# The Impact of Oxygen Surface Coverage and Carbidic Carbon on the Activity and Selectivity of Two-Dimensional Molybdenum Carbide (2D-Mo2C) in Fischer-Tropsch Synthesis

Evgenia Kountoupi, Alan J Barrios, Zixuan Chen, C. R. Muller, Vitaly Ordomsky, Aleix Comas-Vives, A. Fedorov

► To cite this version:

Evgenia Kountoupi, Alan J Barrios, Zixuan Chen, C. R. Muller, Vitaly Ordomsky, et al.. The Impact of Oxygen Surface Coverage and Carbidic Carbon on the Activity and Selectivity of Two-Dimensional Molybdenum Carbide (2D-Mo2C) in Fischer-Tropsch Synthesis. ACS Catalysis, 2024, ACS Catalysis, 14, 10.1021/acscatal.3c03956. [https://doi.org/10.1021/acscatal.3c03956](https://doi.org/10.1021/acscatal.3c03956)

HAL Id: hal-04601549

https://hal.univ-lille.fr/hal-04601549

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# The Impact of Oxygen Surface Coverage and Carbidic Carbon on the Activity and Selectivity of Two-Dimensional Molybdenum Carbide (2D-Mo2C) in Fischer-Tropsch Synthesis

Evgenia Kountoupi, Alan J Barrios, Zixuan Chen, C. R. Muller, Vitaly Ordomsky, Aleix Comas-Vives, A. Fedorov

► To cite this version:

Evgenia Kountoupi, Alan J Barrios, Zixuan Chen, C. R. Muller, Vitaly Ordomsky, et al.. The Impact of Oxygen Surface Coverage and Carbidic Carbon on the Activity and Selectivity of Two-Dimensional Molybdenum Carbide (2D-Mo2C) in Fischer-Tropsch Synthesis. ACS Catalysis, 2024, ACS Catalysis, 14, 10.1021/acscatal.3c03956. [https://doi.org/10.1021/acscatal.3c03956](https://doi.org/10.1021/acscatal.3c03956)

HAL Id: hal-04601549

https://lilloa.hal.science/hal-04601549v1

Submitted on 19 Jun 2024

**HAL** is a multi-disciplinary open access
archive for the deposit and dissemination of sci-
entific research documents, whether they are pub-
lished or not. The documents may come from
teaching and research institutions in France or
abroad, or from public or private research centers.

L'archive ouverte pluridisciplinaire HAL, est
destinée au dépôt et à la diffusion de documents
scientifiques de niveau recherche, publiés ou non,
émanant des établissements d'enseignement et de
recherche français ou étrangers, des laboratoires
publics ou privés.

<figure><img src="image_1.png" /></figure>

Distributed under a Creative Commons Attribution 4.0 International License
# The Impact of Oxygen Surface Coverage and Carbidic Carbon on the Activity and Selectivity of Two-Dimensional Molybdenum Carbide (2D-Mo₂C) in Fischer–Tropsch Synthesis

Evgenia Kountoupi, Alan J. Barrios, Zixuan Chen, Christoph R. Müller, Vitaly V. Ordomsky,*
Alex Comas-Vives,* and Alexey Fedorov*

<figure><img src="image_2.png" /></figure>

Cite This: ACS Catal. 2024, 14, 1834–1845

<figure><img src="image_3.png" /></figure>

Read Online

## ACCESS

<figure><img src="image_4.png" /></figure>

Metrics & More

<figure><img src="image_5.png" /></figure>

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Supporting Information

**ABSTRACT:** Transformations of oxygenates (CO₂, CO, H₂O, etc.) via Mo₂C-based catalysts are facilitated by the high oxophilicity of the material; however, this can lead to the formation of oxycarbides and complicate the identification of the (most) active catalyst state and active sites. In this context, the two-dimensional (2D) MXene molybdenum carbide Mo₂CTₓ (Tₓ are passivating surface groups) contains only surface Mo sites and is therefore a highly suitable model catalyst for structure–activity studies. Here, we report that the catalytic activity of Mo₂CTₓ in Fischer–Tropsch (FT) synthesis increases with a decreasing coverage of surface passivating groups (mostly O*). The *in situ*

removal of Tₓ species and its consequence on CO conversion is highlighted by the observation of a very pronounced activation of Mo₂CTₓ (pretreated in H₂ at 400 °C) under FT conditions. This activation process is ascribed to the *in situ* reductive defunctionalization of Tₓ groups reaching a catalyst state that is close to 2D-Mo₂C (i.e., a material containing no passivating surface groups). Under steady-state FT conditions, 2D-Mo₂C yields higher hydrocarbons (C₅⁺ alkanes) with 55% selectivity. Alkanes up to the kerosine range form, with value of α = 0.87, which is ca. twice higher than the α value reported for 3D-Mo₂C catalysts. The steady-state productivity of 2D-Mo₂C to C₅⁺ hydrocarbons is ca. 2 orders of magnitude higher relative to a reference β-Mo₂C catalyst that shows no *in situ* activation under identical FT conditions. The passivating Tₓ groups of Mo₂CTₓ can be reductively defunctionalized also by using a higher H₂ pretreatment temperature of 500 °C. Yet, this approach leads to a removal of carbidic carbon (as methane), resulting in a 2D-Mo₂C₁⁻ₓ catalyst that converts CO to CH₄ with 61% selectivity in preference to C₅⁺ hydrocarbons that are formed with only 2% selectivity. Density functional theory (DFT) results attribute the observed selectivity of 2D-Mo₂C to C₅⁺ alkanes to a higher energy barrier for the hydrogenation of surface alkyl species relative to the energy barriers for C–C coupling. The removal of O* is the rate-determining step in the FT reaction over 2D-Mo₂C, and O* is favorably removed in the form of CO₂ relative to H₂O, consistent with the observation of a high CO₂ selectivity (ca. 50%). The absence of other carbon oxygenates is explained by the energetic favoring of the direct over the hydrogen-assisted dissociative adsorption of CO.

**KEYWORDS:** carbide catalysts, defunctionalization of MXenes, Fischer–Tropsch synthesis, two-dimensional (2D) materials, oxygen coverage, molybdenum carbide, DFT calculations

<figure><img src="image_7.png" /></figure>

## INTRODUCTION

The Fischer–Tropsch (FT) process has been utilized for nearly a century to hydrogenate carbon monoxide, typically derived from feedstocks such as coal, natural gas, and more recently, biomass, into chemicals and fuels.¹,² This exothermic reaction proceeds according to eq 1.³

$$ (2n + 1)H_2 + nCO \rightarrow C_nH_{(2n+2)} + nH_2O, \\ \Delta H^{0}_{298K} = -165 \text{ kJ mol}_{\text{CO}}^{-1} \quad (1) $$

Product selectivity can be tuned through the choice of catalyst, and it varies between n-alkanes, olefins, and oxygenates (typically, alcohols).⁴ The industrial FT catalysts

are usually based on transition metals such as Fe and Co.⁵⁻⁹ In the past decades, the development of alternative FT catalysts aimed at tailoring the chain-length distribution of the products, for instance, by narrowing the broad Anderson–Schulz–Flory distribution to the desired fuel range (C₁₀–C₂₀ hydrocarbons for diesel fuel).¹⁰,¹¹ In this context, early transition metal

Received: August 22, 2023

Revised: December 20, 2023

Accepted: January 3, 2024

Published: January 19, 2024

<figure><img src="image_8.png" /></figure>
# The Impact of Oxygen Surface Coverage and Carbidic Carbon on the Activity and Selectivity of Two-Dimensional Molybdenum Carbide (2D-Mo₂C) in Fischer–Tropsch Synthesis

Evgenia Kountoupi, Alan J. Barrios, Zixuan Chen, Christoph R. Müller, Vitaly V. Ordomsky,*
Alex Comas-Vives,* and Alexey Fedorov*

