Physical and electrochemical properties of Pd catalysts combined with Ru and Mo on carbon support were investigated. To this end, Pd, Pd1.3Ru1.0, Pd3.2Ru1.3Mo1.0 and Pd1.5Ru0.8Mo1.0 were synthesized on Carbon Vulcan XC72 support by the method of thermal decomposition of polymeric precursors and then physically and electrochemically characterized. The highest reaction yields are obtained for Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C and, as demonstrated by thermal analysis, they also show the smallest metal/carbon ratio compared the other catalysts. XRD (X-ray Diffraction) and Raman analyses show the presence of PdO and RuO2 for the Pd/C and the Pd1.3Ru1.0/C catalysts, respectively, a fact not observed for the Pd3.2Ru1.3 Mo1.0 /C and the Pd1.5Ru0.8Mo1.0/C catalysts. The catalytic activities were tested for the ethanol oxidation in alkaline medium. Cyclic voltammetry (CV) shows Pd1.3Ru1.0/C exhibiting the highest peak of current density, followed by Pd3.2Ru1.3Mo1.0/C, Pd1.5Ru0.8Mo1.0/C and Pd/C. From, chronoamperometry (CA), it is possible to observe the lowest rate of poisoning for the Pd1.3Ru1.0/C, followed by Pd3.2Ru1.3Mo1.0/C, Pd1.5Ru0.8Mo1.0/C and Pd/C. These results suggested that catalytic activity of the binary and the ternary catalysts are improved in comparison with Pd/C. The presence of RuO2 activated the bifunctional mechanism and improved the catalytic activity in the Pd1.3Ru1.0/C catalyst. The addition of Mo in the catalysts enhanced the catalytic activity by the intrinsic mechanism, suggesting a synergistic effect between metals. In summary, we suggest that it is possible to synthesize ternary PdRuMo catalysts supported on Carbon Vulcan XC72, resulting in materials with lower poisoning rates and lower costs than Pd/C.
Fuel cells have sparked a great interest in many research groups as an alternative to generating clean and high-power energy for portable electronics and electric vehicles . Several low molecular weight alcohols (methanol, ethanol, ethylene glycol, isopropanol, and glycerol) have been tested as fuels to replace hydrogen, which generates good power densities and reacts easily with oxygen, but its storage and transportation are difficult [1, 2]. Methanol reacts efficiently with oxygen and generates good current densities, but it is toxic and volatile. Ethanol is an alcohol from renewable sources, produces energy with good power densities, and exhibits a remarkably high theoretical efficiency if completely oxidized to CO2 and H2O. As a result, ethanol seems to be an excellent alternative fuel for fuel cells in mobile devices. However, breaking the ethanol C–C bond is not easy and, consequently, the CO2 formation is low, and the incomplete reaction leads to the poisoning CO [1, 3,4,5,6]
To improve the performance of alcohol fuel cells, it is necessary to use efficient anodic catalysts. Among them, Pt has shown good results in the acid medium [3,4,5,6,7], but it is a noble metal, its cost is high, and its sources of production are scarce. In addition, Pt-based catalysts are easily poisoned by CO, which decreases its efficiency and leads to undesirable intermediates [3, 5].
Due to those reasons, fuel cell research is moving towards other metals to replace Pt as an anode. For example, Pd and Pd alloys have been tested as catalysts and have shown promising results [4,5,6,7,8,9,10,11,12,13,14,15,16,17,18,19,20,21]. Research groups have been dedicated to investigating the role of Pd and Pd combined with other metals in the oxidation of various alcohols. Bimetallic and trimetallic catalysts, such as Pd-M and Pd-M1M2 (M, M1 or M2 = Ru, Au, Sn, Cu, Ni, W, Rh, Bi, Nb, Zr, Ce and Mo), supported in different matrices, aim to decrease the amount of noble metal required and to increase the catalytic activity, minimizing CO poisoning in ethanol oxidation reaction (EOR) and other alcohols [3, 8,9,10,11,12,13,14,15,16,17,18,19,20,21,22,23,24]. Table 1 presents a summary of the main Pd-based catalysts reported in the literature for EOR.
The results presented in Table 1 show an improvement in the catalytic activity for EOR when the catalysts are Pd alloys, in comparison with catalysts only with Pd, with better tolerance to poisoning, higher current densities, and more negative EOR onset potentials being observed for PdM catalysts.
