Influence of Defects and H2O on the Hydrogenation of CO2 to Methanol over Pt Nanoparticles in UiO-67 Metal–Organic Framework

In catalysts for CO2 hydrogenation, the interface between metal nanoparticles (NPs) and the support material is of high importance for the activity and reaction selectivity. In Pt NP-containing UiO Zr-metal–organic frameworks (MOFs), key intermediates in methanol formation are adsorbed at open Zr-sites at the Pt–MOF interface. In this study, we investigate the dynamic role of the Zr-node and the influence of H2O on the CO2 hydrogenation reaction at 170 °C, through steady state and transient isotope exchange experiments, H2O cofeed measurements, and density functional theory (DFT) calculations. The study revealed that an increased number of Zr-node defects increase the formation rates to both methanol and methane. Transient experiments linked the increase to a higher number of surface intermediates for both products. Experiments involving either dehydrated or prehydrated Zr-nodes showed higher methanol and methane formation rates over the dehydrated Zr-node. Transient experiments suggested that the difference is related to competitive adsorption between methanol and water. DFT calculations and microkinetic modeling support this conclusion and give further insight into the equilibria involved in the competitive adsorption process. The calculations revealed weaker adsorption of methanol in defective or dehydrated nodes, in agreement with the larger gas phase concentration of methanol observed experimentally. The microkinetic model shows that [Zr2(μ-O)2]4+ and [Zr2(μ–OH)(μ-O)(OH)(H2O)]4+ are the main surface species when the concentration of water is lower than the number of defect sites. Lastly, although addition of water was found to promote methanol desorption, water does not change the methanol steady state reaction rate, while it has a substantial inhibiting effect on CH4 formation. These results indicate that water can be used to increase the reaction selectivity to methanol and encourages further detailed investigations of the catalyst system.


■ INTRODUCTION
The hydrogenation of CO 2 is receiving attention as a key reaction for sustainable production of fuels and value-added chemicals. 1−3 The activity and selectivity of CO 2 hydrogenation catalysts is strongly influenced by the nature of the metal− support interface. 4−8 For Cu-based catalysts, the presence of ZrO 2 or isolated Zr moieties close to Cu facilitates methanol formation by forming low coordinated Lewis acidic Zr-sites, where formate and methoxy groups form in the presence of CO 2 and H 2 . 9−11 Formate and methoxy groups are also observed at sites at the interface of Cu/Al 2 O 3 : at 4-coordinated sites, methanol forms from bidentate CO 2 bridged between two sites, via formate, while at 3-coordinated sites, CO formation from monodentate CO 2 is favored. 12 On Pt/Al 2 O 3 , it has been proposed that CO forms from carbonate-type intermediates on defective Al sites at the interface, either by O-abstraction by hydrogen, or by the filling of an oxygen vacancy. 13 Studies of the CO 2 hydrogenation reaction to methanol over metal functionalized metal−organic frameworks (MOFs) have also brought further evidence of interactions between the nanoparticles (NPs) and the support material. 14−18 Focusing here on the UiO-series of MOFs, they consist of 12-coordinated Zr 6 O 4 (OH) 4 12+ nodes connected by, e.g., benzene-1,4-dicarboxylic acid linkers (BDC; UiO-66) or biphenyl-4,4′-dicarboxylic acid linkers (BPDC; UiO-67), forming 3-dimensional, porous frameworks with fcc structure.
X-ray photoelectron spectroscopy (XPS) performed on Cu NPs at the UiO-66 surface showed evidence of Zr reduction in the presence of Cu, suggesting an interaction between the Cu NPs and the UiO-66 Zr-node. 14 Furthermore, An et al. reported XPS evidence of Zr reduction in CuZn@UiO-67 with 100% bipyridine type linkers, and proposed that the reaction proceeds by CO 2 adsorption at unsaturated Zr-sites followed by Hspillover from Cu to the Zr-node. 15 In two recent contributions from our group, we reported the CO 2 hydrogenation performance of an exceptionally stable MOF-based catalyst, consisting of Pt nanoparticles (NPs) in situ formed in the cavities of UiO-67, herein called "UiO-67-Pt". The first contribution focused on stability issues, 16 while the second focused on catalyst performance and mechanistic studies. 17 A performance comparison was carried out between UiO-67-Pt and Pt/C, Pt/SiO 2 and Pt/Al 2 O 3 catalysts. The study showed that Pt/C and Pt/SiO 2 produced only CO, while Pt/Al 2 O 3 produced mainly CO and a modest amount of methane and methanol (<10% selectivity to each of methane and methanol) at 170°C, 1−8 bar, H 2 /CO 2 = 6. Notably, UiO-67-Pt formed substantial amounts of methanol (up to 18% selectivity), smaller amounts of methane (up to 2% selectivity), and CO as the majority product, under the same conditions. Combining steady state and transient kinetic methods revealed that methanol is formed from CO 2 via formate intermediates at open Zr-sites at the interface between the Pt NP and the Zr-node. The study further showed that methanol is mechanistically separated from the byproducts, methane and CO, and that methane is formed mainly via CO, on this catalyst. 17 In the current study, the focus is set on the dynamic role of the Zr-node in UiO-67-Pt during the CO 2 hydrogenation reaction. We investigate the influence of the amount of defective open Zrsites (i.e., sites not coordinated to linker molecules) on the formation of all three carbon-containing reaction products: methanol, methane, and CO. Moreover, we employ steady state and transient water cofeed experiments, involving isotope labeling and DFT calculations, to gain insight into the role of node-hydration and influence of water in the reaction. The study shows a positive correlation between the number of node defects and the number of surface intermediates leading to methanol and methane formation, while it has a minor influence on CO formation. Furthermore, water cofeed was found to promote desorption of methanol, while it is detrimental to the formation of methane. These findings provide important leads to further catalyst and process design.
