Optimizing the Performance of Low-Loaded Electrodes for CO2-to-CO Conversion Directly from Capture Medium: A Comprehensive Parameter Analysis

Gas-fed reactors for CO2 reduction processes are a solid technology to mitigate CO2 accumulation in the atmosphere. However, since it is necessary to feed them with a pure CO2 stream, a highly energy-demanding process is required to separate CO2 from the flue gasses. Recently introduced bicarbonate zero-gap flow reactors are a valid solution to integrate carbon capture and valorization, with them being able to convert the CO2 capture medium (i.e., the bicarbonate solution) into added-value chemicals, such as CO, thus avoiding this expensive separation process. We report here a study on the influence of the electrode structure on the performance of a bicarbonate reactor in terms of Faradaic efficiency, activity, and CO2 utilization. In particular, the effect of catalyst mass loading and electrode permeability on bicarbonate electrolysis was investigated by exploiting three commercial carbon supports, and the results obtained were deepened via electrochemical impedance spectroscopy, which is introduced for the first time in the field of bicarbonate electrolyzers. As an outcome of the study, a novel low-loaded silver-based electrode fabricated via the sputtering deposition technique is proposed. The silver mass loading was optimized by increasing it from 116 μg/cm2 to 565 μg/cm2, thereby obtaining an important enhancement in selectivity (from 55% to 77%) and activity, while a further rise to 1.13 mg/cm2 did not provide significant improvements. The tremendous effect of the electrode permeability on activity and proficiency in releasing CO2 from the bicarbonate solution was shown. Hence, an increase in electrode permeability doubled the activity and boosted the production of in situ CO2 by 40%. The optimized Ag-electrode provided Faradaic efficiencies for CO close to 80% at a cell voltage of 3 V and under ambient conditions, with silver loading of 565 μg/cm2, the lowest value ever reported in the literature so far.


Introduction
During the previous decades, human activities have increased atmospheric CO 2 concentrations, stimulating the scientific community toward the development of lesscarbon intensive technologies and depleting the use of fossil fuels. However, renewable energy use requires time to be assessed, and it is of capital relevance to reduce carbon emissions during the energy transition. As a consequence, the renewable-energy-powered electrochemical reduction reaction of CO 2 (eCO 2 RR) into added-value chemicals and fuels (e.g., syngas and methane) has attracted strong interest as a solution for a close carbon cycle [1]. The possibility to obtain carbon-based products from eCO 2 RR at high rates has already been deeply investigated in gas-fed electrolyzers [2], where a stream of pure CO 2 needs to be delivered to the cathode. The perspective to employ such technology in an industrial setting requires coupling between the electrolyzer and CO 2 separation from the other components of flue gasses (e.g., O 2 , N 2 , and H 2 O) emitted by a point source (e.g., an industrial plant). As an example, alkaline solutions (e.g., KOH) are able to capture gaseous CO 2 from flue gasses thanks to reactions that form (bi)carbonates [3]. Since it is known that CO 2 may be extracted from bicarbonate through energy-intensive processes [4], once it has been pressurized, it can be exploited for further valorization through electrolytic conversion. [5] In such kinds of platforms for carbon capture and utilization (CCU), since common gas-fed electrolyzers exhibit low single-pass utilization, around 80% of delivered CO 2 exits from the platform as unreacted gas [6]. In this framework, liquid-fed bicarbonate (HCO 3 − ) electrolyzers have arisen as a new, groundbreaking technology to integrate the capture and conversion of CO 2 (ICCU) [7][8][9] into CO. These reactors introduced the chance to eliminate all the energy-demanding processes (capture/stripping and pressurization) necessary to feed a classical gas-fed eCO 2 RR system. The electrolysis of carbonate solution, i.e., the capture media, is possible using a cation exchange membrane (CEM) or a bipolar membrane (BPM) that, providing an acidic local environment, makes gaseous CO 2 available in proximity to the catalyst for electroreduction. The utilization of a BPM instead of a CEM is now benchmarked since it allows for the employment of an inexpensive nickel anode and prevents products' cross-over [10,11]. The BPM, together with anodic and cathodic catalysts, constitutes a membrane electrode assembly (MEA), which is the benchmark configuration in bicarbonate electrolyzers. In the MEA, the presence of H + (produced in the BPM by water splitting) at the membrane/catalyst interface is responsible for the in situ acidification and thus extraction of CO 2 (i-CO 2 ) from (bi)carbonate, which is converted into CO (Equations (1) and (2)), thanks to the eCO 2 RR catalyst.