This is probably due to the intrinsic mechanism (electronic effect), in which the presence of a second or a third metal modifies the electronic structure of Pd, weakening its adsorption of species containing oxygen [19, 25, 26]. Moreover, the added metals not only strongly interact with the adsorbed hydroxyl groups, making bimetallic catalysts more effective than the monometallic ones, but also may lead to rate-determining step for EOR which has less activation energy. [12, 19].
Another important factor that can also explain the lower poisoning tendency and the higher electrochemistry activity of Pd catalysts combined with other metals is the bifunctional mechanism [27,28,29], in which the oxidation of oxygen-containing species adsorbed on the catalyst surface is facilitated by the presence oxides, which provide oxygenated species for the oxidation of CO to CO2, releasing the active sites of the noble metal to oxidize the ethanol molecules.
However, the amount of the metals added to Pd must be controlled, as their atoms can decrease the number of sites occupied by Pd on the catalyst surface. As an example, it was observed by Ma et al., Gomes et al. and Carrión-Satorre et al. when the Pd/Ru ratio reached 50/50, the catalytic performance decreased, indicating the existence of an ideal amount for the second metal [18,19,20]. Similarly, the addition of Mo to Pd can facilitate the catalysis in OER through electronic effect, but it was also noted the importance of controlling the amount of Mo added to Pd, reinforcing the existence of an appropriated ratio between metals, since it highly affects the catalytic activities [21, 30].
As shown on Table 1, it is common to find Pd-based bimetallic catalysts (PdM/C) in the literature for direct ethanol fuel cells in alkaline medium. However, the number of works relating PdM1M2/C ternary catalysts is considerably low. As for Pt-based catalysts, the reduction of the amount of Pd on the catalysts, by adding one or more metals to it, makes them cheaper and more efficient for fuel cells. Besides, the literature presents studies regarding PtRu and PdRu catalysts, being observed that PdRu exhibits greater catalytic activity than PtRu in alkaline medium [5, 20, 31].
Other than Ru, Mo is an interesting metal to form ternary catalysts with Pd, since the literature reports good results with Pt. Strong synergistic effects were observed for the ternary PtRuMo alloy, concluding that the addition of Mo to Pt and Ru led to the intrinsic mechanism rather than the bifunctional mechanism, which was not observed . Also, the presence of Mo in PtRu catalyst can lead to a significant decrease in synthesis costs since Mo salts are cheaper than Pt and Ru salts . In addition, Mo is an oxophilic metal which combined with noble metals shows promising selectivity and activity for oxidation reactions .
In this sense, this paper aims to synthesize new Pd-based ternary catalysts with different PdRuMo ratios supported on treated Carbon Vulcan XC72 and test them as anodic catalysts for alkaline direct ethanol fuel cells.
Pd, PdRu and PdRuMo/C catalysts were synthesized by using the thermal decomposition method starting from their polymeric precursors . Pd(NO3)2·2H2O (99% pure), RuCl3·6H20 (99% pure) and MoCl5 (95% pure), all acquired from Sigma-Aldrich, were mixed in a solution of anhydrous citric acid (CA) (PA grade; Sigma-Aldrich) and ethylene glycol (EG) (99% pure Sigma-Aldrich) at a 1:4:16 molar ratio (1 metal salts, 4 CA, and 16 EG) and then added to previously treated Carbon Vulcan XC72 (Carbot). The treatment of Carbon Vulcan is detailed in the supplementary material. The formed suspension was stirred at about 80–90 °C for 2 h. After this time, the suspension temperature was raised to 130 °C and allowed to dry. Subsequently, the samples were placed in an oven (Labor SP 1200), heated at 300 °C for 5 min and weighed. The procedure was repeated until constant mass (see supplementary material for more details).
The obtained catalysts were analyzed by powder X-ray diffraction (XRD), thermal analysis (TG), Scanning Electron Microscopy (SEM), Transmission Electron Microscopy (TEM), X-ray Dispersive Energy Analysis (EDX), Brunauer–Emmett–Teller (BET) specific surface areas, and Raman spectroscopy.
