The product selectivity zones in gas diﬀusion electrodes during the electrocatalytic reduction of CO 2 †

Here we report on the most prominent factors influencing the performance of a Cu-based CO 2 electrolyzer operating at high currents. Using a flow-electrolyzer design where CO 2 gas feed passes directly through the electrode interacting with the Cu catalyst layer, we observed that the selectivity of the electrochemical CO 2 reduction in (bulk) pH neutral media can greatly be influenced by adjusting the structure of the electrode. In this, the variations in catalyst loading and ionomer content can profoundly aﬀect the selectivity of CO 2 RR. We explore the hypothesis that this originates from the overall mass transport variations within the porous catalytic layer of the gas diﬀusion electrode. As further evidence for this, apart from the CO 2 electrolysis results, we propose a special method to benchmark the reactant mass transport in flow-cells using oxygen reduction reaction (ORR) limiting current measurements. Our analysis suggests that a restriction of mass transport is highly desirable due to its connection to a local alkalization and corresponding suppression of pH-dependent reaction products, given the absence of local CO 2 concentration limitations. We further show how the electrode structure can be used to push the observed catalytic CO 2 reduction selectivity either towards C 1 or C 2+ products, dependent on the ionomer content and catalyst loading in a cathodic current range of 50 to 700 mA cm (cid:2) 2 . Measurements at various KHCO 3 electrolyte concentrations agree with the notion of the local pH dictating the overall selectivity and point towards the presence of pronounced concentration gradients within the system. Overall, our work suggests that the diﬀerences in electrocatalytic CO 2 reduction selectivity at high currents (in a range of pH neutral buﬀering electrolytes) largely originate from the local concentration gradients defined by the initial catalyst ink formulation and architecture of the catalytic layer, both of which represent a powerful tool for optimization in the production of selected value-added products. The electrocatalytic CO 2 reduction reaction (CO 2 RR) on Cu-based catalysts has the potential to enable the sustainable production of commodity chemicals and fuels by upcycling waste-CO 2 into value-added compounds. Over the recent years, much progress has been made by fabrication of catalysts into so-called gas diﬀusion electrodes (GDEs) to tackle the issue of low CO 2 solubility in aqueous electrolytes and to advance towards commercially viable current densities of 4 300 mA cm (cid:2) 2 . Though the selectivity towards CO 2 RR could be largely improved over the competing HER using GDEs, the underlying factors for an eﬃcient production of the individual CO 2 RR products remain elusive. In the present study, we deploy a flow-electrolyzer system to investigate structure–selectivity- interrelations of a Cu-based GDE in a buffering electrolyte. By systematic investigation of three parameters: (i) particle catalyst loading, (ii) ionomer to catalyst ratio and (iii) buffer capacity, we set out to understand the structural properties that dictate the spatial variation of the selectivity across the catalyst layer at high reaction rates. Thereby, we describe a sequence of zones of distinct selectivity within the catalyst layer (‘‘selectivity zones’’), which arise from the inhomogeneous distribution of the reactants (CO 2 and pH) and control the overall selectivity of the system.


Introduction
The direct electrochemical CO 2 reduction reaction (CO 2 RR) has been emerging as a potential technology for storage of renewable energy and sustainable production of carbon-based chemicals. 1 In this area, the catalyst research has mainly been focused on Cu due to its capability to reduce CO 2 towards valueadded, post-CO products, such as hydrocarbons and alcohols. 2 The control over the electrocatalytic selectivity has been the focal point of Cu-based catalyst research, due to parallel reaction pathways and the resulting mixture of products. 3 Various modifications of Cu have been investigated in order to steer the selectivity towards distinct products, as for instance exposure of specific facets through nanostructuring and altered catalyst composition through oxidative treatments or addition of second metals. [4][5][6][7] Apart from the catalyst itself, the reaction conditions have been repeatedly reported to influence the selectivity of the CO 2 RR. For instance, local pH value gradients establishing at the electrode electrolyte interface, also described as alkalization, were shown to have a decisive impact on reaction selectivity by suppression of mechanistic pathways dependent on the proton transfer as a rate-limiting step. [8][9][10] Studies performed in