To produce a sample with less missing linker defects, a BPDC healing procedure (modified from literature) 19 was performed: 5 g of the UiO-67 sample, predried at 200°C was dispersed in 100 mL DMF at 100°C. BPDC (0.6 g) was added to the solution to replace the BA in UiO-67 (12.5% with respect to BPDC, vide infra) with BPDC. After heating the solution at 100°C overnight, the resulting powder was washed with DMF and acetone as above. This sample is referred to as UiO-67(LD).
Both MOF samples were impregnated with Pt following the procedure reported in ref 16: K 2 PtCl 4 corresponding to a 2:1 BPYDC:Pt molar ratio was added to the MOFs dispersed in DMF at 100°C under stirring and left overnight. After washing in hot DMF and acetone, this leads to the formation of well-defined BPYDC-PtCl 2 moieties (where the BPYDC is in the MOF framework). 20,21 For Pt/ZrO 2 , ZrO 2 particles were prepared by a modified literature procedure. 22  with an XFlash 6|10 energy-dispersive X-ray (EDX) detector was used to estimate the Pt/Zr ratio of the two samples. The Pt/Zr ratio in the two samples were equal within the experimental accuracy (0.042 ± 0.002 and 0.043 ± 0.003 for UiO-67-Pt and UiO-67(LD)-Pt, respectively). Scanning transmission electron microscopy (STEM) images of UiO-67(LD)-Pt after activation and testing was acquired with a FEI Titan G2 60−300 kV microscope.
Most catalytic tests were performed in a fixed bed flow test setup with a stainless-steel reactor (I.D. 7 mm) where the effluent gas is analyzed by an online MS (Pfeiffer) and a GC (TCD-FID). Prior to catalytic testing, the materials were activated at 350°C (5°C min −1 ramp and 4 h isotherm) in flow of 10% H 2 /Ar (40 mL min −1 ). The catalysts (0.2 g) were tested in 1/3/1 and 1/6/3 CO 2 /H 2 /Ar flow (τ = 0.01, g cat min mL −1 ) under 1 and 8 bar pressure, at 170°C. Prehydration, H 2 O cofeed, and 13 CO 2 / 12 CO 2 SSITKA (Steady-State Isotope Transient Kinetic Analysis) experiments were performed and the details are reported in-text.
The high-pressure catalytic tests were performed using a Microactivity Effi unit built by PID Eng & Tech (Micromeritics). The unit is equipped with a high-speed servo-controlled needle valve which allows for precise and stable control of pressure from 1 to 100 bar. A stainless steel flow reactor (6 mm I.D) was used for the tests. The catalysts were activated at 350°C (5°C/min ramp) for 4 h in 10% H 2 in inert (10% Kr in Ar) flow prior to the testing. The catalysts (0.2 g) were tested with 1/ 6/3 CO 2 /H 2 /inert flow ratios (τ = 0.01 and 0.02 g cat min mL −1 for the UiO-67-Pt and Pt/ZrO 2 samples, respectively) aimed at similar CO 2 conversions within 1−30 bar, and 170−240°C. The effluent from the reactor was analyzed with an online GC (Agilent 8890 equipped with one TCD and 2 FIDs, with a methanizer coupled to one of the FIDs to analyze both CO x and oxygenates on one column using one detector).
Computational Details. For the computational study, all chemical species were optimized using DFT calculations with a mixed Gaussian and plane wave method (GPW), 23−25 as implemented in CP2K-6.1 version. 26,27 We used PBE-D3 functional 28,29 with Gaussian basis set DZVP-MOLOPT-SR-GTH. 30,31 A multigrid of size 5 was used to map the Gaussian basis functions, with cutoff energy of 360 Ry for plane wave basis. Energy barriers were calculated using the climbing image nudged elastic band (CI-NEB) method. 32,33 The microkinetic model is built with COPASI. 34 Further details on the calculations are given in the Supporting Information (SI).