XRD was performed on a Bruker D8 Advance diffractometer, following the following parameters: 2θ = 10–90°step of 0.01°, Cu Kα1 radiation (1.54060 Å). The diffractograms were evaluated using “Evolution” (EVA) program (Bruker™) and the crystallite sizes were estimated in nanometers by using the Scherrer equation—(Eq. 1), where D is the estimated crystallite size, K is the form factor (0.9 for spherical crystallites), λ is radiation wavelength (1.5406 Å), β is the diffraction full width at the half-maximum intensity (FWHM) and θ is the angle at the maximum intensity [21, 35].
The lattice parameters for cubic and tetragonal structures were obtained through Eqs. 2 and 3, respectively, where d is the distance between two successive (hkl) planes and a and c are the lattice parameters .
Thermal analysis was processed on a Jupiter STA F3 thermal analyzer under O2 atmosphere at a heating rate of 10 °C·min−1 from 25 to 900 °C. EDX were carried out putting the catalyst samples on a carbon strip attached to an aluminum sample holder and metalized with gold using a Denton Vacuum Desk V metallizer. Then, the images were acquired in an apparatus Jeol JSM 6610L (SEM and EDX was performed afterward). BET specific surface areas of the catalysts were measured using Quanta Chrome Autosorb equipment. Raman spectroscopy was performed on the Witec Alpha 300 confocal equipment (Germany), 20× magnification, green laser (λ = 532 nm) at 20 °C.
Ultrapure water (SARTORIUS mini, Arium™, model MA-UVT) with a resistivity of 18.0 MΩ.cm at 22 °C was used for preparing all the solutions used in the electrochemical tests. Cyclic voltammetry (CV) and Chronoamperometry (CA) were performed with a glassy carbon working electrode (area 0.066 cm2), a graphite counter electrode (area 12.05 cm2) and a saturated calomel electrode (SCE) (Analyzer, model 3A41) as a reference electrode. The working electrode was previously polished with an alumina suspension (n° 3–0.3 μm Skill-Tec) and prepared with a catalytic ink, composed by 1.0 mg of catalyst, 95 μL ethanol (Sigma-Aldrich—99% purity), and 5 μL of Nafion® 117 (Sigma-Aldrich) solution, all homogenized for 30 min in an ultrasonic bath, deposited on its surface and dried at 60 °C.
CV measurements were performed using a PAR-Ametek VersaStat 4™ potentiostat/galvanostat in the potential range from – 0.8 to 0.4 V vs. SCE, 2 cycles with scan rate of 20 mV·s−1 for KOH 1.0 mol L−1 and a solution composed by 5.83 mL ethanol and 100 mL KOH 1.0 mol L−1 (KOH, prepared from 90% purity and ethanol both from Sigma-Aldrich). CA was performed by applying a fixed potential at – 0.4 V vs. SCE for 2 h to a solution composed by 5.83 mL ethanol and 100 mL KOH 1.0 mol L−1. The electrolytes were purged with N2 5.0 (99.9% purity, White Martins) for 10 min.
Results and discussion
The catalysts were synthesized with high yields and the values are shown in Table 2, as well the results of their physical characterizations by EDX, BET surface area and TGA. According to the thermal analysis (Fig. 1), the ternary catalysts (containing Pd, Ru and Mo) exhibit low remaining mass, or low metal content, at 900 °C. As the thermal analysis was performed under oxygen atmosphere, the carbon support was fully oxidized during the process, leaving only the mass of metallic compounds at the end of the measurement [12, 37]. This difference between binary and ternary catalysts can be attribute to a lower carbon loss during the calcination step for the ternary catalysts production, leading to a higher carbon content in the ternary catalysts (Table 2) and suggesting a better interaction between the ternary catalysts and their carbon support.
By the remaining metal masses, it was possible to estimate the percentages of the catalysts supported on carbon, which are approximately 50%, 48%, 30% and 32% for Pd/C, Pd1.3Ru1.0/C, Pd3.2Ru1.3 Mo1.0 /C and Pd1.5Ru0.8Mo1.0/C, respectively (Table 2). The confirmation of oxide presence on Pd/C and Pd1.3Ru1.0/C by thermal analysis is the large loss of mass occurring from 800 °C and related to the decomposition of oxides [12, 56], a fact observed for Pd/C and Pd1.3Ru1.0/C at 900 °C (Fig. 1).