very commonly used KHCO 3 electrolytes with neutral bulk pH, show that the local pH gradients near electrode surface essentially arise from a deficient mass transport unable to buffer the cathodic production of OH À . [11][12][13] For H-type setups, effects of variations in the structure of the catalytic layer have been repeatedly reported to influence the mass transport, critically altering the reaction environment and therefore determining the observed selectivity of the system during electrochemical CO 2 RR. Here, the mass transport can be divided into a transport of reactants directed towards the surface and a transport of products leaving the surface. On the reactant side, in the aqueous electrolyte dissolved, CO 2 is transported towards the catalytic sites, where abundantly available water molecules supply the protons to form reduced carbon compounds under production of OH À . The generated OH À can readily react with the commonly used HCO 3 À electrolyte acting as a buffer. However, HCO 3 À transport from the bulk towards the surface is not sufficiently fast to keep up with the OH À production rate, which locally shifts the pH and bicarbonateequilibrium near the reaction sites. This effect of local alkalization during CO 2 RR was observed experimentally at already moderate potentials by surface enhanced IR and Raman spectroscopy, simulated based on bicarbonate equilibria and often suggested to be the origin of a high selectivity for multi-carbon products during electrochemical CO 2 RR. 12,[14][15][16][17][18] On the products side, carbon compounds need to be transported away from the surface to allow for further reactants to fill in. However, the sustained presence of reactive intermediates such as CO have also been reported to show a beneficial effect on production of ethylene and oxygenates, and was also suggested to show a suppression for the competing HER from water reduction due to the occupation of the reactive sites. [19][20][21][22][23] Generally, an increasing thickness of the catalytic layer, together with the associated electrochemically active surface area (ECSA), increases the mean path of transportation for the reactants and products. This has been proposed to impede a homogeneous through-plane mass transport within the catalytic layer, which results in more pronounced concentration gradients throughout the system. 12,15,24 Accordingly, it has been suggested for mesoporous Ag electrodes of various thicknesses that the CO 2 RR selectivity is sensitive to the concentration gradients and shows the strongest suppression of the competing HER for the thickest electrode at the lowest part of the catalytic layer, where the effect of alkalization was most pronounced. 25,26 Recently, the field of CO 2 RR has progressively moved towards studies of the high current regime in pH neutral and alkaline, gas-feed flow-electrolyzers to approach technological rates. [27][28][29] As the cathodic production of OH À is a function of the current, flow-electrolyzers in buffered electrolytes have been suggested to be particularly affected by local alkalization due to insufficient HCO 3 À transport and the observed high selectivity for C 2+ products has been, at least in part, associated to that effect. [30][31][32] Additionally, the depletion of CO 2 near the catalyst surface has also been reported to limit the accessible CO 2 RR currents and greatly influence the observed catalytic selectivity. [33][34][35] Despite those indications for the crucial role of the electrode structure for high-current CO 2 RR, correlations similar to the impact of mass transport in low-current H-cells remain underexplored for gas diffusion electrodes in flow-electrolyzers. It is plausible that high rate CO 2 RR on GDEs in flow-cell electrolyzers shows the same fundamental correlations of mass transport and catalytic selectivity as those reported for H-cell setups.
We propose that the catalytic selectivity of Cu during high rate CO 2 RR in pH buffering KHCO 3 electrolyte is largely controlled by the mass transport, which can be rationalized by a discussion of CO 2 transport and transport of pH buffering HCO 3 À anions.

Flow-cell electrolyzer setup
We employed a flow-cell electrolyzer with three distinct compartments to investigate CO 2 RR electrolysis at high currents and catalytic rates (Fig. 1a). Two different solutions of 1 M KHCO 3 were used separately as anolyte and catholyte and continuously looped through the two liquid compartments divided by an anion conducting membrane. Anodic and cathodic reaction products were transported out of the respective compartments with the flow of the electrolytes. A convective stream of CO 2 was fed from the third compartment through the backside of the porous cathode towards the catalytic layer, which allowed a fast supply of reactant to the cathodic reaction sites.