CO 2 (g) + H 2 O + 2e − → 2OH − + CO (2) Since OH − is a product of the CO 2 RR as well, the original alkaline capture solution is regenerated, making this system able to implement a closed cycle where CO 2 is sequentially captured and converted. The presence of a MEA ensures a very high local concentration of CO 2 at the electrocatalyst interface without the need of supplying the reactor by a stream of gaseous CO 2 in stoichiometric excess, as happens with gas-fed electrolyzers. This also means that CO 2 RR products are generated at higher concentrations [12]. The gas diffusion electrode (GDE) employed in this kind of system has to ensure the efficient transport of carbon feedstock (i.e., HCO 3 − ) at the BPM/catalyst interface. Therefore it must be engineered differently with respect to the GDEs used in gas-fed electrolyzers, which usually exhibit hydrophobic properties to avoid the accumulation of water and to mitigate the hydrogen evolution reaction (HER) [13], the competing reaction of the CO 2 RR.
Despite the promising advantages, research conducted on this technology so far is still limited compared to more well-known gas-fed electrolyzers. Therefore, a deep investigation into every aspect of the system is needed. Among the first works, Y. C. Li et al. [8] reported a bicarbonate electrolyzer able to keep the high pH of the capture solution for 145 h by using a carbon composite silver electrode, but the highest Faradaic efficiency (FE) toward CO (FE CO ) was~35%. T. Li et al. [7] with a silver nanoparticle-coated carbon support obtained impressive FE CO at a low current density and showed how the employment of an anion exchange membrane (AEM) is detrimental to the electrolyzer's performance. The same conclusion was reported by C. Larrea et al. [14], whereby, although it was responsible for a large ohmic drop between the two electrodes, the necessity to use a BPM in order to have appreciable FE was proven. Z. Zhang et al. [15] showed how the increase in porosity of a silver foam, employed as a cathode, enables more efficient CO 2 conversion; however, even avoiding the utilization of composite carbon electrodes, the FE CO achieved at ambient conditions is around 60%. In addition, they illustrated how higher pressure and higher temperature promote the CO 2 RR. Y. Kim et al. [16] underlined the importance of a trade-off Nanomaterials 2023, 13, 2314 3 of 10 between the active surface and the permeability of the GDE in order to guarantee both a high CO 2 RR rate and efficient transport of bicarbonate (i.e., i-CO 2 generation). E. W. Lees et al. [17] reported important information on the spray coating of a silver catalyst in order to have an efficient GDE in terms of Nafion content and Ag nanoparticle loading. By adding a preliminary deposition step by sputtering physical vapor deposition (PVD) before the spray coating, they reached a very good FE CO (around 82%) using a high silver loading of 2 mg/cm 2 .
The sputtering technique serves as a rapid and reproducible method for manufacturing nanostructured Ag-GDEs with a high surface area in a single step, offering precise control over catalyst loading, layer thickness, and homogeneity. Our research group has already explored and established the reliability of this approach [18]. In this study, we further optimized the sputtering process to fabricate a GDE specifically designed for bicarbonate electrolyzers. To investigate the electrode's performance, we tested different commercial carbon supports with distinct characteristics such as gas diffusion layers (GDLs). This allowed us to delve into the GDL's role and its impact on the FE CO and CO 2 utilization, representing the extent of CO 2 conversion compared to the unreacted CO 2 . During the analysis, we explored the influence of several structural and morphological properties of the cathode on the electrochemical performance. These properties encompassed different catalyst distributions on the GDL, GDL hydrophobicity and permeability. By understanding the significance of these factors, we gain critical insights into optimizing the GDE's design and performance for bicarbonate electrolyzers.
Moreover, electrochemical impedance spectroscopy (EIS) has already demonstrated its efficacy as an efficient tool for studying the charge transfer and transport processes involved in typical systems for CO 2 reduction reactions (CO 2 RRs) [19]. Its utility has made it a valuable technique for the characterization of materials and reactors in this field [20,21]. Despite this, to the best of our knowledge, it has never been employed in studies involving bicarbonate electrolyzers. Remarkably, our paper presents a pioneering application of EIS to investigate the performance of GDEs employed in bicarbonate electrolyzers. This novel approach represents a significant advancement in the field, as previous research has primarily focused on using EIS for other CO 2 RR systems. Through careful modeling of the GDE/electrolyte interface using an equivalent electrical circuit, this paper successfully elucidates the underlying factors influencing the activity and Faradaic efficiency trends of the GDEs.