<figure><img src="image_2.png" /></figure>

Cite This: ACS Catal. 2024, 14, 1834–1845

<figure><img src="image_3.png" /></figure>

Read Online

## ACCESS

<figure><img src="image_4.png" /></figure>

Metrics & More

<figure><img src="image_5.png" /></figure>

Article Recommendations

<figure><img src="image_6.png" /></figure>

Supporting Information

**ABSTRACT:** Transformations of oxygenates (CO₂, CO, H₂O, etc.) via Mo₂C-based catalysts are facilitated by the high oxophilicity of the material; however, this can lead to the formation of oxycarbides and complicate the identification of the (most) active catalyst state and active sites. In this context, the two-dimensional (2D) MXene molybdenum carbide Mo₂CTₓ (Tₓ are passivating surface groups) contains only surface Mo sites and is therefore a highly suitable model catalyst for structure–activity studies. Here, we report that the catalytic activity of Mo₂CTₓ in Fischer–Tropsch (FT) synthesis increases with a decreasing coverage of surface passivating groups (mostly O*). The *in situ* removal of Tₓ species and its consequence on CO conversion is highlighted by the observation of a very pronounced activation of Mo₂CTₓ (pretreated in H₂ at 400 °C) under FT conditions. This activation process is ascribed to the *in situ* reductive defunctionalization of Tₓ groups reaching a catalyst state that is close to 2D-Mo₂C (i.e., a material containing no passivating surface groups). Under steady-state FT conditions, 2D-Mo₂C yields higher hydrocarbons (C₅⁺ alkanes) with 55% selectivity. Alkanes up to the kerosine range form, with value of α = 0.87, which is ca. twice higher than the α value reported for 3D-Mo₂C catalysts. The steady-state productivity of 2D-Mo₂C to C₅⁺ hydrocarbons is ca. 2 orders of magnitude higher relative to a reference β-Mo₂C catalyst that shows no *in situ* activation under identical FT conditions. The passivating Tₓ groups of Mo₂CTₓ can be reductively defunctionalized also by using a higher H₂ pretreatment temperature of 500 °C. Yet, this approach leads to a removal of carbidic carbon (as methane), resulting in a 2D-Mo₂C₁⁻ₓ catalyst that converts CO to CH₄ with 61% selectivity in preference to C₅⁺ hydrocarbons that are formed with only 2% selectivity. Density functional theory (DFT) results attribute the observed selectivity of 2D-Mo₂C to C₅⁺ alkanes to a higher energy barrier for the hydrogenation of surface alkyl species relative to the energy barriers for C–C coupling. The removal of O* is the rate-determining step in the FT reaction over 2D-Mo₂C, and O* is favorably removed in the form of CO₂ relative to H₂O, consistent with the observation of a high CO₂ selectivity (ca. 50%). The absence of other carbon oxygenates is explained by the energetic favoring of the direct over the hydrogen-assisted dissociative adsorption of CO.

**KEYWORDS:** carbide catalysts, defunctionalization of MXenes, Fischer–Tropsch synthesis, two-dimensional (2D) materials, oxygen coverage, molybdenum carbide, DFT calculations

<figure><img src="image_7.png" /></figure>

## INTRODUCTION

The Fischer–Tropsch (FT) process has been utilized for nearly a century to hydrogenate carbon monoxide, typically derived from feedstocks such as coal, natural gas, and more recently, biomass, into chemicals and fuels.¹,² This exothermic reaction proceeds according to eq 1.³

$$ (2n + 1)H_2 + nCO \rightarrow C_nH_{(2n+2)} + nH_2O, \\ \Delta H^{0}_{298K} = -165 \text{ kJ mol}_{\text{CO}}^{-1} \quad (1) $$

Product selectivity can be tuned through the choice of catalyst, and it varies between n-alkanes, olefins, and oxygenates (typically, alcohols).⁴ The industrial FT catalysts

are usually based on transition metals such as Fe and Co.⁵⁻⁹ In the past decades, the development of alternative FT catalysts aimed at tailoring the chain-length distribution of the products, for instance, by narrowing the broad Anderson–Schulz–Flory distribution to the desired fuel range (C₁₀–C₂₀ hydrocarbons for diesel fuel).¹⁰,¹¹ In this context, early transition metal

Received: August 22, 2023

Revised: December 20, 2023

Accepted: January 3, 2024

Published: January 19, 2024

<figure><img src="image_8.png" /></figure>
carbides (TMCs), in particular Mo carbides, have been explored as FT catalysts.¹² Unsupported Mo carbides (cubic α-MoC₁-x and orthorhombic β-Mo₂C phases) yield mainly methane, CO₂, lower alkanes, and alkenes as FT products, with a chain probability growth coefficient (α) equal to 0.3–0.4.¹³⁻¹⁵ Using Mo₂C, the formation of alcohols has been reported as well¹⁶ and approaches to increase the selectivity of Mo carbides to C₂⁺ alcohols include their promotion with alkali metals such as potassium,¹⁷ or dispersing Mo carbide on a support (e.g., Al₂O₃, TiO₂).¹⁸⁻²⁰

Turning to the catalytic pathways of the FT process, the main mechanisms proposed are the carbide mechanism, the CO insertion mechanism, and the hydroxycarbene mechanism, each involving initiation, propagation, and chain termination steps.² Briefly, the carbide mechanism, proposed by Fischer and Tropsch,²¹ proceeds via the dissociative adsorption of CO to C* and O* that occurs simultaneously with the dissociation of H₂ to H* species and the subsequent hydrogenation of C* to CHₓ* (x = 1–3) species; the latter are involved in chain growth (the C–C coupling step).²² The dissociation of CO* may occur directly or may be hydrogen-assisted (molecular or H*).²³ The chain growth step can involve methylene (CH₂*),²⁴ methylidyne (CH*),²⁵⁻²⁸ or coupling between C* and CH* species.²⁹ In the CO insertion mechanism, CO inserts into an M–H bond (initiation) followed by the hydrogenation of the formyl (HCO*) species into CH₂O* species that are hydrogenated to CH₃* species and H₂O; further CO insertion into a metal–alkyl bond and hydrogenation is repeated until chain growth is terminated.³⁰ In contrast, the hydroxycarbene mechanism is linked to the formation of oxygenates and it includes a coupling reaction between two hydroxycarbene (RCOH*, R = H, alkyl) intermediates formed via the hydrogenation of adsorbed CO.³¹

All three main FT mechanisms have been proposed to proceed on Mo₂C. In particular, it has been suggested that Mo₂C catalyzes FT via a direct dissociation of CO into O* and C* species, i.e., a carbidic mechanism.³² Specifically, CO adsorption and H₂ temperature-programmed experiments have been used to confirm the direct dissociation of CO on a Mo₂C surface.¹⁴ However, the O* adsorbates formed can inhibit a further dissociation of CO and thereby deactivate the catalyst.³³ The involvement of an H-assisted pathway for the dissociation of CO has been suggested as well, in particular as a means to avoid the formation of a too-strongly bound O* species that reduce the catalytic turnover.³⁴ Moreover, a computational study suggested a CO insertion mechanism with a coupling between the CHₓ and CH₃O species to proceed on Mo₂C.³⁵ Lastly, the hydroxycarbene mechanism has been suggested for Mo₂C to account for the formation of alcohols.¹⁴

Oxycarbidic Mo₂CₓOᵧ species/phases can form *in situ* from Mo₂C via its reaction with oxygenates, and they have been proposed to be the catalytically activity centers for the dry reforming of methane (DRM) or hydrodeoxygenation reactions.³⁶,³⁷ Depending on the chemical potential of the gas phase, Mo-terminated surfaces of Mo₂C can feature different coverages of O* adsorbates that can block adsorption sites and modify adsorption energies of reaction intermediates, which in turn influences the overall catalytic activity and product selectivity.³⁸,³⁹ While it is generally believed that higher O* coverages are associated with a lower FT activity,³²,⁴⁰ it is yet unclear if there is an optimum (low) O* coverage to yield the highest FT activity on Mo₂C;

furthermore, the dependence of product selectivity on O* coverage of Mo₂C is also understudied.