Cathode electrode design and architecture
The cathode catalyst layer was deposited by airbrushing an ink containing a mixture of Nafion and cubic Cu 2 O nanoparticles on a carbon-based Freudenberg H23C2 gas diffusion layer serving as substrate. As anode, a commercially available dimensionally stable electrode composed of a Ti sheet covered by an Ir-MMO was routinely used. Throughout this study, we will refer to the uncoated Freudenberg H23C2 as the gas diffusion layer, ''GDL'', and to the particle-coated Freudenberg H23C2 as gas diffusion electrode, ''GDE''. Fig. 1b shows the schematic structure of a GDE prepared by spraycoating. In this system, the different elements of the GDE are spatially separated and can be assigned to different layers. The lowest layer consists of carbon fibers and acts as mechanical and conductive backbone of the entire structure. Next, the microporous layer (MPL) functions as conductive and hydrophobic substrate, which allows the electronic and CO 2 transport towards the adjoining catalytic layer. The hydrophobicity, gas permeability and electrical conductivity of the GDL are important parameters that influence the CO 2 RR performance and stability of the GDE. Especially, the hydrophobicity has proven decisive to maintain a sufficient gas (CO 2 ) transport towards the catalytically active sites by preventing a ''flooding'' that is an extensive wetting of the porous GDE structure. For carbon-based GDLs an instability of the wetting characteristics has been observed under application of cathodic potentials and correlated to the catalytic activity towards HER of the carbon structure. 36 To circumvent this effect, PTFE membranes have been investigated as GDL materials, but can suffer from issues of electrical conductivity and mechanical instability. 29 In this study, we use a ''flow-through'' approach, depicted in Fig. 1(b), to minimize flooding issues connected to the use of a carbon-based substrate and focus exclusively on properties of the catalytic layer. The catalytic layer represents the uppermost element of the GDE and is the interface between gaseous transports of CO 2 and liquid transport of electrolyte. Within the catalytic layer, the electronic, ionic and reactant transport intersect and define the reaction environment of the electrocatalytic CO 2 RR and the reactivity of the system. The morphology of the catalytic layer obtained by spraycoating is not trivial and showed a porous, 3-dimensional appearance with a rough surface, visible in cross-section and top-view SEM images of Fig. 1b.
In this paper, we use a previously reported nanocubic Cu 2 O catalyst (see Fig. S1, ESI †) with an edge length of 35 nm to systematically alter the structure of the catalytic layer of a gas diffusion electrode (GDE) for tests in a flow-electrolyzer. 37 By changing macroscopic parameters, as the particle catalyst loading and the ionomer to particle catalyst ratio (Nafion content), we influence the accessibility of catalytically active sites and the through-plane mass transport in the porous structure of the catalytic layer. In this, we correlate the electrode structure with restriction in mass transport, manifesting in local concentration gradients and alkalization, which in turn influences the selectivity of CO 2 RR during a high current density operation in a bulk neutral bicarbonate electrolyte. We chose our previously reported and well-characterized cubic Cu 2 O catalyst as a model catalyst system to investigate the influence of concentration gradients within a flow-cell electrolyzer by variation of three macroscopic parameters: Particle catalyst loading: first, we varied the amount of deposited catalyst particles to obtain GDEs with various catalyst loadings that show differences in layer thickness, roughness and ECSA. In doing so, we affect the mean path of transportation from the bulk sources of CO 2 and KHCO 3 towards the catalytic sites.
Ionomer to particle catalyst ratio: to introduce an impediment for the mass transport, we varied the Nafion content of the ink formulation to obtain GDEs that show different ionomer to catalyst ratios for a constant absolute catalyst loading. Nafion acts as a strong adhesive to introduce a mechanical stability to the catalytic layer, however, the ionomer distribution is a known issue in fuel cell research due to its influence on local reactant transportation and associated mass (oxygen) transport resistances. 38,39 Likewise, the transport of reactants in CO 2 RR towards the active sites should also be sensitive to the local distribution of the ionomer, acting as a barrier for the CO 2 and HCO 3 À transport.
