell testing

The structure of the fuel cell was shown in figure 1. The cathode contacted to oxygen flow field, while the anode connected to the fuel container. The active layer of the cathode was faced to membrane both in DBFCs-PFM and classic DBFCs. The anode, membrane and cathode were compressed together during cell assembling. The oxygen and fuel (0.8 M KBH4 and 6 M KOH) flow rates were 5 sccm and 20 ml min−1, respectively.

The EIS of the cell, by using an electrochemical workstation (CHI650C, ChenHua, Shanghai, China), was measured at open circuit voltage (OCV) with amplitude of 10 mV and the frequencies ranging from 105 Hz to 10−2 Hz.

The polarisation curve of the cell was measured by increasing current and recording voltage, which controlled by a battery testing system (Neware Technology Limited, Shenzhen, China). The cell current was held at 200 mA·cm−2 and recorded the voltage to measure the durability of the cell. The fuel was refreshed about every 5 hours.

Author Contributions

XY proposed the concept. YL directed the research. XY, YL, SL and XW designed the experiments. XY, SL, XW, LW and YC carried out the experiments. XY and YL wrote the main manuscript text and prepared figures. All authors reviewed the manuscript.