Figure 2 shows the XRD patterns of the produced catalysts and all samples display typical diffraction peaks at 2θ = 40.1, 46.5, 68.1 and 82° corresponding to (111), (200), (220) and (311) planes of Pd face-centered cubic (fcc) structure (JCPDS 46–1043) [12, 20, 21]. Peaks at 33.84, 41.93, 54.72, 60.2○ and 71.25○ are also observed in the Pd/C catalyst and are attributed to the planes (101), (110), (112), (103) and (202) of the PdO tetragonal phase (JCPDS 41–1107) [8, 17,18,19]. The catalyst Pd1.3Ru1.0/C contains three distinct peaks centered at approximately 28.09, 35.1 and 54.5○, which can be attributed to the presence of RuO2 with a tetragonal structure referring to the planes (110), (101) and (211) (JCPDS 01–0702-662), respectively [20, 27].
The presence of RuO2 may indicate the unsuccessful alloy formation between Pd and Ru, since studies reported a small amount of Ru dissolved in the fcc structure of Pd [20, 39, 42]. In addition, Fisher et al.  suggested that PdRu alloy can be formed at temperatures below 250 °C and it was not observed at higher temperatures. The present work synthesized the catalysts at 300 °C and it can be another reason for the non-alloy formation between Pd and Ru on the Pd1.3Ru1.0/C catalyst.
The comparison between the angles of (111) plane of Pd fcc structure shows that Pd/C, Pd1.3Ru1.0/C and Pd1.5Ru0.8Mo1.0/C present this plane at 40.12, 40.12 and 40.11○, respectively, and Pd3.2Ru1.3Mo1.0/C presents two distinct phases of cubic Pd: one at 39.06○ (JCPDS 01-087-0637) and another at 40.12○ (JCPDS 46-1043). Pd3.2Ru1.3 Mo1.0 /C also presents peaks at 45.41, 66.17 and 79.60○ corresponding to (200), (220) and (311) planes of Pd fcc structure (JCPDS 01-087-0637) (Fig. 2). No displacement is observed at 2θ for Pd/C and Pd1.3Ru1.0/C, suggesting no alloy formation between Pd and Ru, a fact observed by Moraes et al. in the study of Pd catalysts .
Carrión-Satorre et al.  and Monyoncho et al.  studied PdRu/C catalysts with metal proportions similar to the ones used in this work and suggested ineffective incorporation of Ru into the Pd lattice. On the other hand, Pd3.2Ru1.3 Mo1.0/C and Pd1.5Ru0.8Mo1.0/C present diffraction peak displacements (Table 2), suggesting the formation of alloys as observed by Moraes et al. for Pd catalysts modified by Ni and Sn .
Table 3 presents the lattice parameters (a, b, and c), volume (V) and the estimated crystallite sizes (D) for the catalysts, calculated by Eqs. 2 and 3 respectively. The addition of metals with atomic radius greater than Pd (1.28 Å) to its structure, as in the case of Mo (1.29 Å), increases the lattice parameters, thus indicating an expansion of the crystalline lattice. This fact has been reported in the literature, where metals with atomic radius greater than Pd, such as Au (1.34 Å) and Sn (1.40 Å), increased its lattice parameters when added to it .
The estimated crystallite sizes of the produced catalysts were calculated by Eq. 1, measuring between 16.0 and 47.0 nm for Pd fcc phase. These values do not match those reported in the literature, where crystallite sizes between 4 and15 nm were observed. Possible reasons for this discrepancy are related to the synthesis method adopted and the metal/carbon ratio used [10,11,12]. Based on the metal/carbon ratio, Pillai et al.  studied catalysts with metal/carbon ratios between 20 and 40% and prepared them by metal reduction with formic acid technique and observed an increase in the crystallite size when the metal proportion was around 30%. Similar behavior is observed for the catalysts Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C prepared in this work by the technique using citric acid, which present metallic loads around 30 and 32%, respectively. Concerning the synthesis method, this work adopted a method not reported in the literature for the preparation of Pd ternary catalysts and it can explain the production of crystallites with sizes higher than the values reported (Table 2), since the preparation technique is one of the factors that affect the structure of the particles . In addition, it is important to emphasize that Eq. 1 determines, more accurately crystallite size of spherical particles .