Buffer capacity: to induce various buffer capacities, we varied the concentration of the KHCO 3 electrolyte to alter the buffer capacity within our system. A higher concentration of HCO 3 À offers more buffer capacity, in turn resulting in decreased pH gradients at the interface and counteracting the effect of alkalization. The present work is not about setting new number records in product selectivity, but to pinpoint controlling factors for the product selectivity in a technological GDE under more realistic reaction conditions. To characterize the mass transport properties of CO 2 RR GDEs, we employ oxygen reduction limiting current measurements typically used in the hydrogen fuel cell community as diagnostic tool in the field of CO 2 reduction, the results of which reveal how closely GDE structure and the resulting catalytic selectivity are connected. The conclusions of this work are consistent with previous reports on the importance of near electrode surface pH and CO 2 concentration, but expand our understanding of the relationships between catalyst layer structure of a GDE and reaction selectivity during CO 2 RR. 12,29,31,33,40,41 The systematic investigation of the effects within our work prompt us to propose the notion of layered ''selectivity zones'', which has not been, to the best of our knowledge, previously described for a Cu-based GDE in a flow-electrolyzer. We believe that our selectivity zone model will aid the future design of efficient Cu-based GDEs for CO 2 electrolyzers in buffered electrolytes of near-neutral pH. View Article Online

Effect of particle catalyst loading on CO 2 electrolysis
In Fig. 2, we present the distributions of four important products observed during CO 2 RR on Cu: C 2 H 4 , CH 4 , H 2 and HCOO À , obtained at fixed applied current densities on electrodes containing varying catalyst loadings. The influence of catalyst loading on the product distribution has been tested at fixed concentration of 1.0 M KHCO 3 and at fixed binder content (10 wt% Nafion). Here, the FE of C 2 H 4 , CH 4 , H 2 and HCOO À is displayed as a function of the applied current density for catalyst mass loadings ranging from 0.3 mg cm À2 to 2.0 mg cm À2 . We specifically focus on this set of products, as they have distinctly different rate-limiting reaction steps, which show either a strong pH-dependence (CH 4 , HCOO À and H 2 ) or primarily independence (C 2 H 4 ) and can therefore provide insight in the local reaction environment. 42,43 A first key observation is the clear suppression of all pH-dependent products (CH 4 , HCOO À and H 2 ) at high mass loadings of the catalyst, which was invariably linked to a favored production of ethylene. Note how the FE of CH 4 , which is a preferred product during CO 2 RR at high proton concentration, plummeted to below 1%, as soon as catalyst loading was increased to 1.3 mg cm À2 and higher. In contrast, in experiments using very low catalysts loadings of below 0.4 mg cm À2 the FE for CH 4 raised to above 20%, see Fig. 2b. While this trend was qualitatively in line with the production of H 2 and HCOO À (Fig. 2c and d) the change in FE for C 2 H 4 showed the opposite behavior, see Fig. 2a. Here, the decrease of catalyst loading below 0.4 mg cm À2 resulted in a FE for C 2 H 4 of below 20%, whereas higher loadings allowed for a more selective C 2 H 4 production and increased FE to around 30%. Due to the well-known sensitivity of CO 2 RR selectivity to the electrode potential, we plotted the product FE against IR-free RHE potentials in Fig. S2 (ESI †). Note that as the shift in selectivity is also visible on an IR-free potential scale, we thereby succeed in excluding variations in electrode potential as the sole origin of the observed effect. Additional information of FE for the remaining CO 2 RR products (EtOH, PrOH and CO) are given in Fig. S3 (ESI †) and agree with the observed favorable production C 2+ compounds at high catalyst loadings. We also plotted the FE of gas products as a function of time, see Fig. S4   View Article Online electrolysis are given in Fig. S5a and b (ESI †). We observed a progressive roughening and introduction of pores to the surface upon increase of particle loading. Such structural changes suggest an increase in electrochemically accessible surface area (ECSA), which we have investigated by quantification of the electrochemical charging of the double layer (see Fig. S6, ESI †). As a measure of the ECSA, we calculated the double-layer capacitance, shown in Fig. S5c (ESI †), which showed an increase with particle loading and agrees with our observation of a progressive surface roughening in SEM images. In accordance with an increased ECSA, we noticed a higher catalytic activity during CO 2 RR for the high particle loadings visible in the polarization curves of Fig. S5d (ESI †). Our observations suggest that the catalytic selectivity during high-rate CO 2 RR is sensitive to the structure of the catalytic layer, which can be affected by variation of the catalyst loading. We suspect that the correlation between catalytic selectivity and catalyst loading originates in changes of the mass transport (e.g. transport of CO 2 and HCO 3 À ), which in turn affect the local pH and reactant concentration near the electrode.
Effect of particle catalyst to ionomer ratio (Nafion content) on CO 2 electrolysis In order to further investigate the mass transport as potential origin of shifts in catalytic selectivity, we varied the binder content within the catalytic layer. Inspired by fuel cell research, we suspect that increasing amounts of ionomer within the catalytic layer represents a barrier for the mass transport of reactive species as dissolved CO 2 and HCO 3 À towards reaction sites. Fig. 3 shows the effect of an increase in Nafion content within the catalytic layer of a GDE on the selectivity during CO 2 RR. A suppression of CH 4 and HCOO À is evident in samples with high Nafion content, see Fig. 3b and d, similar to what we have observed at high catalyst mass loadings. Interestingly, samples with high Nafion content (30 and 50 wt%) show a suppression of HER and increased C 2 H 4 FE only at a relatively low current density of smaller than 300 mA cm À2 (Fig. 3a and c).