Journal of the American Chemical Society pubs.acs.org/JACS Article In our previous study 17 we concluded that the active site for methanol formation are the Zr-nodes of the UiO-67 system. In this work, the reactivity of the Zr-sites active toward the reaction products CH 3 OH and H 2 O, was explored in more detail. To decrease the computational cost of the overall study, we constructed a simple model where the UiO-67 framework optimized from our previous work 17 is stripped to a single zirconium node with 12 benzoate linkers, as shown in Figure 1(a). To maintain the structure of the MOF and better simulate the real configuration of the catalyst, carbon atoms at the end of the linkers were constrained in all directions to prevent the node from deforming and maintaining the integrity of the MOF. One linker was removed from the model in Figure 1(a) to simulate a missing linker defect as shown in Figure 1(b). This system is used to investigate the equilibrium between methanol and water desorption. Two linkers were also removed from the original 12 linkers model system to create either the two adjacent missing linker defects in Figure 1(c) or two opposite missing linker defects in Figure 1(d). The one linker and two linker defect systems were used to model the UiO-67(LD) and the UiO-67 systems, respectively ( Figure 2). This model should sufficiently replicate the qualitative aspects of the catalytic system. Missing linker defects may be capped by OH − /H 2 O molecules. 17,35−37 With the DFT calculated energetics we constructed a micro kinetic model (MKM) that represents all possible chemical reactions for methanol and water adsorption and desorption. To study the role of water in the transient formation of methanol we performed an isotope study by replacing hydrogen with deuterium in all intermediates and built another MKM as shown in SI Figure S13.
■ RESULTS AND DISCUSSION Characterization. XRD and N 2 adsorption of UiO-67 before and after the BPYDC healing procedure, called UiO-67 and UiO-67(LD), respectively, showed that the procedure had no effect on the crystallinity of the MOF, nor any significant effect on the porosity and surface area of the material (SI Figures   S1 and S2). This finding suggests that the structural change of the system, if any, is minor.
In line with previous studies of the material, solution state 1 H NMR analysis identified four organic carboxylate species in both samples; BPDC, BPYDC, benzoic acid (BA), and formic acid (FA), where formic acid originates from decomposition of DMF during synthesis (SI Figure S3). 38 Quantification of the relative amounts of the species, with respect to BPDC showed that the BPYDC amount was comparable in the two samples, and in good agreement with the target amount of synthesis (11 and 10% in UiO-67 and UiO-67(LD), respectively) ( Table 1). The benzoic acid amount was 60% lower in the UiO-67(LD) sample. Thus, successful replacement of a major portion of the benzoic acid in the UiO-67 sample was achieved through the BPDC healing procedure. A minor amount of FA (2%) was observed in both samples.
Both materials show the same TGA-decomposition profile, but the normalized weight predecomposition (T < 500°C) is significantly higher in the BPDC-healed analog UiO-67(LD), evidencing that the number of Zr-sites coordinated to linker or benzoate is higher as compared to the pristine UiO-67 sample.
Defect calculations 39 were performed by combining the results from 1 H NMR and evaluating the normalized weight during TGA at 200°C. They showed that BPDC-healing procedure resulted in an increased BPDC/node ratio (increasing from 4.75 to 5.35) and a decreased BA/node ratio (0.68 to 0.27), while the BPYDC and FA to node ratios were unchanged (Table 2). Thus, the parent MOF UiO-67 has, after synthesis, on average one less linker coordinated to each Zr-node, as compared to the healed analog. 40 This translates into one    In our previous work on the UiO-67-Pt material, species originating from benzoate/linkers, as well as residual DMF solvent, were observed in gas phase during the activation procedure at 350°C in 10% H 2 /Ar. 17 Figure 3 shows the two most intense online MS signals related to benzoate/linker type fragments during activation of UiO-67-Pt and UiO-67(LD)-Pt. The same signal profile is observed for both materials; however, in line with the TGA and 1 H NMR results, a lower amount of benzoate related species is released from the BPDC-healed sample, UiO-67(LD)-Pt.
TEM images of UiO-67(LD)-Pt after activation at 350°C (4 h) followed by testing for CO 2 hydrogenation at 170°C for ∼4.5 h (vide infra) are shown in Figure 4. The size of the Pt NPs is around 4 nm in diameter (3.9 ± 0.6 nm), which is comparable to the nonhealed UiO-67-Pt analog (3.6 ± 0.7 nm, see ref 17). Thus, the two catalysts are comparable both in Pt amount and NP size, but differ in the number of Zr node defects, and are therefore suited for investigating the influence of defects on the CO 2 hydrogenation reaction.