Preparation and Morphological Characterization of Ag GDEs
DC Sputtering (Quorum Technologies Ltd., Lewes, UK, Q150T) was used to prepare the Ag electrodes. Three commercial carbon papers (GDL, Ion Power) of 5 cm 2 characterized by different permeability and wettability (Table S1) were used as substrates, with a silver disk (99.999%, Nanovision, Brugherio, Italy) as the target. The deposition current was fixed at 50 mA, while the deposition time was varied to control the silver mass-loading (100 s, 300 s, and 600 s). A total of 6 GDE samples (A-F) were prepared, whose properties are reported in Table S2. All of the samples were prepared by depositing silver on both faces of the carbon papers, except for sample A. The mass loading was determined by weighing the sample before and after the silver deposition and then by dividing the weight difference by the geometric area of the GDL. The morphology of the commercial carbon-based supports and Ag-GDE samples was investigated by field emission scanning electron microscopy (FESEM, Zeiss Auriga, Oberkochen, Germany).

Electrochemical Tests and Product Analyses
The electrochemical screening was performed in a bicarbonate electrolyzer (Scribner, Cell Fixture) placed in a vertical position, whose schematic representation is reported in Figure 1. A more detailed description of the system is provided in the Supporting Information. A 5 cm 2 MEA was employed in the electrolyzer, and it was made by a bipolar membrane (FumaSep FBM, FumaTech, Bietigheim-Bissingen, Germany) sandwiched be-tween a Nickel foam (99.5%, GoodFellow, Huntingdon, UK) and a Ag GDE. KHCO 3 (99.5%, Sigma-Aldrich, St. Louis, MO, USA) 2 M was used as a catholyte and KOH (Sigma-Aldrich) 1 M was used as an anolyte by dissolving 200 g and 56 g, respectively, in 1 L of ultra-pure water. A peristaltic pump was used to continuously recirculate 60 mL of bicarbonate solution and 40 mL of potassium hydroxide at a flow rate of 5 mL/min. Electrolysis was carried out at ambient temperature and pressure by applying a constant cell voltage (V cell ) of 3 V (Potentiostat, BioLogic VSP, Seyssinet-Pariset, France). Gas-phase products were delivered to a microgas chromatograph (µGC, Fusion, INFICON) by a N 2 35 mL/min stream (Bronkhorst, EL-FLOW select) and analyzed on-line throughout the entire duration of the experiment. The microgas chromatograph, which is preceded by a mass flow reader (Bronkhorst, Ruurlo, The Netherlands, EL-FLOW prestige), is composed of two channels with a 10 m Rt-Molsieve 5A column and an 8 m Rt-Q-Bond column, and each channel has a microthermal conductivity detector. Two tests were conducted per set of experiments, and the results are reported as average values (the error bars correspond to the absolute error). Additional details on the calculation of the CO partial current density, FE, CO 2 utilization, mass activity, and partial mass activity are provided in the Supporting Information.

Electrochemical Tests and Product Analyses
The electrochemical screening was performed in a bicarbonate electrolyzer (Scribner, Cell Fixture) placed in a vertical position, whose schematic representation is reported in Figure 1. A more detailed description of the system is provided in the Supporting Information. A 5 cm 2 MEA was employed in the electrolyzer, and it was made by a bipolar membrane (FumaSep FBM, FumaTech, Bietigheim-Bissingen, Germany) sandwiched between a Nickel foam (99.5%, GoodFellow, Huntingdon, UK) and a Ag GDE. KHCO3 (99.5%, Sigma-Aldrich, St. Louis, MO, USA) 2 M was used as a catholyte and KOH (Sigma-Aldrich) 1 M was used as an anolyte by dissolving 200 g and 56 g, respectively, in 1 L of ultra-pure water. A peristaltic pump was used to continuously recirculate 60 mL of bicarbonate solution and 40 mL of potassium hydroxide at a flow rate of 5 mL/min. Electrolysis was carried out at ambient temperature and pressure by applying a constant cell voltage (Vcell) of 3 V (Potentiostat, BioLogic VSP, Seyssinet-Pariset, France). Gas-phase products were delivered to a microgas chromatograph (μGC, Fusion, INFICON) by a N2 35 mL/min stream (Bronkhorst, EL-FLOW select) and analyzed on-line throughout the entire duration of the experiment. The microgas chromatograph, which is preceded by a mass flow reader (Bronkhorst, Ruurlo, The Netherlands, EL-FLOW prestige), is composed of two channels with a 10 m Rt-Molsieve 5A column and an 8 m Rt-Q-Bond column, and each channel has a microthermal conductivity detector. Two tests were conducted per set of experiments, and the results are reported as average values (the error bars correspond to the absolute error). Additional details on the calculation of the CO partial current density, FE, CO2 utilization, mass activity, and partial mass activity are provided in the Supporting Information.