Figure 3 shows the Raman spectra, and it is possible to see peaks of greater intensity related to PdO and RuO2. Pd/C shows typical PdO Raman spectrum, with the most intense peak at 646 cm−1. McBride et al.  and Zhao et al.  obtained similar spectrum at room temperature for PdO, with the most intense peak at 648 cm−1, which is very close to the value found in this work. Therefore, the results presented by Raman spectroscopy are in accordance with the TG and XRD results, proving the formation of PdO on the Pd/C catalyst. Pd57Ru43/C shows Raman displacement values at 628 and 698 cm−1. Shin et al.  and Meng et al.  obtained these values at room temperature for the RuO2 spectrum. The result of Raman spectroscopy for Pd1.3Ru1.0/C also agrees with its XRD results. Pd3.2Ru1.3 Mo1.0 /C and Pd1.5Ru0.8Mo1.0/C do not show Raman displacements for oxides (Fig. 3), confirming the results of TG and XRD, where no oxides were observed for those catalysts, suggesting the more effective incorporation of Ru and Mo into the palladium structure. In summary, the results achieved by TG, XRD and Raman suggest the formation of alloys on Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C, but not on Pd1.3Ru1.0/C.
BET surface areas for Pd/C, Pd1.3Ru1.0/C, Pd3.2Ru1.3 Mo1.0 /C, Pd1.5Ru0.8Mo1.0/C were 27.5, 100, 47.2 and 38.9 m2 g−1, respectively (Table 2). In comparison to treated Cvulcan, there is a considerable decrease in its BET surface area after the production of the catalysts (211.1 m2g−1- supplementary material). The reduction in the surface area of the carbon is noticeable when impregnated with metal, indicating the existence of metal nanoparticles on its surface. This can be explained by the pore clogging caused by the metals, leading to a decrease in the support surface area [36, 46]. In addition, a smaller surface area indicates a better particles distribution on the support, preventing the absorption of nitrogen [47, 48].
Figure 4 shows voltammetric profile of the catalysts in alkaline medium with similar anodic and cathodic current densities in the potential range between – 0.8 V and 0.4 V vs SCE. This potential range was adopted by the fact that voltammetric curve for compounds with Pd usually present three distinct regions during the scan: the so-called hydrogen region, observed from – 0.8 to – 0.4 V: the oxidation region of Pd to PdO, observed in the potential range between – 0.4 and 0.4 V and the PdO reduction, observed between – 0.6 and – 0.4 V [12, 20].
In Fig. 4a it is possible to see the peaks of cathodic potentials (Ecat), also defined in Table 4, for all the catalysts. Pd/C shows a peak of PdO reduction at – 0.40 V, related to PdO + H2O + e− → Pd + 2 OH− (Eq. 4) . In the Pd1.3Ru1.0/C catalyst, the presence of Ru displaces the cathodic peak to E = – 0.30 V, a fact explained by the reduction of ruthenium oxides . The displacement of Ecat values for Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C catalysts may be related to the stronger interaction of Ru and Mo with Pd, corroborated by the formation of oxides for these catalysts.
Figure 4b shows the cyclic voltammograms of the catalysts in KOH/ethanol medium and Table 4 shows their electrochemical parameters. Two peaks are observed in the ethanol voltammograms and are relative to its oxidation. In the forward scan, the observed peak corresponds to the oxidation of species adsorbed in the catalysts generated by the dissociative adsorption of ethanol. In the backward scan, the peak is related to the removal of carbonaceous species not completely oxidized in the forward scan . According to Hammed , the oxidation reaction of ethanol on Pd results from the adsorption of ethanol on the electrocatalytic surface, where it is not completely oxidized in an alkaline medium and can be represented by Eqs. 4, 5, 6 and 7.
The EOR initiation potential (Eonset) shows more negative values for the catalysts containing metals added to Pd (Table 4). This fact suggests not only a greater facility to initiate the reaction (Eq. 4) , but also to modify the Pd/C structure by adding Ru and Mo to Pd catalysts, favoring the catalysis of the EOR. Maximum values of current density for anodic oxidation peak (jpeak) are also observed. The Pd1.3Ru1.0/C catalyst shows the highest jpeak value and the greatest variation of the oxidation peak compared to Pd/C, followed by the Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C catalysts.