A further increase of current density, results in a strong rise of FE for HER at the cost of total CO 2 RR FE. We suspect that this change in selectivity at high currents is caused by an excessive content of Nafion, which reduces the mass transport to a point, where the reactant (CO 2 ) transport becomes limiting for CO 2 RR and causes the HER to dominate in the process. While such a correlation between the Nafion content and the limited reactant transport is restricting for CO 2 RR selectivity for a current density larger than 300 mA cm À2 , it shows an increase at lower rates. Excessive amounts of ionomer influence potentially the electrical accessibility of the catalyst particles, which is why we investigated the change in electrochemical double layer capacitance and catalytic activity. Here, we only observed minor changes in double layer capacitance with varied Nafion loading, but a lower catalytic activity of the 50 wt% Nafion sample was apparent (see Fig. S7, ESI †). Again, to exclude differences in electrode overpotential as cause of the observed trend, we plotted IR-free RHE electrode potentials against the product FE in Fig. S8 (ESI †), which still clearly shows the ionomer induced shift in selectivity. In agreement with our previous observation, the FE for gas products as a function of time showed only small changes at constant current for the electrodes prepared with different Nafion loadings, see Fig. S9 (ESI †), suggesting a stability of the system over the investigated testing time. Furthermore, we have also investigated the change in surface structure at different Nafion contents by SEM, shown in Fig. S10 (ESI †). Here, an intermediate content of Nafion (10 and 30 wt%) resulted in a rough surface of the catalytic layer, whereas the extreme cases of 0 wt% and 50 wt% showed a relatively smooth surface. Noteworthy is the pronounced coverage of the Cu 2 O cubes supposedly by the ionomer in the 50 wt% Nafion sample, visible in images of higher magnification, consistent with the idea of representing a distinct barrier for the mass transport. Additional CO 2 RR products (CO, EtOH and PrOH) are given in Fig. S11 (ESI †), which showed a higher selectivity for EtOH with increased Nafion content at moderate currents. Our observations on the effects of increased Nafion content are qualitatively in line with the effect of particle catalyst loading. In both cases, we generally observed a higher selectivity for C 2+ products when either binder content or particle loading was increased. It seems feasible that a similar origin causes the observed selectivity shifts, given their high qualitative agreement.

Effect of buffer capacity (KHCO 3 concentration) on CO 2 electrolysis
Fig. 4a-f shows the influence of the bulk KHCO 3 concentration on the C 2+ (C 2 H 4 , EtOH and PrOH) and C 1 (CH 4 , HCOO À ) selectivity during CO 2 electrolysis in the flow-cell. Here, we used different Nafion contents of 10 wt% to 50 wt% and a constant catalyst loading of about 0.7 mg cm À2 . For the 50 wt% Nafion sample we observed no significant change in catalytic selectivity, when increasing electrolyte concentration from 0.1 M to 1.0 M KHCO 3 , see Fig. 4a and d. Both concentrations showed the highest C 2+ selectivity of roughly 40% FE at 200 mA cm À2 , whereas a larger current density resulted in the increase of the competing HER (Fig. S12a, ESI †). Further increase of KHCO 3 electrolyte to 3 M lowered the C 2+ FE and favored HER over the whole investigated current range. In contrast, the FE for C 1 products seemed largely unaffected by the change in KHCO 3 concentration. Next, the 30 wt% Nafion sample showed a clear dependence of C 2+ and C 1 FE on the KHCO 3 concentration during CO 2 RR, see Fig. 4b and e. While we were able to achieve a combined C 2+ FE of almost 70% at 600 mA cm À2 , the use of higher KHCO 3 concentrations of 1 and 3 M led to a decreased C 2+ FE to around 50% and 30%, respectively. For the FE of C 1 products we observed an inverse behavior, here 3 M KHCO 3 showed the highest combined C 1 FE of roughly 20%, while the use of 1 M and 0.1 M KHCO 3 led to a subsequent decrease. Our observations during CO 2 RR, using a 10 wt% Nafion sample were quite similar to the case of a 30 wt% Nafion sample, see Fig. 4c and f. Again, we achieved the highest C 2+ selectivity at the lowest