Electrochemical Impedance Spectroscopy
EIS measurements were performed in a three-electrode single compartment cell at room temperature with a Biologic VSP electrochemical workstation. The working electrode was a Ag GDE with a geometric area of 0.4 cm 2 . A Pt wire was used as the counter electrode, and Ag/AgCl (3 M Cl − ) was used as the reference, with both purchased from ALS. The electrolyte was a CO2-saturated 2 M KHCO3 (99.5%, Sigma-Aldrich) aqueous solution. The analysis was performed at a potential of −1 V vs. a reversible hydrogen electrode (RHE) with an AC signal with 10 mV of amplitude and a 0.1-10 5 Hz frequency range.

Results and Discussion
As the first step of GDE optimization, it was investigated as to whether it is more convenient to deposit the silver only on one side of the carbon support or on both of them ( Figure 2a). Therefore, keeping the same sputtering parameters and carbon support, two samples were made. On the first one (sample A), silver was sputtered only on the face in

Electrochemical Impedance Spectroscopy
EIS measurements were performed in a three-electrode single compartment cell at room temperature with a Biologic VSP electrochemical workstation. The working electrode was a Ag GDE with a geometric area of 0.4 cm 2 . A Pt wire was used as the counter electrode, and Ag/AgCl (3 M Cl − ) was used as the reference, with both purchased from ALS. The electrolyte was a CO 2 -saturated 2 M KHCO 3 (99.5%, Sigma-Aldrich) aqueous solution. The analysis was performed at a potential of −1 V vs. a reversible hydrogen electrode (RHE) with an AC signal with 10 mV of amplitude and a 0.1-10 5 Hz frequency range.

Results and Discussion
As the first step of GDE optimization, it was investigated as to whether it is more convenient to deposit the silver only on one side of the carbon support or on both of them ( Figure 2a). Therefore, keeping the same sputtering parameters and carbon support, two samples were made. On the first one (sample A), silver was sputtered only on the face in contact with the bipolar membrane, while on the second one, the sputtering process was replicated on the opposite side as well (sample B), the one facing the graphite flow field. As shown in Figure 2b, sample A exhibits relatively good activity and FE CO . This implies that the most active interface is the one facing the bipolar membrane, namely the region with the highest concentration of i-CO 2 , since it is in proximity to the BPM. However, sputtering the silver on the other side of the GDL as well boosted the FE CO from 55% to 77%. Considering the results of this experiment, silver was deposited on both faces of the GDE samples tested from then on. that the most active interface is the one facing the bipolar membrane, namely the region with the highest concentration of i-CO2, since it is in proximity to the BPM. However, sputtering the silver on the other side of the GDL as well boosted the FECO from 55% to 77%. Considering the results of this experiment, silver was deposited on both faces of the GDE samples tested from then on. The carbon support used to obtain the results mentioned just above was not treated with polytetrafluoroethylene (PTFE) nor did it include a microporous layer (MPL). These two characteristics are fundamental if this electrode had been used in a common gas-fed CO2RR reactor [18]. In gas-fed reactors, the MPL and the hydrophobic treatment produce water repellent properties that can prevent the carbon fiber backing from flooding. In bicarbonate electrolyzers, the hydrophobic feature inhibits the transport of bicarbonate from the flow field toward the BPM, where the low-pH region is located. In this way, the production of i-CO2 drastically decreases, hence also the FECO, JCO, and the CO2 utilization ( Figure 3). By using a hydrophobic carbon support (sample C), the FECO decreases to 23%, while JCO and the overall activity (Jtot) ( Figure S1a) are significantly affected as well. The carbon support used to obtain the results mentioned just above was not treated with polytetrafluoroethylene (PTFE) nor did it include a microporous layer (MPL). These two characteristics are fundamental if this electrode had been used in a common gas-fed CO 2 RR reactor [18]. In gas-fed reactors, the MPL and the hydrophobic treatment produce water repellent properties that can prevent the carbon fiber backing from flooding. In bicarbonate electrolyzers, the hydrophobic feature inhibits the transport of bicarbonate from the flow field toward the BPM, where the low-pH region is located. In this way, the production of i-CO 2 drastically decreases, hence also the FE CO , J CO , and the CO 2 utilization (Figure 3). By using a hydrophobic carbon support (sample C), the FE CO decreases to 23%, while J CO and the overall activity (J tot ) ( Figure S1a) are significantly affected as well.  