The greatest catalytic performance exhibited by Pd1.3Ru1.0/C can be related to four factors [12, 20, 50]: crystallite size, BET surface area, electronic effect and bifunctional mechanisms. Pd1.3Ru1.0/C shows the larges BET surface area and the smallest average crystallite size (Tables 2 and 3), which facilitates the passage of electrons on the catalyst surface during the EOR. In addition, the presence of RuO2 favors the bifunctional mechanism, with the oxide favoring the oxidation of CO to CO2. Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C show larger crystallite sizes, suggesting their catalytic activities are not due to this factor, but are related to the BET surface area (Table 2) and to the electronic effect mechanism generated by the alloys formed between the metals, which modify their electronic structures, reducing the activation energy required for the EOR [16, 17].
Chronoamperometry is an important electrochemical technique for the evaluation of catalytic activity and stability of PdM/C and PdM1M2/C catalysts in EOR. In this sense, Fig. 5 shows the chronoamperometric curves for ethanol oxidation at – 0.4 V, since it was observed that the region between – 0.6 and – 0.4 V could give us an idea of the trends that can be observed in a fuel cell with PdRu-based catalysts .
During the first minutes of analysis, a sharp reduction in the current is observed and it is followed by a slower decline over the time. At the beginning, the active sites of the catalysts are free of adsorbed organic molecules (CH3CH2OH, CH3CO and CH3COOH) and it promotes high adsorption rates. However, as the time passes, the active sites become fully occupied and the adsorption of a new ethanol molecule occurs only after the releasing of a site, causing the poisoning of the active sites by these molecules. Stabilization is observed at, approximately, 300, 1000, and 600 s for Pd/C, Pd1.3Ru1.0/C, Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C catalysts, respectively (Fig. 5). Poisoning rate (δ) can be calculated through Eq. 9 by measuring the linear decay of the current density over a time greater than 300 s .
It can be seen from Table 4 that adding metals to Pd shifts δ to more negative values, suggesting that added metals contribute to decrease the poisoning rate of binary and ternary catalysts. Pd1.3Ru1.0/C shows the lowest δ value and the longest stabilization time (approximately 1000 s) and this is maybe due to the presence of Ru, a chemical element more oxyphilic than Pd on the catalyst. Ru may favor the formation of oxidized species (RuO2) on the surface of the material and this oxide activates oxygen atoms in the EOR, favoring the reaction and making the catalyst more resistant to poisoning . Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C instead show intermediate values of stabilization time (approximately 600 s) and more negative δ values compared to Pd/C catalyst, but more positive than Pd1.3Ru1.0/C catalyst. This fact can also be explained by the electronic effect mechanism, in which the metals added to the Pd modify its electronic structure and form alloys with Pd, reducing both the poisoning of the active sites of the catalysts and the EOR activation energy . These facts confirm CV results, with Pd1.3Ru1.0/C showing greater catalytic activity for EOR, followed by Pd3.2Ru1.3Mo1.0/C, Pd1.5Ru0.8Mo1.0/C and Pd/C (Fig. 5 and Table 4), being also the most stable and the most poisoning resistant catalyst.
Petrii  reported that PtRu catalysts had a high tolerance to CO and facilitated the oxidation of CO to CO2, due to the bifunctional mechanism, where the presence of Ru strongly modified the surface of Pt and activated oxygen species. Thus, the performance of PtRuMo/C catalysts for the ethanol oxidation could be is related to the high affinity of their oxides in relation to the OH species, providing species of oxygen at the surface of the catalyst with lower potential compared to pure Pd catalysts. That is, the presence of Ru and/or Mo maybe favors the bi-functional mechanism and can accelerate the dissociation of H2O molecules to form OHads, facilitating the oxidation of adsorbed alcohols or poisons, thus recovering the active sites of Pd so that the oxidation reaction continues. Therefore, due to the similarities between Pt and Pd, similar behavior is expected, a fact observed in the intermediate behavior of the poisoning rate of Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C, lower poisoning rate of Pd1.3Ru1.0/C (Table 4) and stabilization time (Pd1.3Ru1.0/C ~ 300; Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C ~ 600 s – Fig. 5).