One strategy to improve our understanding of the catalytic activity of Mo₂C relies on the use of model catalysts with well-defined structures and surfaces, which facilitates their spectroscopic characterization and bridges the gap to computational models.⁴¹⁻⁴⁴ In this context, well-defined two-dimensional (2D) carbides of the MXene family,⁴⁵⁻⁴⁸ in particular Mo₂CTₓ (Tₓ are O, OH, and F surface termination groups), can serve as model catalysts owing to the controllable reductive defunctionalization of Mo₂CTₓ (either partial or complete),⁴⁹,⁵⁰ in combination with a thermal stability of up to ca. 550–600 °C (for multilayer Mo₂CTₓ with a nanoplatelet morphology),⁴⁹,⁵⁰ and a single (0001) basal surface structure.⁴⁶ Specifically, Mo₂CTₓ-derived catalysts proved useful in deciphering the electronic state of Mo atoms (average oxidation state of Mo that is linked to the O* coverage) under (reverse) water gas shift (R)WGS conditions. For instance, under RWGS conditions, a Mo₂CTₓ-derived catalyst free from Tₓ groups evolved toward a structure with a relatively low but measurable O* coverage.⁵⁰ In contrast, under WGS conditions, the same catalyst evolved to a full O* coverage, i.e., similar to the state of Mo in the parent Mo₂CTₓ (ca. +4.5 average Mo oxidation state), and the catalytic activity declined with increasing surface functionalization by O* species.⁴⁹,⁵⁰

This work aims to understand the relation between the composition of Mo₂CTₓ-derived catalysts, in particular their surface oxygen coverage and carbidic carbon content, and activity and selectivity in the FT process. We show that Mo₂CTₓ pretreated at 500 °C in undiluted H₂ (i.e., Mo₂CTₓ~500~), a material with Mo atoms only in a carbidic state (Mo²⁺), is a notably more active FT catalyst than Mo₂CTₓ pretreated at 400 °C (i.e., Mo₂CTₓ~400~), which has both Mo²⁺ and Mo⁴⁺ states in a ratio of ca. 2:3. Interestingly, the activity of Mo₂CTₓ~400~ increases appreciably with time on stream (TOS), which is explained by a decreasing Tₓ coverage with TOS via an *in situ* reduction of Mo⁴⁺ oxycarbidic states to the Mo²⁺ carbidic state. Interestingly, while both the *in situ* activated Mo₂CTₓ~400~ and Mo₂CTₓ~500~ display comparable steady-state CO conversion rates, a substantially different product selectivity is observed between these two catalysts at ca. 90% CO conversion. Specifically, while the *in situ* activated Mo₂CTₓ~400~ produces predominantly C₅⁺ alkanes, Mo₂CTₓ~500~ is selective to methane (55 and 61%, respectively). This distinct selectivity is explained by differences in the structure (and the active sites) and in particular the substoichiometric carbidic carbon content in Mo₂CTₓ~500~. The latter material is more accurately described as 2D-Mo₂C₁-x (rather than 2D-Mo₂C), with an atomic ratio of Mo to Ccarb of 2.8:1, while *in situ* activated Mo₂CTₓ~400~ features an atomic ratio of Mo to Ccarb of 1.9:1, which is close to that in the starting Mo₂CTₓ i.e., (2.0 ± 0.2):1. In addition, the morphology of the catalyst is found to impact the chain probability growth coefficient α that is approximately twice higher for the 2D-Mo₂C catalyst relative to reported values for 3D-Mo₂C (0.87 and ca. 0.3–0.4, respectively), which might be due to a confinement effect (chain growth in the interlayer space between the MXene sheets). The amount of C₅⁺ hydrocarbons produced per catalyst mass is substantially larger (by ca. 2 orders of magnitude) for 2D-Mo₂C relative to a reference β-Mo₂C catalyst (exposed to identical pretreatment conditions), highlighting the high (yet understudied) potential of MXenes for thermocatalytic applications. Density functional theory
carbides (TMCs), in particular Mo carbides, have been explored as FT catalysts.¹² Unsupported Mo carbides (cubic α-MoC₁-x and orthorhombic β-Mo₂C phases) yield mainly methane, CO₂, lower alkanes, and alkenes as FT products, with a chain probability growth coefficient (α) equal to 0.3–0.4.¹³⁻¹⁵ Using Mo₂C, the formation of alcohols has been reported as well¹⁶ and approaches to increase the selectivity of Mo carbides to C₂⁺ alcohols include their promotion with alkali metals such as potassium,¹⁷ or dispersing Mo carbide on a support (e.g., Al₂O₃, TiO₂).¹⁸⁻²⁰

Turning to the catalytic pathways of the FT process, the main mechanisms proposed are the carbide mechanism, the CO insertion mechanism, and the hydroxycarbene mechanism, each involving initiation, propagation, and chain termination steps.² Briefly, the carbide mechanism, proposed by Fischer and Tropsch,²¹ proceeds via the dissociative adsorption of CO to C* and O* that occurs simultaneously with the dissociation of H₂ to H* species and the subsequent hydrogenation of C* to CHₓ* (x = 1–3) species; the latter are involved in chain growth (the C–C coupling step).²² The dissociation of CO* may occur directly or may be hydrogen-assisted (molecular or H*).²³ The chain growth step can involve methylene (CH₂*),²⁴ methylidyne (CH*),²⁵⁻²⁸ or coupling between C* and CH* species.²⁹ In the CO insertion mechanism, CO inserts into an M–H bond (initiation) followed by the hydrogenation of the formyl (HCO*) species into CH₂O* species that are hydrogenated to CH₃* species and H₂O; further CO insertion into a metal–alkyl bond and hydrogenation is repeated until chain growth is terminated.³⁰ In contrast, the hydroxycarbene mechanism is linked to the formation of oxygenates and it includes a coupling reaction between two hydroxycarbene (RCOH*, R = H, alkyl) intermediates formed via the hydrogenation of adsorbed CO.³¹

All three main FT mechanisms have been proposed to proceed on Mo₂C. In particular, it has been suggested that Mo₂C catalyzes FT via a direct dissociation of CO into O* and C* species, i.e., a carbidic mechanism.³² Specifically, CO adsorption and H₂ temperature-programmed experiments have been used to confirm the direct dissociation of CO on a Mo₂C surface.¹⁴ However, the O* adsorbates formed can inhibit a further dissociation of CO and thereby deactivate the catalyst.³³ The involvement of an H-assisted pathway for the dissociation of CO has been suggested as well, in particular as a means to avoid the formation of a too-strongly bound O* species that reduce the catalytic turnover.³⁴ Moreover, a computational study suggested a CO insertion mechanism with a coupling between the CHₓ and CH₃O species to proceed on Mo₂C.³⁵ Lastly, the hydroxycarbene mechanism has been suggested for Mo₂C to account for the formation of alcohols.¹⁴

Oxycarbidic Mo₂CₓOᵧ species/phases can form *in situ* from Mo₂C via its reaction with oxygenates, and they have been proposed to be the catalytically active centers for the dry reforming of methane (DRM) or hydrodeoxygenation reactions.³⁶,³⁷ Depending on the chemical potential of the gas phase, Mo-terminated surfaces of Mo₂C can feature different coverages of O* adsorbates that can block adsorption sites and modify adsorption energies of reaction intermediates, which in turn influences the overall catalytic activity and product selectivity.³⁸,³⁹ While it is generally believed that higher O* coverages are associated with a lower FT activity,³²,⁴⁰ it is yet unclear if there is an optimum (low) O* coverage to yield the highest FT activity on Mo₂C;

furthermore, the dependence of product selectivity on O* coverage of Mo₂C is also understudied.