KHCO 3 concentration of 0.1 M, Fig. 4 Effect of variations in KHCO 3 concentration on the CO 2 RR selectivity towards C 2+ products using 50 wt% (a), 30 wt% (b), and 10 wt% (c) of Nafion. Effect of variations in KHCO 3 concentration on the CO 2 RR selectivity towards C 1 products using 50 wt% (d), 30 wt% (e), and 10 wt% (f) of Nafion. In all cases Cu 2 O loading was const. at 0.7 mg cm À2 . Additional information on FE of H 2 and CO are given in Fig. S12 (ESI †). which enabled a combined FE of almost 60% over a broad range of cathodic currents. The use of an increased KHCO 3 concentration of 1 and 3 M resulted in a dramatically decreased C 2+ FE of 40% and 5%, respectively. At the same time, the highest C 1 FE observed on the 10 wt% Nafion sample increased from a maximum of 13%, towards 17% and roughly 23% for respective KHCO 3 concentrations of 0.1 M, 1.0 M and 3.0 M. In parallel to the CO 2 RR, the HER also proved sensitive to KHCO 3 concentration and showed an overall increase with KHCO 3 concentration, whereas the 50 wt% sample seemed to be generally less sensitive to the buffer concentration (Fig. S12a-c, ESI †). At all Nafion contents we observed a higher selectivity for C 2+ products and generally lower HER and C 1 FE, when we employed KHCO 3 electrolytes of a lower concentration during electrolysis, however, this effect seemed to be dependent on Nafion content and was most pronounced for the lowest Nafion content of 10 wt%.
Implementation of the ORR as a diagnostic tool for benchmarking the mass transport limitations within a complex porous electrode system As the effects of the local pH, the mass transport and the catalyst kinetics are superimposed and, therefore, often difficult to be unambiguously deconvoluted, especially due to parallel reaction pathways of CO 2 RR on Cu and the competing HER, we resorted to the oxygen reduction reaction (ORR) for further discussion of the correlation between binder content and mass transport. In doing so, we were able to exploit the more positive standard reduction potential of the ORR, with respect to the CO 2 RR, to fully avoid the HER. Hence, we obtained data that we can interpret with overall less complexity, schematically depicted in Fig. 5a. We take the view that such an approach allows for a more direct investigation of the mass transport limitations within our system. To probe the mass transport towards the catalytically active centers of the Cu 2 O particles, we varied the partial pressure of O 2 in an N 2 feed at a constant electrode potential of À0.45 V RHE . We chose this potential to achieve the highest possible rate of ORR, while avoiding a region of considerable HER activity, indicated in Fig. 5b. By tracing the change in ORR current as a function of O 2 partial pressure at a fixed electrode potential, we can directly access changes in mass transport caused by variations in binder content. In Fig. 5c, we can see a rise in ORR current with increase in partial pressure of O 2 until around 0.3 bar, where the ORR current of the 10 wt% Nafion sample approaches a plateau. This transition supposedly originates in a change from a primarily mass transport dominated regime, towards one, were activation resistances are denying higher reduction rates. The regimes of mass transport and catalytic kinetics are indicated by different levels of shading in Fig. 5c, but should be rather understood as a visual orientation and not as a strict border between the two. A comparison of three samples with Nafion loadings ranging from 10 to 50 wt% shows an increased ORR current in the mass transport domain of below 0.3 bar of O 2 partial pressure for lower loadings of the ionomer, however, this difference seemed to decrease progressively with a higher partial O 2 pressure (Fig. S13, ESI †). The observed behavior suggests that the mass transport remains limiting even at higher O 2 partial pressure for samples of high Nafion content, whereas samples of reduced binder content showed primarily kinetic limitations at a similar partial pressure of O 2 and constant electrode potential. Our results suggest that the binder content of the catalytic layer of a GDE interferes with the reactant transport. Here, a high binder content induces larger resistances for the reactant transport and can lead to significant mass transport limitations.