The main challenges for the development of new materials for ethanol fuel cells are related to the catalyst poisoning, which decreases its efficiency, and the high cost of the Pd salts used for the preparation of the catalysts. Nowadays, the average price of 1 g of Pd(NO3)2·2 H2O used in this work, is about US$ 150.00 . Both poisoning and material cost can be reduced by lowering the amount of Pd on the catalyst, either by increasing the amount of the support or adding metals less nobles. Table 5 shows the comparison between the results obtained for Pd1.3Ru1.0/C, Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C in relation to Pd/C. This table brings the amount of Pd (considering Pd/C 100%), the percentage of the maximum oxidation peak variation (Δjpeak), the approximate increase in the percentage of the average time to initiate the catalyst poisoning (% t), the decrease in the percentage of poisoning (Δδ) and the percentage of cost reduction in relation to Pd/C (% $), with the value of US$ 150.00/g of the Pd salt being reduced.
From the data presented in Table 5, the three catalysts prove to be more efficient than Pd/C. Pd1.3Ru1.0/C shows the highest variation in the maximum oxidation peak, the lowest propensity for poisoning and the longest stability. However, due to the higher percentage of Pd, it would have a higher cost compared to Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C. Pd3.2Ru1.3Mo1.0/C shows a lower peak of current density and an increase in the percentage of poisoning by about 28% in relation to Pd1.3Ru1.0/C. So, Pd3.2Ru1.3Mo1.0/C can be considerably less stable than Pd1.3Ru1.0/C, but due to its lower percentage of Pd it decreases its cost. Pd1.5Ru0.8Mo1.0/C shows similar results to Pd3.2Ru1.3Mo1.0/C and a small variation in the cost in relation to the total cost. Therefore, analyzing the values presented in Table 5, it is possible the development of alloys with Pd, Ru and Mo on carbon Vulcan as support aiming to decrease the poisoning rate and the cost of these catalysts. We encourage the performance of other tests with the catalysts of this [52,53,54,55] work to study their properties, as well as the synthesis and characterization of new proportions of the PdRuMo alloy, to obtain a greater reduction in the degree of poisoning and greater decrease in the cost of these materials. Concluding, the Table 6 presents a summary of the main characteristics and differences between the catalysts evaluated in this work, where we observed that Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C can have a low cost compared to Pd/C and Pd1.3Ru1.0/C, due to the smaller amounts of Pd, also showing an intermediate rate of poisoning by CO, suggesting they are viable as catalysts for fuel cells.
Pd1.3Ru1.0/C shows the best catalytic activity and the lowest propensity for poisoning due to the bifunctional mechanism related to the presence of RuO2. Pd3.2Ru1.3Mo1.0/C and Pd1.5Ru0.8Mo1.0/C show the highest synthesis yields and an intermediate propensity for poisoning compared to Pd/C and Pd1.3Ru1.0/C, a fact explained by the electronic effect mechanism created by the formation of alloys between the used metals. Due to the lower amount of Pd used in the synthesis of ternary PdRuMo/C catalysts and the results presented, we suggest a combination of these three metals supported on Cvulcan as catalyst in alkaline direct ethanol fuel cells.
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The authors thank the Brazilian agency FAPES (Fundação de Amparo a Pesquisa e Inovação do Espírito Santo) for the financial support by means of grant n○ 85201154 and n° 515/2016. We also thank the laboratories responsible for the characterization of the developed materials: LPT/LMC—Physics Departament (UFES) for BET Area, Labpetro—Chemistry Departament (UFES) for Raman and XRD measurements (Technical Cooperation agreement). 0050.0022844.06.4 and CT-Infra 01/2007-FINEP 0202/08), Luccar (Morfology Department-CSS/UFES) for SEM/EDX/TEM and Labpol—Dr. Kinglston Soares (CMM/IFES) for TG. Special thanks to Antonio Augusto Lopes Marins (DQUI-UFES) for the suggestions in the discussion of XRD and Raman analyses.
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Fornazier Filho, Y., da Cruz, A.C.C., Pedicini, R. et al. Development of palladium catalysts modified by ruthenium and molybdenum as anode in direct ethanol fuel cell. Mater Renew Sustain Energy 10, 5 (2021). https://doi.org/10.1007/s40243-020-00187-1
- Palladium-based catalysts
- Electronic interaction mechanism
- Bifunctional mechanism