Once the importance of using a GDE with no hydrophobic treatment and presence of a catalyst on both its faces has been confirmed, the silver mass loading was optimized by modulating the sputtering time. The performances of GDEs with silver mass loading of 116 μg/cm 2 (sample D), 565 μg/cm 2 (sample B), and 1.13 mg/cm 2 (sample E) were explored by carrying out electrolysis in the flow cell and an EIS analysis in a three-electrodes set-up. As reported in Figure 4a, the sample with 116 μg/cm 2 of silver shows the lowest FE (55%), while the other two samples with higher mass loading exhibit better selectivity toward CO. However, since the 1.13 mg/cm 2 sample did not provided any improvement in selectivity with respect to 565 μg/cm 2 , the latter was identified as optimal catalyst load-  Once the importance of using a GDE with no hydrophobic treatment and presence of a catalyst on both its faces has been confirmed, the silver mass loading was optimized by modulating the sputtering time. The performances of GDEs with silver mass loading of 116 µg/cm 2 (sample D), 565 µg/cm 2 (sample B), and 1.13 mg/cm 2 (sample E) were explored by carrying out electrolysis in the flow cell and an EIS analysis in a three-electrodes set-up. As reported in Figure 4a, the sample with 116 µg/cm 2 of silver shows the lowest FE (55%), while the other two samples with higher mass loading exhibit better selectivity toward CO. However, since the 1.13 mg/cm 2 sample did not provided any improvement in selectivity with respect to 565 µg/cm 2 , the latter was identified as optimal catalyst loading since it achieved an FE CO value of 77%, namely, to the best of our knowledge, the lowest loaded silver-based GDE reported in the literature so far (Table 1). Most probably, the great amount of material deposited in sample E lowered the permeability of the GDE, inhibiting the mass transport of bicarbonate and affecting the selectivity. The performance in terms of CO 2 utilization followed a similar trend to the Faradaic efficiency: it was doubled by increasing the silver loading from 116 µg/cm 2 to 565 µg/cm 2 , while, with sample E, the increase to 1.13 mg/cm 2 of silver loading did not further enhance the CO 2 utilization. J CO and J tot ( Figure S1a) increased with higher loadings as confirmed by the EIS analysis (Table S3 and Figure S2). Indeed, the increasing trend of activities observed during bicarbonate electrolysis could be related to the value of the charge transfer resistance (R ct ). This parameter describes the catalyst's ability to exchange electrons with the reactants, applicable to both the CO 2 RR and HER. R ct decreases from 1.42 Ω cm 2 to 0.92 Ω cm 2 when augmenting the amount of silver from 116 µg/cm 2 to 565 µg/cm 2 (Figure 4b). A further decrease (0.38 Ω cm 2 ) was experienced with the highest loaded sample (E). Since the electrochemical surface area (ECSA) is considered to be proportionally associated to the double layer capacitance C dl derivable from the EIS analysis (Table S3) [22], the intrinsic activity of various materials can be compared by investigating the C dl normalized current densities ( Figure S3) [23]. This investigation confirmed 565 µg/cm 2 as the optimal mass loading since it showed the highest C dl normalized current density, hence the largest presence of active sites for the CO 2 RR to CO. However, the higher mass activity obtained with sample D (87.1 mA/mg Ag ) compared to samples B and E highlights the excellent performance of this type of GDE even at very low mass-loading (Figure 4c).  This work * This is the nominal loading; the experimental one was not reported by T. Li et al. [7]. ** Loading not present since a silver foam was used as a free-standing GDE. As already mentioned, the structural characteristics of the carbon composite electrode are crucial in the determination of the catalytic behavior of the GDE in bicarbonate electrolyzers. In particular, the choice of the GDL is critical, as its permeability to the bicarbonate solution directly impacts the i-CO2 production efficiency. It is known that the catalyst's selectivity toward CO tends to increase when the system is more proficient in  This work * This is the nominal loading; the experimental one was not reported by T. Li et al. [7]. ** Loading not present since a silver foam was used as a free-standing GDE.