Discussion
Electrode structure determines concentration gradients during CO 2 electrolysis Combining our observations, we can schematically depict the proposed influence of the catalytic layer structure on the selectivity during high-rate CO 2 RR electrolysis in a pH-neutral buffering media. Fig. 6a, shows a schematic GDE and illustrates the relevant reactions, as well as the through-plane transport of reactants and products in the catalytic layer during CO 2 RR. While CO 2 is fed in a gaseous state to the GDE, we take the view that CO 2 is highly likely to physically dissolve in the electrolyte prior to its reduction on the catalyst surface due to the presumable presence of a native solvent layer caused by the hydrophilicity of charged electrodes. Accordingly, the transport of reactive species (CO 2 and HCO 3 À ) and products has to occur through a diffusion layer of finite thickness to reach or leave the electrode surface. On the catalyst, OH À is being produced during the reductive reaction of CO 2 and H 2 O. The OH À can readily react with the present buffering HCO 3 À anions that are diffusively transported from the bulk electrolyte, which reduces the local pH increase near the surface and creates CO 3 2À in the process. The change of the local pH is a function of the current density that is a measure of the OH À production rate and the molar flux of HCO 3 À anions transported towards the electrode surface in a diffusive manner. The generated CO 3 2À is being transported towards the bulk of the electrolyte, where it can equilibrate with excess CO 2 to regenerate the buffer by formation of HCO 3 À , therefore, preventing larger changes in bulk pH. It is important to note that in GDEs the source of CO 2 and buffering HCO 3 À anions are on opposing sides as indicated by opposed directions of arrows in Fig. 6a. This phase asymmetric feed implies a largely decoupled transport of dissolved CO 2 and HCO 3 À towards the electrode surface of GDEs in flowelectrolyzers, which is in contrast to conventional electrodes that are fully submerged in liquid electrolytes during CO 2 RR in H-cell setups. The proposed effect for variation of ionomer to catalyst ratio (Nafion content) and particle catalyst loading is depicted in Fig. 6b-d and is largely associated to the through-plane concentration gradients of CO 2 and HCO 3 À within the catalytic layer.
Here, the effect of increasing the particle catalyst loading can be rationalized by a larger mean path of transportation for CO 2 and HCO 3 À through the thicker catalytic layer. This longer distance of transportation results in a further decrease along the concentration gradients for both species, see Fig. 6b and c. This would in turn cause regions of high alkalinity and depletion of CO 2 , respectively. We suspect that the increase in Nafion content causes a quite similar drop in reactant concentration throughout the layer. Here, as we have shown from our ORR measurements, an extensive content of Nafion in the catalytic layer presents a barrier for the mass transport of reactants, e.g. O 2 or CO 2 , towards the Cu sites. Such impediment of the mass transport can be rationalized by a slower through-plane transport of reactants (CO 2 and HCO 3 À ) and steeper associated concentration gradients perpendicular to the catalytic layer, see Fig. 6b and d. Essentially, the outcome is similar to the increased particle loading and results in regions of high alkalinity and depletion of CO 2 at high ionomer content. Additionally, both, the Nafion content and particle catalyst loading influenced the apparent morphology of the catalyst layer (see Fig. S5 and S10, ESI †), which has often been reported in literature to change the catalytic selectivity. However, given the comparatively small change in double layer capacitance (see Fig. S6 and S7, ESI †), we take view that such morphological changes did not critically influence the overall performance. A more detailed discussion on the change in morphology can be found in the ESI † of this work.
Finally, the effect of an increased KHCO 3 bulk concentration can also be rationalized by a discussion of the HCO 3 À concentration gradient. Here, the generally higher HCO 3 À concentration offers a higher buffer capacity and can in turn reduce the pH gradient throughout the catalytic layer. An additional effect could be caused by the sensitivity of the physical solubility of CO 2 for the ionic strength, which could lead to a depletion of CO 2 reactant at high KHCO 3 concentrations.