An XPS study was carried out for UiO-67 (with 10% bipy linkers) before and after Pt impregnation, and after subsequent reductive pretreatment as well as catalytic testing (SI Figures  S5−S7). The study showed that Pt is mainly in reduced state, and that Zr(IV) is partly reduced to Zr(III), after reduction and after subsequent testing of UiO-67-Pt. The results are in agreement with previous XAS studies of UiO-67-Pt and with XPS and NAP-XPS studies of Cu/UiO-66 and CuZn/UiO-67. 14−17 CO 2 adsorption isotherms were measured at 25−50°C for pristine UiO-67 and for UiO-67-Pt before and after reduction (SI Figure S8). Pt impregnation and subsequent reduction led to a small reduction in CO 2 uptake per gram material, but did not change the measured interaction strength between CO 2 and the material. The CO 2 adsorption enthalpy was in all cases 18−19 kJ/mol, similar to what previously reported for UiO-67 MOF. 41 Catalytic Investigation. UiO-67-Pt versus Pt/ZrO 2 . Conversion-selectivity plots versus pressure and temperature for UiO-67-Pt and Pt/ZrO 2 , obtained under steady-state conditions, clearly demonstrate the superior methanol production ability of the MOF-based catalyst, with a maximum of 42% (versus 6%) methanol selectivity at 30 bar, 170−190°C, at similar conversion ( Figure 5). This result confirms the unique metal−support interaction created between Pt NPs stabilized by the UiO-67 framework, and the defect (linker-deficient) Zrnodes surrounding it. The methanol selectivity observed for the Pt/ZrO 2 catalyst is similar to what was previously reported, i.e.; 6% methanol selectivity at 200°C, 10 atm. 22 Influence of Missing Linker Defects on the Reaction. The influence of missing linker defects in UiO-67 (UiO-67-Pt versus UiO-67(LD)-Pt) on catalytic performance was evaluated in a "reaction-onset" experiment by the following procedure: First, the materials were activated in a reducing flow of 10% H 2 in Ar (40 mL min −1 , m cat = 0.2 g, 1 bar) ramping to 350°C followed by a 4 h isotherm before cooling to 170°C in Ar flow. Second, the reaction feed of CO 2 /H 2 /Ar(10Kr) = 1/3/1, τ = 0.01 g cat min mL −1 was introduced to the reactor and the reactor pressure was subsequently increased to 8 bar. The results are presented in Figure 6, where the formation rates of CO, CH 4 , and CH 3 OH are shown in the left-hand figure, and the CH 3 OH selectivity is shown to the right.
Both catalysts show the same trends with time on stream: the rate of methanol formation increases rapidly during the first hour of reaction, then decreases comparatively fast and reaches a steady state after approximately 3 h on stream. At peak methanol formation, the rate is approximately 6 times higher than at steady state. The formation rates of CO and CH 4 both decrease with  Journal of the American Chemical Society pubs.acs.org/JACS Article time on stream until steady state is reached after about 1.5 h. The relative temporal change is significantly larger for the small amounts of CH 4 formed, as compared to the majority product CO. Under the given conditions, the CH 4 selectivity was <1%. In a second experiment for UiO-67-Pt, where the tested sample was reactivated and retested, an identical transient behavior was observed (SI Figure S9), suggesting that the transient regime with decreasing activity is caused by reversible catalyst changes. The transient regime of the CO 2 hydrogenation reaction is addressed further in the next section.
Comparing the absolute values of the reaction rates over the two catalyst samples, it is evident that the CO formation rates are comparable, while the rate of methanol formation is approximately 60% lower (at steady state) over the less defective UiO-67(LD)-Pt sample ( Figure 6). This corresponds to methanol selectivity of ∼7% and ∼13%, respectively. A 60% decrease was also observed in the methane formation rate, between the UiO-67 and UiO-67(LD) samples. To assess the reproducibility of the measurements, another identical test of UiO-67(LD)-Pt was performed. In that case, the same trend was observed and the methanol formation rate was somewhat higher,    Figure 7). 17 It further suggests that methane is also formed at the interface of the Zrnode and the Pt NP. Conversely, the similar CO formation rates observed over the two materials suggest that the rate-limiting step of CO formation is catalyzed by the Pt NP surface, without an influence of the Pt NP−Zr node interface.
To verify that the origin of the lower methanol and methane formation rates is the number of intermediates, we turned to 13 CO 2 SSITKA measurements. Due to limitations in the transient experimental setup, the measurements were performed under ambient pressure. Moreover, the reaction was performed in D 2 instead of H 2 to increase the methanol production (caused by the strong inverse kinetic isotope effect) 17,42 and to allow for monitoring of both methanol and methane during the isotope transient. At steady state conditions (CO 2 /D 2 /inert = 1/6/3, τ = 0.01 g cat min mL −1 , T = 170°C, 1 bar), the rates of CO, methane, and methanol formation were approximately 10%, 60%, and 50% lower, respectively, over UiO-67(LD)-Pt than over UiO-67-Pt (Figure 8, left), comparable to the differences observed in experiments under 8 bar pressure. The transient evolution of 13 CO, 13 CD 4 and 13 CD 3 OD after switching from a feed of 13 CO 2 +D 2 to 12 CO 2 +D 2 at time = 0, is shown in Figure 8 (right). The transient evolution of the normalized intensity of the 13 C products formed over UiO-67(LD)-Pt overlap those of UiO-67-Pt, previously reported in ref 17, evidencing that the reaction proceeds through the same mechanism, with the same intrinsic kinetics, while the number of active sites is different.