As already mentioned, the structural characteristics of the carbon composite electrode are crucial in the determination of the catalytic behavior of the GDE in bicarbonate electrolyzers. In particular, the choice of the GDL is critical, as its permeability to the bicarbonate solution directly impacts the i-CO 2 production efficiency. It is known that the catalyst's selectivity toward CO tends to increase when the system is more proficient in producing i-CO 2 [24].
This observation was further confirmed by comparing the performance of the same GDE (sample B) using a less concentrated bicarbonate solution. When the concentration is halved from 2 M to 1 M, the carbon feedstock is poorer and the i-CO 2 generated drops. This introduces a mass transport limitation, causing a decrease in FE CO from 77% to 55%, while the CO 2 utilization drastically increased from 40% to 83%, as reported in Figure 5. is halved from 2 M to 1 M, the carbon feedstock is poorer and the i-CO2 generated drops. This introduces a mass transport limitation, causing a decrease in FECO from 77% to 55%, while the CO2 utilization drastically increased from 40% to 83%, as reported in Figure 5. Increasing the permeability of the GDL would have a similar effect to using a higher electrolyte concentration. This improvement allows for enhanced flow of bicarbonate through the GDE, reaching the BPM, and consequently, the low-pH region becomes capable of producing a larger amount of i-CO2. Therefore, sample B was compared, whilst keeping the same mass loading (565 μg/cm 2 ), to a GDE (sample F) whose GDL has a permeability that is four times higher. The effect of permeability is evident in Figure 6a, which shows the amount of CO2 released inside the reactor as a function of the GDE's permeability. The graph presents the total i-CO2 produced, which was calculated by summing the concentrations of CO2 and CO detected at the electrolyzer outlet during electrolysis.
However, as shown in Figure 6b, the improvement in i-CO2 production given by the high permeability of sample F did not provide an enhancement of selectivity; in fact, FECO dropped from 77% in sample B to 58%. Most probably, having a very open structure (see FESEM micrographs in Figure S4), which allows it to be more permeable to the bicarbonate, introduces a problem of mass transportation of i-CO2 toward the active sites, af- Increasing the permeability of the GDL would have a similar effect to using a higher electrolyte concentration. This improvement allows for enhanced flow of bicarbonate through the GDE, reaching the BPM, and consequently, the low-pH region becomes capable of producing a larger amount of i-CO 2 . Therefore, sample B was compared, whilst keeping the same mass loading (565 µg/cm 2 ), to a GDE (sample F) whose GDL has a permeability that is four times higher. The effect of permeability is evident in Figure 6a, which shows the amount of CO 2 released inside the reactor as a function of the GDE's permeability. The graph presents the total i-CO 2 produced, which was calculated by summing the concentrations of CO 2 and CO detected at the electrolyzer outlet during electrolysis. Nanomaterials 2023, 13, x FOR PEER REVIEW 9 of 11

Conclusions
In this work, novel high-performance Ag electrodes for bicarbonate electrolyzers were fabricated via a simple and scalable sputtering method. Silver thin films were deposited on commercial carbon supports and used as free-standing gas diffusion electrodes without any post-treatment. Thanks to the highly repeatable deposition technique, GDEs with different carbon substrates and silver mass loadings were reliably tested at Vcell = 3 V to understand their effect in terms of activity and selectivity in CO2-to-CO conversion. The final result of this investigation presents Ag-GDEs with a FECO close to 80%, which is comparable to the state-of-the-art achievement with a mass loading of 565 μg/cm 2 (sample B). This mass loading is significantly lower compared to the well-performing Ag-GDEs reported in the literature. Moreover, increasing the permeability of the carbon GDL significantly enhanced the activity and, consequently, the mass-activity. As a result, sample F exhibited remarkably high partial mass activity compared to the values reported in the literature for bicarbonate electrolyzers. The new Ag electrode reported respectable results in terms of CO2 utilization, which turned out to be around 40%, while, when the bicarbonate concentration was halved to 1 M, it reached 83%. Additionally, our research marks a significant advancement in the field of GDE development for bicarbonate electrolyzers by introducing the application of electrochemical impedance spectroscopy. This innovative technique provided us with a valuable opportunity to delve deeper into the underlying factors that influenced the GDE's performance within the reactor. In fact, the charge transport