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Ag/AgCl, achieving a plateau when the latter potential value was surpassed. Hence, for Catalysts 2021, 11, 482 higher potentials than −2.2 V, the cell worked at a mass-transfer controlled rate. Therefore, a similar evaluation was carried out based on the Cu-06 catalyst results. At potentials more negative than −1.5 V vs. Ag/AgCl (see Figure 4), the Cu-06 catalyst is more selective towards the HER, which indicates that the evaluated region might be mass transfer limited. The decrease of the total carbon partial current density (mainly consti- tuted by CO production) and the increase of the H2 partial current density could confirm Therefore, a similar evaluation was carried out based on the Cu-06 catalyst results. and Nafion binder loading on the GDE performance. As suggested by Duarte et al. [28], At potentials more negative than −1.5 V vs. Ag/AgCl (see Figure 4), the Cu-06 catalyst is this study should be realised in a region of conditions where mass-transfer limitations can more selective towards the HER, which indicates that the evaluated region might be mass be excluded. Therefore, in our case, the catalyst and Nafion binder loading effects were transfer limited. The decrease of the total carbon partial current density (mainly constituted 7 of 19 the low concentration of CO2 under operating conditions. vs. Ag/AgCl, achieving a plateau when the latter potential value was surpassed. Hence, fOornhtihgheeortphoeternhtianlsdth,aitnw−2o.u2lVd,tbhecuesllewfuolrktoedcaotnasmidaesrs-trhaensifnefrlucoentrcoelloedfcrattea.lystloading evaluated at −1.5 V vs. Ag/AgCl, as shown in Sections 2.3.3 and 2.3.4. by CO production) and the increase of the H2 partial current density could confirm the low concentration of CO2 under operating conditions. Figure 4. Influence of the cathodic potential on the Faradaic efficiencies (FEs) (a) and partial current densities (b) with Cu-06 gas diffusion electrodes (GDEs) loaded with ~4 mg cm−2 and tested in Figure 4. Influence of the cathodic potential on the Faradaic efficiencies (FEs) (a) and partial cur- 1 M KHCO3. rent densities (b) with Cu-06 gas diffusion electrodes (GDEs) loaded with ⁓4 mg cm−2 and tested in 1 M KHCO3. On the other hand, it would be useful to consider the influence of catalyst loading and Nafion binder loading on the GDE performance. As suggested by Duarte et al. [28], 2.3.2.thCisosmtupdayrsishonuldbebtewreaelnisetdheinDairfefgeiroenotfSctoundietidonCsawtahleyrestmsass-transfer limitations can be excluded. Therefore, in our case, the catalyst and Nafion binder loading effects were Figure 5a shows the very stable chronoamperometry responses of the CuZ and CuZA evaluated at −1.5 V vs. Ag/AgCl, as shown in Sections 2.3.3 and 2.3.4. GDEs. The CA obtained for the Cu-06 was included for comparison. In agreement with theL2S.3V.2.mCeoamspuarreimsonenbtestw(FeeignuthreD5bif)fe,rtehnetsSetudaietdaCshatoawlystshatthecurrentdensityvaluesare −2 similar toFitghuarter5eaaschhoewdsbthyetvheeryCsuta-b0l6e chartoanloyasmt (p⁓e1ro7metArycrmespo)nastes−1o.f5thVe Cvus.ZAagnd/ACguCZlA. At this GDEs. The CA obtained for the Cu-06 was included for comparison. In agreement with the LSV measurements (Figure 5b), these data show that the current density values are similar to that reached by the Cu-06 catalyst (~17 mA cm−2) at −1.5 V vs. Ag/AgCl. At this applied potential, the addition of ZnO and Al2O3 does not promote the catalytic activity; however, to evaluate the productivity of CO2 reduction products, it is important to evaluate the selectivity (FEs). Figure 5b compares the FEs obtained with the different catalysts tested at the same potential value of −1.5 V vs. Ag/AgCl. The FE towards H2 and CO decrease in the following order: CuZA-06-03-01 > CuZ-06-03 > Cu-06. This trend is also confirmed in Figure 5c by the productivity of the gas products. At the same time, it should be observed that CO is the second product in terms of FEs, except the Cu-06 catalyst, for which a slightlyPDF Image | Gas Diffusion Electrode Systems for the Electro CO2 Conversion
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