The mean surface residence time τ res and the number of surface intermediates N ad leading to formation of the three products, listed in Table 3, are parameters where no underlying assumptions about the kinetic model is required. 43,44 In agreement with the overlapping isotope transients and the lower steady state methanol formation rate over UiO-67(LD)-Pt (50% of the rate over UiO-67-Pt), the number of intermediates leading to methanol formation on UiO-67(LD)-Pt is 40% of the number of intermediates on the defective analog. That is, N ad , UiO-67(LD)-Pt /N ad , UiO-67-Pt = 0.4. A similar observation is made for methane formation, where N ad , UiO-67(LD)-Pt /N ad , UiO-67-Pt = 0.3. These data confirm the importance of Zr-node defects for methane formation. N ad for CO is, however, somewhat lower than expected for the defective analog, since similar reaction rates were observed over the two materials at 8 bar pressure, and only 10% lower CO formation rate was observed here. However, considering the error margins of the experiments and the data treatment, the agreement is reasonable.
As a final observation from the data presented in Figure 8  Influence of Zr-Node Hydration on the Reaction. In the comparison of UiO-67-Pt and UiO-67(LD)-Pt, after the onset of reaction at 8 bar pressure, a transient regime lasting approximately 2 h was observed for the formation of all three carbon-containing reaction products (see Figure 6). In this section, the origin of this transient regime is investigated for UiO-67-Pt.   Figure 9 shows an FT−IR spectrum of the Zr-μ 3 −OH region of the sample during activation. The full FT−IR spectrum and its features are described in detail elsewhere. 17,45,47,48 The intense peak of Zr-μ 3 −OH at 3669 cm −1 decreases with increased temperature, and even before 350°C is reached, the signal is completely absent. Notably, the dehydration causes a reordering of the Zr-node from Zr 6 O 8 (i.e., Zr 6 O 4 (OH) 4 ), where Zr is 8coordinated, to a distorted Zr 6 O 6 analog where Zr is 7coordinated. 45,46 The reordering is reversible and does not induce overall changes to the framework structure, nor to the connecting carboxylates. 45 When the temperature is decreased to 245°C, and a reaction feed of 1/6 CO 2 /H 2 is introduced to the IR-cell, the signal of Zr-μ 3 −OH increases as H 2 O is produced in the reaction, and reaches a plateau in less than 5 min (Figure 9). At 170°C, under steady state reaction conditions, the signal of Zr-μ 3 −OH is larger, compared to 245°C. Under these conditions, the Zr-μ 3 −OH groups are dynamic and H readily exchanges for D during H/D exchange experiments, either by direct H-spillover or via reaction products. 17 Considering the reaction-onset experiment at 8 bar, we notice that no signal of H 2 O was detected in the GC until ∼1 h on stream. Furthermore, the appearance of gas phase H 2 O coincided with a substantial drop in the methanol formation rate (Figure 10, left). Interestingly, the molar amount of H 2 O formed until it appeared in the GC (calculated from reaction stoichiometry), corresponds to about 40% of the estimated number of Zr-μ 3 −OH groups in the MOF. This observation indicates a correlation between the transient regime with higher methanol formation rate and the Zr-nodes' state of hydration and/or the presence of H 2 O.
To further investigate the influence of the state of hydration of the Zr-nodes, a reaction-onset experiment was performed starting from a prehydrated catalyst. After the activation procedure, the MOF was exposed to a flow of wet Ar (saturated with H 2 O vapor at room temperature) at 170°C prior to the switch to reaction feed and subsequent pressure increase. The product formation rates with time on stream over the initially dehydrated and prehydrated catalysts are shown in Figure 10 (right). The transient regime is very different in the two measurements. Over the prehydrated catalyst, the methanol peak is gone, and the methanol formation rate instead gradually increases toward steady state, reaching the same value as over the initially dehydrated sample. For methane, the rate of formation starts, and is maintained at the steady state value, which is the same for the dehydrated and prehydrated catalyst.  This observation adds further evidence to the importance of Zrnode defects in CH 4 formation. No evident change in CO formation is observed. The prehydration results clearly demonstrate that hydration of the Zr-node is of importance, however, this experiment alone cannot distinguish whether it is due to an intrinsic activity difference between the dehydrated and hydrated Zr-node, or due to competitive adsorption between methanol (and methane) and H 2 O. The influence of H 2 O on the reaction is addressed further in the following section.