One strategy to improve our understanding of the catalytic activity of Mo₂C relies on the use of model catalysts with well-defined structures and surfaces, which facilitates their spectroscopic characterization and bridges the gap to computational models.⁴¹⁻⁴⁴ In this context, well-defined two-dimensional (2D) carbides of the MXene family,⁴⁵⁻⁴⁸ in particular Mo₂CTₓ (Tₓ are O, OH, and F surface termination groups), can serve as model catalysts owing to the controllable reductive defunctionalization of Mo₂CTₓ (either partial or complete),⁴⁹,⁵⁰ in combination with a thermal stability of up to ca. 550–600 °C (for multilayer Mo₂CTₓ with a nanoplatelet morphology),⁴⁹,⁵⁰ and a single (0001) basal surface structure.⁴⁶ Specifically, Mo₂CTₓ-derived catalysts proved useful in deciphering the electronic state of Mo atoms (average oxidation state of Mo that is linked to the O* coverage) under (reverse) water gas shift (R)WGS conditions. For instance, under RWGS conditions, a Mo₂CTₓ-derived catalyst free from Tₓ groups evolved toward a structure with a relatively low but measurable O* coverage.⁵⁰ In contrast, under WGS conditions, the same catalyst evolved to a full O* coverage, i.e., similar to the state of Mo in the parent Mo₂CTₓ (ca. +4.5 average Mo oxidation state), and the catalytic activity declined with increasing surface functionalization by O* species.⁴⁹,⁵⁰

This work aims to understand the relation between the composition of Mo₂CTₓ-derived catalysts, in particular their surface oxygen coverage and carbidic carbon content, and activity and selectivity in the FT process. We show that Mo₂CTₓ pretreated at 500 °C in undiluted H₂ (i.e., Mo₂CTₓ~500~), a material with Mo atoms only in a carbidic state (Mo²⁺), is a notably more active FT catalyst than Mo₂CTₓ pretreated at 400 °C (i.e., Mo₂CTₓ~400~), which has both Mo²⁺ and Mo⁴⁺ states in a ratio of ca. 2:3. Interestingly, the activity of Mo₂CTₓ~400~ increases appreciably with time on stream (TOS), which is explained by a decreasing Tₓ coverage with TOS via an *in situ* reduction of Mo⁴⁺ oxycarbidic states to the Mo²⁺ carbidic state. Interestingly, while both the *in situ* activated Mo₂CTₓ~400~ and Mo₂CTₓ~500~ display comparable steady-state CO conversion rates, a substantially different product selectivity is observed between these two catalysts at ca. 90% CO conversion. Specifically, while the *in situ* activated Mo₂CTₓ~400~ produces predominantly C₅⁺ alkanes, Mo₂CTₓ~500~ is selective to methane (55 and 61%, respectively). This distinct selectivity is explained by differences in the structure (and the active sites) and in particular the substoichiometric carbidic carbon content in Mo₂CTₓ~500~. The latter material is more accurately described as 2D-Mo₂C₁-x (rather than 2D-Mo₂C), with an atomic ratio of Mo to Ccarb of 2.8:1, while *in situ* activated Mo₂CTₓ~400~ features an atomic ratio of Mo to Ccarb of 1.9:1, which is close to that in the starting Mo₂CTₓ i.e., (2.0 ± 0.2):1. In addition, the morphology of the catalyst is found to impact the chain probability growth coefficient α that is approximately twice higher for the 2D-Mo₂C catalyst relative to reported values for 3D-Mo₂C (0.87 and ca. 0.3–0.4, respectively), which might be due to a confinement effect (chain growth in the interlayer space between the MXene sheets). The amount of C₅⁺ hydrocarbons produced per catalyst mass is substantially larger (by ca. 2 orders of magnitude) for 2D-Mo₂C relative to a reference β-Mo₂C catalyst (exposed to identical pretreatment conditions), highlighting the high (yet understudied) potential of MXenes for thermocatalytic applications. Density functional theory
<figure><img src="image_9.png" /><figcaption>**Figure 1.** (a) Schematic representation and (b) XRD pattern of as-prepared multilayered Mo₂CTₓ. (c) Raman spectra of Mo₂CTₓ, Mo₂CTₓ~400~ and Mo₂CTₓ~500~. The diamond symbol denotes a peak from the quartz capillary. (d) SEM images of Mo₂CTₓ~400~ and Mo₂CTₓ~500~. (e) Mo 3d and (f) C 1s XPS spectra of Mo₂CTₓ, Mo₂CTₓ~400~, and Mo₂CTₓ~500~. (g) Atomic ratio between molybdenum and carbidic carbon of Mo₂CTₓ, Mo₂CTₓ~400~, and Mo₂CTₓ~500~. (h) Schematic representation of the reductive defunctionalization of Mo₂CTₓ via H₂ pretreatment.</figcaption></figure>

(DFT) calculations identify a low barrier for the direct CO dissociation, suggesting a carbide mechanism, in which chain growth preferentially occurs via the coupling between CH\* and C\* species. The DFT energy profile corroborates the experimentally observed selectivity patterns, including the production of higher alkanes and CO₂ in the absence of oxygenates.

## METHODS

**Synthesis and Characterization.** Mo₂Ga₂C was synthesized from β-Mo₂C and metallic Ga following a reported method.⁵¹ The subsequent removal of Ga to yield the multilayered Mo₂CTₓ was performed by stirring Mo₂Ga₂C with 14 M HF at 140 °C for 7 days.⁴⁹,⁵⁰,⁵²,⁵³ The activated catalysts denoted Mo₂CTₓ~400~ and Mo₂CTₓ~500~ were prepared by treating the as synthesized Mo₂CTₓ (ca. 40 mg) in a vertical quartz reactor (i.d. 12 mm) with a flow of undiluted H₂ (20 mL min⁻¹, 1 bar) at 400 and 500 °C, respectively (heating ramp was 5 °C min⁻¹) for 2 h.⁵⁰ While we have reported previously that Mo₂CTₓ~500~ corresponds to 2D-Mo₂C, which is a multilayered material with a morphology of Mo₂CTₓ but with the absence of Tₓ groups,⁵⁰ in what follows we refine this description and demonstrate that Mo₂CTₓ~500~ is more appropriately represented as 2D-Mo₂C₁⁻ₓ. The activated materials were cooled down under N₂ flow (20 mL min⁻¹) and transferred to a glovebox (H₂O and O₂ < 1 ppm) without exposure to air. The materials denoted as β-Mo₂C(400) and β-Mo₂C(500) were prepared from β-Mo₂C in the above-described conditions, at 400 and 500 °C, respectively. For the catalytic FT tests, the activated materials were prepared in situ before switching to the reaction conditions, as described below. Additional details on the synthesis of materials and details on the powder X-ray diffraction (XRD), X-ray photoelectron

spectroscopy (XPS), Raman spectroscopy, and CO chemisorption methods are provided in the Supporting Information.

**Catalytic Testing.** The catalytic performance of β-Mo₂C and Mo₂CTₓ after H₂ pretreatment, was evaluated in two different reactors. The first reactor, made of stainless-steel SS316 with an internal diameter and length of 2 and 150 mm, respectively, allowed the quantification of the liquid products. A second reactor, made of Hastelloy X, with an internal diameter and length of 9.1 and 305 mm, respectively, was used in experiments performed to recover and characterize the activated catalysts without air exposure. In a typical catalytic experiment in the SS316 reactor, β-Mo₂C or Mo₂CTₓ (100 mg) was first pretreated in undiluted H₂ (20 mL min⁻¹) at, respectively, 400 or 500 °C (ramping rate 1 C min⁻¹) for 2 h; subsequently, the temperature decreased to 180 °C, the gas atmosphere was switched to syngas (H₂:CO = 2:1), and the pressure was set to 25 bar with the subsequent increase of the reaction temperature to 330 °C. N₂ contained in the gas bottle of CO (5%) served as an internal standard. In the material recovery experiments employing the Hastelloy X reactor, a N₂ flow of 1 or 2 mL min⁻¹ was used as an internal standard to calculate the CO conversion. Time zero of the TOS scale corresponds to the first GC point for which the concentration of the internal standard (N₂) stabilized (i.e., after ca. 2 h of the start of the experiments in the 2 mm reactor and ca. 4.5 h for the experiments in the 9.1 mm reactor). The total flow rate was 8.5 or 9.5 mL min⁻¹, yielding weight hourly space velocities (WHSV) of 5.1 or 5.7 L gcat⁻¹ h⁻¹ for the SS316 and Hastelloy X reactors, respectively. Gas chromatography (GC) analysis of the reagents and gaseous reaction products was performed using a Varian CP 3800 instrument equipped with a thermal conductivity detector (TCD) and a flame ionization detector (FID). Two columns were used for the analysis, a packed CTR
<figure><img src="image_9.png" /><figcaption>**Figure 1.** (a) Schematic representation and (b) XRD pattern of as-prepared multilayered Mo₂CTₓ. (c) Raman spectra of Mo₂CTₓ, Mo₂CTₓ⁻₄₀₀ and Mo₂CTₓ⁻₅₀₀. The diamond symbol denotes a peak from the quartz capillary. (d) SEM images of Mo₂CTₓ⁻₄₀₀ and Mo₂CTₓ⁻₅₀₀. (e) Mo 3d and (f) C 1s XPS spectra of Mo₂CTₓ, Mo₂CTₓ⁻₄₀₀, and Mo₂CTₓ⁻₅₀₀. (g) Atomic ratio between molybdenum and carbidic carbon of Mo₂CTₓ, Mo₂CTₓ⁻₄₀₀, and Mo₂CTₓ⁻₅₀₀. (h) Schematic representation of the reductive defunctionalization of Mo₂CTₓ via H₂ pretreatment.</figcaption></figure>