In line with the proposed emergence of concentration gradients, as suggested within the present work and visualised in Fig. 6, previous studies reported on considerable local deviations from bulk reactant concentrations during CO 2 RR based on calculations from transport models. Here, most studies focused on the electrode to catholyte interface and described a depletion in CO 2 concentration and an increase in OH À and CO 3 2À concentration in this near-electrode surface region. The magnitude of the emerging concentration gradients was suggested to be heavily dependent on the diffusion layer thickness, which is highly sensitive to convective interferences through effects such as buoyancy. 12,14,31,44 Studies that additionally included the thickness of an extended catalyst layer in their transport models reported on an inhomogeneous reactant concentration throughout the catalyst layer during high-rate electrolysis, which is qualitatively in agreement with our proposition depicted in Fig. 6. 26,32,45 Concentration gradients establish ''selectivity zones'' As a consequence of the through-plane concentration gradients for CO 2 and pH within the catalytic layer, we propose zones of distinctly different CO 2 RR selectivity as a function of distance from the MPL substrate in direction of the catholyte, shown in Fig. 7. Here, a schematic cross section of a GDE with indications for the suggested change in local reaction environment and catalytic selectivity dependent on the spatial location within the catalytic layer is depicted. The zone closest to the MPL shows the highest proximity to the gaseous CO 2 feed and furthest distance from the bulk KHCO 3 electrolyte, which results in a region of high pH and CO 2 concentration. With increasing distance from the MPL, those conditions reverse and can result in a CO 2 -deficient zone with lower pH value. Our observed experimental catalytic CO 2 selectivities directly correlate and support the zone model. Here, the region of high pH and CO 2 concentration directly adjacent to the MPL gives optimal conditions for selective production of pH independent CO 2 RR (C 2+ ) products, as ethylene. With further distance from the MPL, the pH value decreases and the catalytic selectivity can shift towards CO 2 RR products, which are preferred at higher proton concentration (C 1 ), e.g. CH 4 . Finally, in the outermost region of the catalytic layer CO 2 concentration might become deficient, which shifts the catalytic selectivity towards an increased competition by HER. The proposed ''selectivity zone'' model is qualitatively in line with recent computational studies that report on pronounced differences in spatial production rates for individual CO 2 RR products throughout the extended structure of the catalyst layer. Based on micro kinetic calculations, the studies revealed pronounced differences in local reaction rates that arise from a non-uniform reactant distribution. The reactant concentration gradients have been described to establish in-plane as well as through-plane of the catalyst layer, causing a complex spatial distribution in CO 2 RR and HER activity. 26,32,45,46 Based on the proposed selectivity zones, a selective CO 2 RR electrolyzer for production of C 2+ compounds in buffering electrolytes would require the deliberate introduction of an impediment for the transport of buffering anions. This could be realized by controlling the structure of the GDE through an increased thickness and a higher density of the catalytic layer, if the transport of CO 2 remains sufficient. Next to the discussed parameters within this work, further structural control of the catalytic layer could be achieved by variations in the deployed catalyst particle size or introduction of conductive supporting materials of a defined porosity. Additionally, operation conditions could achieve a similar effect and contribute for further increase in C 2+ selectivity. Here, lowering electrolyte flow-rates and avoiding bubble formation at the electrode to electrolyte interface could reduce the interfacial convection and in turn lead to creation of an increased hydrodynamic boundary layer thickness, further limiting the transport of buffering anions. We hypothesize that the notion of spatial ''selectivity zones'' (selectivity zone model) has a broader validity; as a result of this, the structure-selectivity-relationships described here should be also applicable to other (non-Cu) CO 2 RR systems or even to other reaction processes in GDEs. Similar interrelations of catalyst layer thickness and CO 2 RR selectivity in buffered electrolytes have been reported for CO evolving systems of Ag and Au catalysts, as well as for systems deploying Sn particles for selective formation of HCOO À . 25,[47][48][49][50][51] At its core, the selectivity zones model describes a dependency of the HER and CO 2 RR reaction rates on the spatial reactant concentration due to concentration overpotentials and accordingly should apply to various systems in the field of electrocatalytic CO 2 RR.

Conclusion
In this study, we have investigated relations between electrode structure, more specifically, catalyst loading and Nafion content, and the resulting product selectivity of Cu-based CO 2 RR electrolysis at high currents in a bulk pH-neutral flow-electrolyzer. We found that with increasing catalyst loading, that is catalyst layer thickness, or Nafion content the production of pH-sensitive products (e.g. H 2 , CH 4 and HCOO À ) could be suppressed and C 2+ species were produced more selectively. To explain this, we showed that the Nafion content influences the mass transport using an ORR limiting current analysis at varying oxygen partial pressure as a diagnostic tool. We concluded that such changes in mass transport define and control the local reaction environment in form of pH and CO 2 concentration, and hence can be used to deliberately tune the reaction selectivity. Here, concentration gradients in through-plane direction of the porous catalytic layer are more pronounced and shift the observed catalytic selectivity during CO 2 RR electrolysis. Varying the KHCO 3 electrolyte concentration showed that the selectivity of the system is highly sensitive to the concentration of the buffering media and agreed with our proposal that the local pH variations are crucial in determining the CO 2 RR selectivity. Our study demonstrates how the structure of the catalytic layer is a key parameter to influence local mass transport and provides an effective way to tune the selectivity during pH neutral (bulk) CO 2 RR electrolysis at high currents.

Conflicts of interest
There are no conflicts to declare.