Influence of H 2 O on the Reaction with Hydrated Nodes. The influence of H 2 O on the reaction was investigated through cofeed experiments at 170°C and ambient pressure (CO 2 /H 2 /inert = 1/6/3, τ = 0.01 g cat min mL −1 ). To enable monitoring of transient as well as steady state effects, the reaction feed was switched between feeds of CO 2 + H 2 and CO 2 + H 2 + xH 2 O (x = 0.6, 1.2, 1.7, and 2 vol %). Figure 11 (left) shows the product formation rates when switching from dry to 1.7% H 2 O reaction feed. All three carbon-containing products are affected by the presence of H 2 O in the reaction feed. The rates of CO and CH 4 formation decrease to a new steady state within the time resolution of the GC measurements (∼16 min), while methanol first increases by more than an order of magnitude then decreases and reaches steady state after ∼30 min.
The influence of pH 2 O on the reaction rates at steady state is shown in Figure 11 (right). An increasing H 2 O pressure has a substantial inhibiting effect on the CH 4 formation rate (−0.4 order), and only minor effect on CO formation rate (−0.1 order). In a previous contribution, we reported that all product formation rates decreased with increasing contact time due to an inhibiting effect of CO and/or H 2 O. 17 Reaction orders in p(CO + H 2 O) of −1.1, −0.7, and −1.0, for CO, CH 4 , and CH 3 OH formation were observed. Thus, the reaction orders observed here in pH 2 O suggest that for CO, self-inhibition mainly causes the negative effect of contact time on the CO formation rate, while both majority products (CO and H 2 O) inhibit CH 4 formation, and only CO inhibits CH 3 OH formation. Figure 11. Left: Rate of CO (squares), CH 4 (circles), and CH 3 OH (triangles) formation during a switch from CO 2 + H 2 to CO 2 + H 2 + xH 2 O (x = 1.7 vol %) at time = 0. Right: Influence of pH 2 O on the steady state formation rates of CO, methanol and methane. pH 2 O is estimated as the sum of the cofed pH 2 O and half of the pH 2 O produced in the reaction at steady state (calculated from reaction stoichiometry). The in-plot numbers are the respective reaction orders. Units in the right-hand plot represent the variable X in "log(X)". Conditions: CO 2 /H 2 /inert = 1/6/3 with 0 (yielding an average 0.08), 0.6, 1.2, 1.7, or 2 vol % H 2 O, τ = 0.01 g cat min mL −1 , T = 170°C, 1 bar. Figure 12. Transient evolution of the normalized methanol formation rate when switching from dry to wet reaction feed, in CO 2 + H 2 (left) and CO 2 + D 2 (right). H 2 O vol % in feed = 0.6 (blue), 1.2 (pink), 1.7 (orange), and 2 (gray). The inset shows the rate of methanol formation when switching from wet (1.7% H 2 O) to dry feed. The black trace is a moving average. Conditions: 1/6/3 CO 2 /H 2 (D 2 )/Ar ambient pressure, T = 170°C, τ = 0.01 g cat min mL −1 .
Journal of the American Chemical Society pubs.acs.org/JACS Article Although a large transient influence of the introduction of H 2 O was observed for methanol formation, the steady state value is unchanged (zero order). However, as seen in Figure 11 (right), the rate of methanol formation at pH 2 O = 0.006 (log(pH 2 O) = −2.2) is somewhat lower than the rate under "dry conditions" (i.e., no added H 2 O, average log(pH 2 O) = −3.1), and when the pH 2 O increases further, the rate of methanol formation increases slightly (relative to pH 2 O = 0.006). When only considering the methanol formation rate under wet conditions in the analysis, the reaction order in pH 2 O is estimated to 0.25. If the orders are in fact different at low and high pH 2 O, then it may suggest that the reaction proceeds via different pathways or is limited by different elementary steps in the two regimes of pH 2 O. To assess the possibility of different reaction pathways/rate-limiting steps further, the influence of H 2 O should be investigated at pH 2 O values closer to those obtained under the "dry" conditions, as well as in the intermediate range. These pH 2 O values are however outside the experimentally achievable range of our test-setup and hence outside the scope of this study.