(DFT) calculations identify a low barrier for the direct CO dissociation, suggesting a carbide mechanism, in which chain growth preferentially occurs via the coupling between CH\* and C\* species. The DFT energy profile corroborates the experimentally observed selectivity patterns, including the production of higher alkanes and CO₂ in the absence of oxygenates.

## METHODS

**Synthesis and Characterization.** Mo₂Ga₂C was synthesized from β-Mo₂C and metallic Ga following a reported method.⁵¹ The subsequent removal of Ga to yield the multilayered Mo₂CTₓ was performed by stirring Mo₂Ga₂C with 14 M HF at 140 °C for 7 days.⁴⁹,⁵⁰,⁵²,⁵³ The activated catalysts denoted Mo₂CTₓ⁻₄₀₀ and Mo₂CTₓ⁻₅₀₀ were prepared by treating the as synthesized Mo₂CTₓ (ca. 40 mg) in a vertical quartz reactor (i.d. 12 mm) with a flow of undiluted H₂ (20 mL min⁻¹, 1 bar) at 400 and 500 °C, respectively (heating ramp was 5 °C min⁻¹) for 2 h.⁵⁰ While we have reported previously that Mo₂CTₓ⁻₅₀₀ corresponds to 2D-Mo₂C, which is a multilayered material with a morphology of Mo₂CTₓ but with the absence of Tₓ groups,⁵⁰ in what follows we refine this description and demonstrate that Mo₂CTₓ⁻₅₀₀ is more appropriately represented as 2D-Mo₂C₁⁻ₓ. The activated materials were cooled down under N₂ flow (20 mL min⁻¹) and transferred to a glovebox (H₂O and O₂ < 1 ppm) without exposure to air. The materials denoted as β-Mo₂C(400) and β-Mo₂C(500) were prepared from β-Mo₂C in the above-described conditions, at 400 and 500 °C, respectively. For the catalytic FT tests, the activated materials were prepared in situ before switching to the reaction conditions, as described below. Additional details on the synthesis of materials and details on the powder X-ray diffraction (XRD), X-ray photoelectron

spectroscopy (XPS), Raman spectroscopy, and CO chemisorption methods are provided in the Supporting Information.

**Catalytic Testing.** The catalytic performance of β-Mo₂C and Mo₂CTₓ after H₂ pretreatment, was evaluated in two different reactors. The first reactor, made of stainless-steel SS316 with an internal diameter and length of 2 and 150 mm, respectively, allowed the quantification of the liquid products. A second reactor, made of Hastelloy X, with an internal diameter and length of 9.1 and 305 mm, respectively, was used in experiments performed to recover and characterize the activated catalysts without air exposure. In a typical catalytic experiment in the SS316 reactor, β-Mo₂C or Mo₂CTₓ (100 mg) was first pretreated in undiluted H₂ (20 mL min⁻¹) at, respectively, 400 or 500 °C (ramping rate 1 C min⁻¹) for 2 h; subsequently, the temperature decreased to 180 °C, the gas atmosphere was switched to syngas (H₂:CO = 2:1), and the pressure was set to 25 bar with the subsequent increase of the reaction temperature to 330 °C. N₂ contained in the gas bottle of CO (5%) served as an internal standard. In the material recovery experiments employing the Hastelloy X reactor, a N₂ flow of 1 or 2 mL min⁻¹ was used as an internal standard to calculate the CO conversion. Time zero of the TOS scale corresponds to the first GC point for which the concentration of the internal standard (N₂) stabilized (i.e., after ca. 2 h of the start of the experiments in the 2 mm reactor and ca. 4.5 h for the experiments in the 9.1 mm reactor). The total flow rate was 8.5 or 9.5 mL min⁻¹, yielding weight hourly space velocities (WHSV) of 5.1 or 5.7 L gcat⁻¹ h⁻¹ for the SS316 and Hastelloy X reactors, respectively. Gas chromatography (GC) analysis of the reagents and gaseous reaction products was performed using a Varian CP 3800 instrument equipped with a thermal conductivity detector (TCD) and a flame ionization detector (FID). Two columns were used for the analysis, a packed CTR
1 column connected to the TCD and an Rt-Q-PLOT capillary column connected to the FID. Heavier hydrocarbon products were collected and analyzed offline. ¹H NMR analysis of the liquid fraction validated the absence of oxygenates (Figure S6). To analyze the heavier hydrocarbon products, ca. 90 mg of the heavy hydrocarbon fraction was dissolved in dichloromethane and subsequently analyzed using a SCION SQ-GCMS instrument. The Anderson–Schulz–Flory distribution was plotted for C₁₀–C₂₃ products to calculate the chain growth probability coefficient α. When the catalytic experiments were performed in a larger reactor, the activated catalysts were recovered in a glovebox for characterization and handled without exposure to air. In this reactor setup, the gaseous CO consumption was quantified with a PerkinElmer Clarus 580 GC equipped with a TCD.

**Computational Details.** Periodic DFT calculations were performed with the Vienna Ab Initio Simulation Package (VASP).⁵⁴,⁵⁵ The reported energy values correspond to Gibbs energies at 330 °C and 25 bar. The theoretical model of the (0001) facet of 2D-Mo₂C is shown in Figure S16 and has been previously reported.⁵⁶ Further details of the DFT calculations are provided in the Supporting Information.

## ■ RESULTS

**Materials.** Multilayered nanoplatelets of Mo₂CTₓ shown schematically in Figure 1a were obtained by etching Ga from Mo₂Ga₂C with HF, following a published method.⁴⁹ The XPS spectrum of Mo₂CTₓ features only a trace signal in the Ga 2p region, consistent with the successful removal of Ga (Figure S1). XRD of Mo₂CTₓ shows no reflections due to Mo₂Ga₂C but reveals a sharp characteristic low angle peak at 8.5°, owing to the (0002) planes of the stacked nanosheets in multilayered Mo₂CTₓ (Figure 1b).⁴⁹,⁵³

Our previous Mo K-edge X-ray absorption near edge structure (XANES) study has shown that while the edge energy of Mo₂CTₓ is found at 20011.2 eV, indicating an average ca. Mo⁴⁺ oxidation state in Mo₂CTₓ, the energies for β-Mo₂C and a material obtained after the pretreatment of Mo₂CTₓ in undiluted H₂ at 500 °C for 2 h (Mo₂CTₓ~500) are close, i.e., 20000.8 and 20001.4 eV, respectively.⁵⁰ In addition, XPS analysis of Mo₂CTₓ~500, performed under airtight conditions, revealed the presence of a single electronic state of Mo at a binding energy of 228.4 eV, assigned to the Mo²⁺ state. The layered structure of Mo₂CTₓ~500 is evident from the presence of the (0002) reflection at 11.5° (XRD measurement performed in air). To conclude, our reported data showed that after pretreatment in undiluted H₂ for 2 h, Mo₂CTₓ transforms into a material that is free from detectable amounts of surface termination groups.⁵⁰ That being said, using 20% H₂/N₂ at 500 °C leads only to a partial defunctionalization of Mo₂CTₓ.⁴⁹