resistances and the double-layer capacitances derived from the fitting of the experimental Nyquist plot provided an effective explanation for the different behaviors of However, as shown in Figure 6b, the improvement in i-CO 2 production given by the high permeability of sample F did not provide an enhancement of selectivity; in fact, FE CO dropped from 77% in sample B to 58%. Most probably, having a very open structure (see FESEM micrographs in Figure S4), which allows it to be more permeable to the bicarbonate, introduces a problem of mass transportation of i-CO 2 toward the active sites, affecting the FE CO . The R ct provided by the EIS analysis in sample F is around three times lower (Figure 6c), meaning that it includes a higher number of active sites for catalysis, either for CO 2 RR or HER, as evidenced by the double-layer capacitance and displayed in Figure 6d. The slightly larger value of the C dl of the most permeable GDE, 1.06 mF/cm 2 compared to 0.92 mF/cm 2 , indicates a higher ECSA and confirms the presence of a larger number of active sites. The R ct and C dl values account for the high values of J tot (Figure S1a), partial mass activity ( Figure S1b), and J CO observed in sample F, ensuring a good CO 2 utilization percentage even with a lower FE CO and increased i-CO 2 production. In fact, the partial mass activity for CO was found to be 40 mA/mg Ag (Figure S1b), surpassing values reported in the literature (Table 1). It is important to emphasize that despite the lower Faradaic efficiency, the significantly high J CO achieved, explained by the higher ECSA, makes sample F likely the most suitable GDE for industrial purposes in syngas production.

Conclusions
In this work, novel high-performance Ag electrodes for bicarbonate electrolyzers were fabricated via a simple and scalable sputtering method. Silver thin films were deposited on commercial carbon supports and used as free-standing gas diffusion electrodes without any post-treatment. Thanks to the highly repeatable deposition technique, GDEs with different carbon substrates and silver mass loadings were reliably tested at V cell = 3 V to understand their effect in terms of activity and selectivity in CO 2 -to-CO conversion. The final result of this investigation presents Ag-GDEs with a FE CO close to 80%, which is comparable to the state-of-the-art achievement with a mass loading of 565 µg/cm 2 (sample B). This mass loading is significantly lower compared to the well-performing Ag-GDEs reported in the literature. Moreover, increasing the permeability of the carbon GDL significantly enhanced the activity and, consequently, the mass-activity. As a result, sample F exhibited remarkably high partial mass activity compared to the values reported in the literature for bicarbonate electrolyzers. The new Ag electrode reported respectable results in terms of CO 2 utilization, which turned out to be around 40%, while, when the bicarbonate concentration was halved to 1 M, it reached 83%. Additionally, our research marks a significant advancement in the field of GDE development for bicarbonate electrolyzers by introducing the application of electrochemical impedance spectroscopy. This innovative technique provided us with a valuable opportunity to delve deeper into the underlying factors that influenced the GDE's performance within the reactor. In fact, the charge transport resistances and the double-layer capacitances derived from the fitting of the experimental Nyquist plot provided an effective explanation for the different behaviors of the GDEs during bicarbonate electrolysis. Therefore, by using EIS as a powerful characterization tool for GDEs in bicarbonate electrolyzers, this work contributes to the growing body of knowledge in this emerging field of research.
The profound insights gained from this study offer a comprehensive understanding of the intricate electrochemical processes taking place within GDEs during bicarbonate electrolysis. Based on the results obtained by this work, the herein-proposed Ag GDEs demonstrate exceptionally promising potential for low-cost electrodes in the future industrial implementation of integrated carbon capture and conversion through bicarbonate electrolyzers.
Supplementary Materials: The following supporting information can be downloaded at: https:// www.mdpi.com/article/10.3390/nano13162314/s1. Tables S1 and S2 on the features of commercial carbon papers and Ag-GDEs; Figure S1 reporting the total density current and the partial mass activity; details on the reactor set-up; formulas used to calculate Faradaic efficiencies, partial density current, i-CO 2 , CO 2 utilization, mass activity, and partial mass activity; details on and results (Table S3 and Figure S2) of the EIS analysis; Figure S3 reports the values of J tot /C dl ; Figure S4 displays the FESEM images of the GDEs. Ref. [25] is cited in the Supplementary Materials.