Having assessed the influence of H 2 O at steady state, we turn to the transient influence. Figure 12 (left) shows the intensity of methanol (m/z = 31), normalized to the dry steady state reaction rate, when switching from the dry feed to wet feeds containing different pH 2 O. The peak size increases significantly with increasing pH 2 O in the wet feed, and integration of the peaks yields an approximate 0.5 order dependence in pH 2 O for methanol formed during the transient. Interestingly, when switching back from wet to dry conditions, the methanol formation rate instead decreases rapidly, and then slowly increases to the dry steady state value. The normalized intensity of methanol during the switch from 1.7% to 0% H 2 O in the feed is shown in the inset in Figure 12. Changing from wet to dry conditions, the approach to steady state is somewhat slower, as compared to from dry to wet, but the magnitude of the transient change increases with pH 2 O in both cases, i.e., the gas phase methanol concentration decreases with increasing pH 2 O. The highly similar, but inverse, behavior of methanol during switches from dry versus wet reaction conditions indicates that the two transients are caused by reversible adsorption/desorption phenomena. Prior studies of other materials showed that methanol may adsorb and form a methoxy group. Water may subsequently react with the methoxy group to reform gas-phase methanol. 49−53 Such interactions could explain the transient changes in methanol. However, under identical conditions, no methoxy groups were observed during operando FT−IR of UiO-67-Pt. 17 However, Larmier et al. observed methoxy groups on Cu/ZrO 2 by in situ DRIFTS when exposed to CO 2 and H 2 (1:3) under 5 bar pressure and 230°C (closed system), and by ex situ solid-state NMR after exposure for 12 h. 10 To get further insights into the mechanism of transient methanol formation, identical experiments were performed using D 2 instead of H 2 , i.e., switching from CO 2 + D 2 to CO 2 + D 2 + xH 2 O. By this approach, it is possible to identify the source of hydrogen in the desorbed methanol. At steady state, the influence of pH 2 O on the reaction rates in D 2 (Figure 12, right) is unchanged for CO (−0.1) and slightly less negative for methane (−0.3), as compared to H 2 . For methanol a negative 0.2 order in pH 2 O is observed, and the slope (SI Figure S11) is linear in the whole pH 2 O range, including dry conditions. Considering the high complexity of the role of H 2 O and its influence on the reaction, the origin of this isotope effect is likely manifold. Turning next to the transient regime, Figure 12 (right) shows the intensity of methanol (m/z = 34), normalized to the dry steady state reaction rate, when switching from the dry feed to wet feeds of different pH 2 O. The same trend is observed in D 2 as in H 2 ; the peak size of methanol desorption and adsorption increases with pH 2 O. Considering the source of hydrogen, interestingly, the desorbed methanol does not contain significant amounts of H from H 2 O. This suggests that methanol desorption via protonation of OCD 3 by H 2 O is not the main pathway.
The amount of methanol produced during the transient (in D 2 ) is approximately 18, 25, and 33 μmol g cat −1 for pH 2 O = 0.006, 0.012, and 0.017, respectively. These amounts are comparable to the number of intermediates (23 μmol g cat −1 ) leading to methanol formation determined from 13 C-SSITKA under identical, dry, conditions (see Figure 8 and Table 3).
To further understand the role of water in methanol desorption, the free energy pathways for the adsorption of water and methanol to a hydrated Zr-node with one missing linker were calculated at 170°C (Figure 13 and SI Table S3). Starting from the missing linker structure (1), which involves two Zr-vacant sites and two μ-O bridges, coordination of water and methanol followed by proton transfer reactions generate the 11 intermediates shown in Figure 13. These intermediates have been labeled by using numbers, to indicate species with different substituents at Zr, and superscript H and/or Me to indicate whether the origin of the substituent is water and/or methanol, respectively. The calculated energy barriers connecting these intermediates are in all cases very low (<25 kJ/mol for proton transfer reactions and 0 kJ/mol for adsorption of methanol and water in Zr-vacant sites). Therefore, the pathway is mainly dictated by thermodynamics. In the presence of MeOH, the formation of the most stable intermediate  54 2 MeH is therefore predicted to be the most abundant species at equilibrium, even though all intermediates are accessible at the reaction conditions. The preference for 2 MeH was also confirmed using a microkinetic model (MKM) constructed with all possible pathways shown in Figure 13. The MKM showed that, at equal or larger concentrations of water compared to methanol (as expected for a CO 2 hydrogenation reaction yielding CO as the main product), the concentration of species containing methoxy groups (3 Me and 5 MeMe ) were very low (∼0 mol/L), which is consistent with them not being observed under experimental conditions. Using 1 M of 1, H 2 O and MeOH, 0.98 M of 2 MeH is observed; while using 1 M of 1 and water, and 0.03 of MeOH, the species observed are 2 MeH (0.03 M), 2 HH (0.5 M), 3 H (0.034 M), and 1 (0.5 M). The latter result suggests that 3 H is never a main species but 2 HH or 1, which may be relevant in alcohol dehydration processes. 