With these results in mind, we pretreated Mo₂CTₓ at 400 °C under a flow of undiluted H₂ for 2 h (material denoted as Mo₂CTₓ~400) and performed a Raman analysis to compare the results obtained to that of as-prepared Mo₂CTₓ and Mo₂CTₓ~500. The Raman spectrum of as-prepared Mo₂CTₓ, excited by a 780 nm laser, displays two characteristic bands centered at 143 and 252 cm⁻¹ (Figure 1c and Figure S2). Raman bands at similar positions were also reported for Ti-based MXenes.⁵⁷ Theoretical calculations of a 2D-Mo₂CO₂ model with O* groups occupying a 3-fold hollow site attributed the Raman vibrations at 123 and 236 cm⁻¹ to in-plane (E_g) and out-of-plane (A₁g) vibrations of the O* groups, respectively.⁵⁸ Our experimentally observed frequencies for

Mo₂CTₓ are ca. 20 cm⁻¹ higher than the calculated ones, possibly owing to the presence of oxo, hydroxy, and fluoro terminations in Mo₂CTₓ in the experimental system as identified by XPS analysis (Figure S3; the DFT model only considered oxo groups instead). Next, we assessed the evolution of the Raman bands at 143 and 252 cm⁻¹ as a function of pretreatment temperature (spectra collected of materials kept in airtight capillaries). While the spectrum of Mo₂CTₓ~400 features only a low-intensity A₁g band that is shifted to 264 cm⁻¹, both E_g and A₁g vibrations are absent in Mo₂CTₓ~500, in line with the complete surface defunctionalization in this material. According to scanning electron microscopy, both Mo₂CTₓ~400 and Mo₂CTₓ~500 feature a layered nanoplatelet morphology typical for initial Mo₂CTₓ (Figure 1d).⁴⁹,⁵⁰,⁵³

Initial Mo₂CTₓ features a mixture of Mo⁴⁺ (55%) and Mo⁵⁺ (45%) states with the respective binding energies of 229.5 and 232.4 eV, owing to the oxidation of Mo sites by the Tₓ groups; note that there is no Mo²⁺ state due to carbidic Mo in initial (i.e., as-prepared) Mo₂CTₓ (Figure 1e and Table S7).⁴⁹,⁵⁰ In contrast, the two main electronic states of Mo found in Mo₂CTₓ~400 are Mo⁴⁺ (57%) and Mo²⁺ (38%) with the respective binding energies of 229.1 and 228.3 eV, (Table S7, Figure 1e, and Figure S4). Finally, in Mo₂CTₓ~500, Mo is exclusively in a Mo²⁺ state (carbidic Mo).⁴⁹,⁵⁰ The corresponding average oxidation states of Mo in Mo₂CTₓ, Mo₂CTₓ~400, and Mo₂CTₓ~500 are ca. +4.5 (Mo⁴⁺/Mo⁵⁺ in ca. 1:1 ratio), +3.3 (Mo⁴⁺ and Mo²⁺ in ca. 3:2 ratio), and +2 (only carbidic Mo), respectively. Overall, the XPS data are consistent with the partially defunctionalized Mo sites in Mo₂CTₓ~400.

Turning to the C 1s XPS region of Mo₂CTₓ, in addition to adventitious carbon at a binding energy of 284.7 eV, peaks fitted with BE at 283.4, 285.9, and 288.5 eV are assigned to carbidic carbon (C-Mo), C-O, and C=O fragments, respectively (Figure 1f and Table S8). Importantly, initial Mo₂CTₓ displays an atomic ratio of molybdenum to carbidic carbon (Mo:Ccarb) of (2.0 ± 0.2):1 (Figure 1g; the error bar represents the standard deviation from the measurement of three independent batches of Mo₂CTₓ). Mo₂CTₓ~400 displays a Mo:Ccarb ratio of 1.9:1, similar to that of initial Mo₂CTₓ. In contrast, the Mo:Ccarb ratio in Mo₂CTₓ~500 is increased notably to 2.8:1. This result can be explained by the loss of carbidic carbon during the H₂ pretreatment at 500 °C (in the form of methane, *vide infra*).

We have further verified inferences from the XPS study by performing a H₂ temperature-programmed reduction (TPR) experiment using Mo₂CTₓ and following the off-gas by MS analysis (Figure S5). Species with a *m/z* ratio of 16 and 15 appear due to the ionization of methane. The signal of those species undergoes only a slight increase during the isothermal segment at 400 °C, and a notable rise is observed when the temperature is increased to 500 °C, consistent with the XPS results discussed above. Species with *m/z* 18 and 17 are predominantly due to the ionization of water; the latter is formed during the reductive defunctionalization of the Tₓ groups. During this experiment, we cofed N₂ to H₂ as an internal standard (2 mL min⁻¹ of N₂ flow added to 20 mL min⁻¹ of H₂). The observed stability of the *m/z* 28 signal during the entire TPR-MS experiment validates that the observed intensity changes of other signals can be associated with the reductive transformations of Mo₂CTₓ.

A schematic representation visualizing the structural modification during the reductive defunctionalization of
1 column connected to the TCD and an Rt-Q-PLOT capillary column connected to the FID. Heavier hydrocarbon products were collected and analyzed offline. ¹H NMR analysis of the liquid fraction validated the absence of oxygenates (Figure S6). To analyze the heavier hydrocarbon products, ca. 90 mg of the heavy hydrocarbon fraction was dissolved in dichloromethane and subsequently analyzed using a SCION SQ-GCMS instrument. The Anderson–Schulz–Flory distribution was plotted for C₁₀–C₂₃ products to calculate the chain growth probability coefficient α. When the catalytic experiments were performed in a larger reactor, the activated catalysts were recovered in a glovebox for characterization and handled without exposure to air. In this reactor setup, the gaseous CO consumption was quantified with a PerkinElmer Clarus 580 GC equipped with a TCD.

**Computational Details.** Periodic DFT calculations were performed with the Vienna Ab Initio Simulation Package (VASP).⁵⁴,⁵⁵ The reported energy values correspond to Gibbs energies at 330 °C and 25 bar. The theoretical model of the (0001) facet of 2D-Mo₂C is shown in Figure S16 and has been previously reported.⁵⁶ Further details of the DFT calculations are provided in the Supporting Information.

## ■ RESULTS

**Materials.** Multilayered nanoplatelets of Mo₂CTₓ shown schematically in Figure 1a were obtained by etching Ga from Mo₂Ga₂C with HF, following a published method.⁴⁹ The XPS spectrum of Mo₂CTₓ features only a trace signal in the Ga 2p region, consistent with the successful removal of Ga (Figure S1). XRD of Mo₂CTₓ shows no reflections due to Mo₂Ga₂C but reveals a sharp characteristic low angle peak at 8.5°, owing to the (0002) planes of the stacked nanosheets in multilayered Mo₂CTₓ (Figure 1b).⁴⁹,⁵³

Our previous Mo K-edge X-ray absorption near edge structure (XANES) study has shown that while the edge energy of Mo₂CTₓ is found at 20011.2 eV, indicating an average ca. Mo⁴⁺ oxidation state in Mo₂CTₓ, the energies for β-Mo₂C and a material obtained after the pretreatment of Mo₂CTₓ in undiluted H₂ at 500 °C for 2 h (Mo₂CTₓ~500) are close, i.e., 20000.8 and 20001.4 eV, respectively.⁵⁰ In addition, XPS analysis of Mo₂CTₓ~500, performed under airtight conditions, revealed the presence of a single electronic state of Mo at a binding energy of 228.4 eV, assigned to the Mo²⁺ state. The layered structure of Mo₂CTₓ~500 is evident from the presence of the (0002) reflection at 11.5° (XRD measurement performed in air). To conclude, our reported data showed that after pretreatment in undiluted H₂ for 2 h, Mo₂CTₓ transforms into a material that is free from detectable amounts of surface termination groups.⁵⁰ That being said, using 20% H₂/N₂ at 500 °C leads only to a partial defunctionalization of Mo₂CTₓ.⁴⁹