38,55 As discussed above (Figure 12), cofeed experiments shows that adding water into the system increases the observed methanol concentration initially. To gain further insight into this experimental observation, we set up a MKM where the equilibrated structure 2 MeH at 1 mol/L concentration was used as a starting point and then different amounts of water is introduced to the system (see SI Figure S12). These simulations show that when any additional water was introduced into the Journal of the American Chemical Society pubs.acs.org/JACS Article system it causes methanol to desorb from the system, in agreement with the experimental observations. The adsorbed methanol is desorbed from the Zr-site and is replaced by a water molecule, resulting in structure 2 HH in Figure 13. The equilibria 2 MeH ↔ 3 H ↔ 2 HH is in agreement with the nonobservation of CD 3 OH in the experiments performed with CO 2 and D 2 followed by addition of H 2 O (see Figure 7, in which the orange H could be D). However, the equilibria between 2 MeH and 3 Me , which is thermodynamically preferred, could also play a role in the reaction leading to H/D-exchange. To determine the relevance of this process, DFT calculations were performed considering deuterated species and different proton-transfer mechanisms (Figures 14 and S13). All mechanisms proceed without any additional energy barriers beyond thermodynamics. Figure 14 shows that the relative energy of 3 H compared to  Table S4). Nevertheless, these energy differences are created because of the isotope exchange, and will not exist in a normal experiment using H 2 , in which the proton in desorbed methanol may originate from either water already present or newly added. An interesting result from the energies shown in Figure 13 is that the adsorption of methanol in 1 (ΔG = −7.2 kJ/mol) is less favorable than in 3 H (ΔG = −50.4 kJ/mol) by 43.2 kJ/mol. Clearly, methanol is more strongly adsorbed to a hydrated node than to a dehydrated node, which could partially account for the larger methanol formation rate at the reaction-onset (due to more rapid liberation of the defective Zr site for another reaction cycle) (see Figure 10). A similar result has already been reported for water in defective UiO-66 type MOFs. 56,57 Structural and electronic analysis of 1, 4 Me , 3 H , and 2 MeH suggest that the reason for the larger adsorption energies for MeOH in 3 H is the formation of an H-bond between MeOH and the terminal OH (see SI). We also wanted to evaluate the influence of having two missing linkers in the methanol and water adsorption (see Table  S5). With this goal, we built two model systems, in which two missing linkers in adjacent (3 H -adj) and opposite (3 H -opp) positions were replaced by −OH groups (see Figure 1), and calculated the methanol adsorption in each model. The free energy for the first and second methanol adsorption with 3 H -adj are 3.2 and 66.9 kJ/mol; while with 3 H -opp, they are −39.3 and −35.6 kJ/mol, respectively. These energies show that methanol binds stronger on a node with a single missing linker (3 H , ΔG = −50.4 kJ/mol) than on nodes with an additional, adjacent, or opposite, missing linker defect. In the case of adjacent linkers, the adsorption energies change drastically, especially in the case where water is coordinated to one Zr-atom attached to an OH group (ΔG = +66.9 kJ/mol). This result strongly suggests that having a larger number of defects not only increases the number of active sites to produce methanol but also facilitates methanol desorption.
These results show that both water and missing linkers play an important role in methanol desorption by either displacing the equilibria or changing the methanol adsorption energies. However, Figure 10 suggests that water does not have an important influence on the MeOH formation rate at steady state. Instead, it decreases the rate of methane significantly. An explanation to this observation is the following: As represented in Figure 15, interaction of adsorbed CO with a Zr atom from a node should be feasible at the interface between Pt NPs and Zr nodes. This coordination would increase the electophilicity of C and favor the hydride transfer, which has been proposed to be the rate-limiting step for the CO hydrogenation to methane with Pt-NPs. 58 When adding water to the system, the equilibria between CO and water will be displaced favoring water coordination and disfavoring methane formation. In the case of methanol (see Figure 7), this competition takes place before the formation of formate, which is thermodynamically preferred of having 2 HH . Therefore, it would not influence the rate-limiting step of methanol, which has been proposed to be the hydrogenation of formate.

■ CONCLUSIONS
The dynamic role of the Zr-node during CO 2 hydrogenation over UiO-67-Pt and the influence of defects and water on the reaction have been investigated by steady state and isotope transient kinetic studies, as well as water cofeed experiments.
A UiO-67-Pt MOF catalyst was designed with fewer defects to influence the rate of methanol formation. 13 C-SSITKA experiments verified that a lower number of defect sites led to lower methanol formation rates, and that this decrease was caused by a lower number of surface intermediates. This result serves as a proof-of-principle in rational design of a MOF catalyst based on fundamental understanding. Importantly, the methane formation rate had a similar dependency of Zr node defects, while the CO formation rate was almost invariant with defect density. These results strongly suggest that the rate-limiting step of CO formation occurs at the Pt NPs, while the rate-limiting step of methane formation, like methanol, takes place at the Pt NP−Zr node interface.
By comparing the onset of reaction over a sample with dehydrated Zr-nodes to the onset over a prehydrated sample, it was found that the rate of methanol and methane formation are both higher over a dehydrated node than over a hydrated node. Adding surplus water to the feed has an inhibiting effect on