With these results in mind, we pretreated Mo₂CTₓ at 400 °C under a flow of undiluted H₂ for 2 h (material denoted as Mo₂CTₓ~400) and performed a Raman analysis to compare the results obtained to that of as-prepared Mo₂CTₓ and Mo₂CTₓ~500. The Raman spectrum of as-prepared Mo₂CTₓ, excited by a 780 nm laser, displays two characteristic bands centered at 143 and 252 cm⁻¹ (Figure 1c and Figure S2). Raman bands at similar positions were also reported for Ti-based MXenes.⁵⁷ Theoretical calculations of a 2D-Mo₂CO₂ model with O* groups occupying a 3-fold hollow site attributed the Raman vibrations at 123 and 236 cm⁻¹ to in-plane (E_g) and out-of-plane (A₁g) vibrations of the O* groups, respectively.⁵⁸ Our experimentally observed frequencies for

Mo₂CTₓ are ca. 20 cm⁻¹ higher than the calculated ones, possibly owing to the presence of oxo, hydroxy, and fluoro terminations in Mo₂CTₓ in the experimental system as identified by XPS analysis (Figure S3; the DFT model only considered oxo groups instead). Next, we assessed the evolution of the Raman bands at 143 and 252 cm⁻¹ as a function of pretreatment temperature (spectra collected of materials kept in airtight capillaries). While the spectrum of Mo₂CTₓ~400 features only a low-intensity A₁g band that is shifted to 264 cm⁻¹, both E_g and A₁g vibrations are absent in Mo₂CTₓ~500, in line with the complete surface defunctionalization in this material. According to scanning electron microscopy, both Mo₂CTₓ~400 and Mo₂CTₓ~500 feature a layered nanoplatelet morphology typical for initial Mo₂CTₓ (Figure 1d).⁴⁹,⁵⁰,⁵³

Initial Mo₂CTₓ features a mixture of Mo⁴⁺ (55%) and Mo⁵⁺ (45%) states with the respective binding energies of 229.5 and 232.4 eV, owing to the oxidation of Mo sites by the Tₓ groups; note that there is no Mo²⁺ state due to carbidic Mo in initial (i.e., as-prepared) Mo₂CTₓ (Figure 1e and Table S7).⁴⁹,⁵⁰ In contrast, the two main electronic states of Mo found in Mo₂CTₓ~400 are Mo⁴⁺ (57%) and Mo²⁺ (38%) with the respective binding energies of 229.1 and 228.3 eV, (Table S7, Figure 1e, and Figure S4). Finally, in Mo₂CTₓ~500, Mo is exclusively in a Mo²⁺ state (carbidic Mo).⁴⁹,⁵⁰ The corresponding average oxidation states of Mo in Mo₂CTₓ, Mo₂CTₓ~400, and Mo₂CTₓ~500 are ca. +4.5 (Mo⁴⁺/Mo⁵⁺ in ca. 1:1 ratio), +3.3 (Mo⁴⁺ and Mo²⁺ in ca. 3:2 ratio), and +2 (only carbidic Mo), respectively. Overall, the XPS data are consistent with the partially defunctionalized Mo sites in Mo₂CTₓ~400.

Turning to the C 1s XPS region of Mo₂CTₓ, in addition to adventitious carbon at a binding energy of 284.7 eV, peaks fitted with BE at 283.4, 285.9, and 288.5 eV are assigned to carbidic carbon (C-Mo), C-O, and C=O fragments, respectively (Figure 1f and Table S8). Importantly, initial Mo₂CTₓ displays an atomic ratio of molybdenum to carbidic carbon (Mo:Ccarb) of (2.0 ± 0.2):1 (Figure 1g; the error bar represents the standard deviation from the measurement of three independent batches of Mo₂CTₓ). Mo₂CTₓ~400 displays a Mo:Ccarb ratio of 1.9:1, similar to that of initial Mo₂CTₓ. In contrast, the Mo:Ccarb ratio in Mo₂CTₓ~500 is increased notably to 2.8:1. This result can be explained by the loss of carbidic carbon during the H₂ pretreatment at 500 °C (in the form of methane, *vide infra*).

We have further verified inferences from the XPS study by performing a H₂ temperature-programmed reduction (TPR) experiment using Mo₂CTₓ and following the off-gas by MS analysis (Figure S5). Species with a *m/z* ratio of 16 and 15 appear due to the ionization of methane. The signal of those species undergoes only a slight increase during the isothermal segment at 400 °C, and a notable rise is observed when the temperature is increased to 500 °C, consistent with the XPS results discussed above. Species with *m/z* 18 and 17 are predominantly due to the ionization of water; the latter is formed during the reductive defunctionalization of the Tₓ groups. During this experiment, we cofed N₂ to H₂ as an internal standard (2 mL min⁻¹ of N₂ flow added to 20 mL min⁻¹ of H₂). The observed stability of the *m/z* 28 signal during the entire TPR-MS experiment validates that the observed intensity changes of other signals can be associated with the reductive transformations of Mo₂CTₓ.

A schematic representation visualizing the structural modification during the reductive defunctionalization of
<figure><img src="image_10.png" /><figcaption>**Figure 2.** Conversion of CO with TOS using (a) β-Mo₂C₄₀₀, (b) Mo₂CTₓ-500, and (c) Mo₂CTₓ-400 in FT. Insets show the gas-phase product distribution for the steady-state activity that corresponds to XCO = 2, 94, and 88%, respectively. (d) Liquid phase analysis (post reaction) for Mo₂CTₓ-400. Catalytic tests were performed in a stainless-steel reactor with 2 mm internal diameter at 25 bar, 330 °C, with a CO:H₂ ratio of 1:2 and a space velocity of 5.1 L·(gcat·h)⁻¹. The carbon balance is close to 100% for most of GC points and exceeds 90% for all GC points. (e) Steady-state gravimetric rate of CO consumption and C₅⁺ production for β-Mo₂C₄₀₀, Mo₂CTₓ-500, and Mo₂CTₓ-400-TOS₈h as well as the respective initial rates (i.e., before *in situ* activation) for Mo₂CTₓ-400-TOS₁h. (f) Mo 3d (left) and C 1s (right) XPS spectra of Mo₂CTₓ-400 and Mo₂CTₓ-500 after ca. 2 h TOS. Experiments designed to recover and characterize the activated catalyst were performed in a Hastelloy reactor with 9.1 mm internal diameter at 25 bar, 330 °C, with a CO:H₂ ratio of 1:2 and a space velocity of 5.7 L·(gcat·h)⁻¹.</figcaption></figure>

Mo₂CTₓ under undiluted H₂ yielding Mo₂CTₓ-400 and Mo₂CTₓ-500 (i.e., 2D-Mo₂C₁-x) is shown in Figure 1h.

**In Situ Activation of Mo₂CTₓ-400 under FT Conditions.**

Turning to the FT activity of the prepared materials, we first examined the performance of the reference β-Mo₂C₄₀₀ using a H₂:CO ratio of 2:1, 330 °C, and 25 bar and a WHSV of 5.1 L·(gcat·h)⁻¹. β-Mo₂C₄₀₀ shows a stable CO conversion of only ca. 2% (Figure 2a). At this very low conversion (that corresponds to a gravimetric CO consumption of 1.3 mmol CO gcat·h⁻¹), the selectivity to CO₂ is 15% and the partial selectivities (i.e., selectivity excluding CO₂) to CH₄, C₂–C₄ alkanes, C₂–C₄ alkenes, and C₅⁺ alkanes are 52, 23, 13, and 12%, respectively (Figure 2a). No organic liquid fraction in amounts sufficient for analysis was produced.

In sharp contrast, Mo₂CTₓ-500 displays, under identical testing conditions, an initial conversion of 94% and shows no further changes in CO conversion and product selectivity within the whole duration of the experiment (ca. 20 h TOS, Figure 2b and Table S1). The selectivity to CO₂ on Mo₂CTₓ-500 is 48%, while the partial selectivities to CH₄, C₂–C₄ alkanes, and C₅⁺ alkanes are 61, 37, and 2%, respectively. In contrast to β-Mo₂C₄₀₀, no significant amounts of olefins (i.e., >0.5%) are detected for Mo₂CTₓ-500. As in the case of β-Mo₂C₄₀₀, no organic liquid fraction in amounts sufficient for analysis was produced during the catalytic test. Overall, Mo₂CTₓ-500 is a poor FT catalyst that produces 19.9 mmol CH₄ gcat·h⁻¹ and merely 0.6 mmol C₅⁺ gcat·h⁻¹ (i.e., it is rather a methanation catalyst than a catalyst for FT).

Next, we assessed the FT activity of Mo₂CTₓ-400 under identical conditions and observed a remarkable *in situ* activation of Mo₂CTₓ-400 with TOS; that is, the initial CO conversion of 12% at ca. 1 h increased to 88% after 8 h of TOS and remained stable until the end of the experiment (ca. 20 h,

Figure 2c). We denote the initial catalyst as Mo₂CTₓ-400-TOS₁h and the catalyst that has undergone the *in situ* activation and reached the steady-state conditions as Mo₂CTₓ-400-TOS₈h. The selectivity to CO₂ for Mo₂CTₓ-400-TOS₈h is 50%, which parallels that of Mo₂CTₓ-500. Yet, the partial selectivities to CH₄, C₂–C₄ alkanes, and C₅⁺ alkanes are 25, 20, and 55%, respectively (Figure 2c and Table S1, entry 4). The liquid fraction, accumulated throughout the experiment, consisted of water and higher alkanes, with an alkane distribution corresponding to a chain growth probability coefficient α = 0.87 (Figure 2d). This α value is ca. two times higher than the value reported for unsupported 3D molybdenum carbides (α-MoC₁-x and β-Mo₂C)¹⁴ and is similar to Fe-based FT catalysts.⁵⁹ Furthermore, no oxygenates (Figure S6) or waxes were formed on Mo₂CTₓ-400. When evaluating the transient period of the experiment, it is observed that with increasing CO conversion, the selectivity toward CO₂ increases at the expense of hydrocarbon selectivity (Figure S7 and Table S1, entries 2–4).

The gravimetric rate of CO consumption and that of C₅⁺ production for β-Mo₂C₄₀₀, Mo₂CTₓ-500, Mo₂CTₓ-400-TOS₁h, and Mo₂CTₓ-400-TOS₈h are plotted in Figure 2e and presented in Table S2. More specifically, Mo₂CTₓ-400-TOS₈h and Mo₂CTₓ-500 convert CO with similar rates, i.e., 58 and 62 mmol CO gcat·h⁻¹, at 88 and 94% CO conversion, respectively. These rates are ca. 7 and 45 times higher relative to Mo₂CTₓ-400-TOS₁h and β-Mo₂C₄₀₀, at 16 and 2% CO conversion, respectively. Interestingly, the gravimetric formation rate to C₅⁺ alkanes (15.7 mmol C₅⁺ gcat·h⁻¹) displayed by Mo₂CTₓ-400-TOS₈h is ca. 25 times higher than that of Mo₂CTₓ-500. In what follows, we will rationalize the *in situ* activation results by correlating the activities of Mo₂CTₓ-400
<figure><img src="image_10.png" /><figcaption>**Figure 2.** Conversion of CO with TOS using (a) β-Mo₂C₄₀₀, (b) Mo₂CTₓ-500, and (c) Mo₂CTₓ-400 in FT. Insets show the gas-phase product distribution for the steady-state activity that corresponds to XCO = 2, 94, and 88%, respectively. (d) Liquid phase analysis (post reaction) for Mo₂CTₓ-400. Catalytic tests were performed in a stainless-steel reactor with 2 mm internal diameter at 25 bar, 330 °C, with a CO:H₂ ratio of 1:2 and a space velocity of 5.1 L·(gcat·h)⁻¹. The carbon balance is close to 100% for most of GC points and exceeds 90% for all GC points. (e) Steady-state gravimetric rate of CO consumption and C₅⁺ production for β-Mo₂C₄₀₀, Mo₂CTₓ-500, and Mo₂CTₓ-400-TOS₈h as well as the respective initial rates (i.e., before *in situ* activation) for Mo₂CTₓ-400-TOS₁h. (f) Mo 3d (left) and C 1s (right) XPS spectra of Mo₂CTₓ-400 and Mo₂CTₓ-500 after ca. 2 h TOS. Experiments designed to recover and characterize the activated catalyst were performed in a Hastelloy reactor with 9.1 mm internal diameter at 25 bar, 330 °C, with a CO:H₂ ratio of 1:2 and a space velocity of 5.7 L·(gcat·h)⁻¹.</figcaption></figure>

Mo₂CTₓ under undiluted H₂ yielding Mo₂CTₓ-400 and Mo₂CTₓ-500 (i.e., 2D-Mo₂C₁-x) is shown in Figure 1h.

**In Situ Activation of Mo₂CTₓ-400 under FT Conditions.**

Turning to the FT activity of the prepared materials, we first examined the performance of the reference β-Mo₂C₄₀₀ using a H₂:CO ratio of 2:1, 330 °C, and 25 bar and a WHSV of 5.1 L·(gcat·h)⁻¹. β-Mo₂C₄₀₀ shows a stable CO conversion of only ca. 2% (Figure 2a). At this very low conversion (that corresponds to a gravimetric CO consumption of 1.3 mmol CO gcat·h⁻¹), the selectivity to CO₂ is 15% and the partial selectivities (i.e., selectivity excluding CO₂) to CH₄, C₂–C₄ alkanes, C₂–C₄ alkenes, and C₅⁺ alkanes are 52, 23, 13, and 12%, respectively (Figure 2a). No organic liquid fraction in amounts sufficient for analysis was produced.

In sharp contrast, Mo₂CTₓ-500 displays, under identical testing conditions, an initial conversion of 94% and shows no further changes in CO conversion and product selectivity within the whole duration of the experiment (ca. 20 h TOS, Figure 2b and Table S1). The selectivity to CO₂ on Mo₂CTₓ-500 is 48%, while the partial selectivities to CH₄, C₂–C₄ alkanes, and C₅⁺ alkanes are 61, 37, and 2%, respectively. In contrast to β-Mo₂C₄₀₀, no significant amounts of olefins (i.e., >0.5%) are detected for Mo₂CTₓ-500. As in the case of β-Mo₂C₄₀₀, no organic liquid fraction in amounts sufficient for analysis was produced during the catalytic test. Overall, Mo₂CTₓ-500 is a poor FT catalyst that produces 19.9 mmol CH₄ gcat·h⁻¹ and merely 0.6 mmol C₅⁺ gcat·h⁻¹ (i.e., it is rather a methanation catalyst than a catalyst for FT).

Next, we assessed the FT activity of Mo₂CTₓ-400 under identical conditions and observed a remarkable *in situ* activation of Mo₂CTₓ-400 with TOS; that is, the initial CO conversion of 12% at ca. 1 h increased to 88% after 8 h of TOS and remained stable until the end of the experiment (ca. 20 h,

Figure 2c). We denote the initial catalyst as Mo₂CTₓ-400-TOS₁h and the catalyst that has undergone the *in situ* activation and reached the steady-state conditions as Mo₂CTₓ-400-TOS₈h. The selectivity to CO₂ for Mo₂CTₓ-400-TOS₈h is 50%, which parallels that of Mo₂CTₓ-500. Yet, the partial selectivities to CH₄, C₂–C₄ alkanes, and C₅⁺ alkanes are 25, 20, and 55%, respectively (Figure 2c and Table S1, entry 4). The liquid fraction, accumulated throughout the experiment, consisted of water and higher alkanes, with an alkane distribution corresponding to a chain growth probability coefficient α = 0.87 (Figure 2d). This α value is ca. two times higher than the value reported for unsupported 3D molybdenum carbides (α-MoC₁-x and β-Mo₂C)¹⁴ and is similar to Fe-based FT catalysts.⁵⁹ Furthermore, no oxygenates (Figure S6) or waxes were formed on Mo₂CTₓ-400. When evaluating the transient period of the experiment, it is observed that with increasing CO conversion, the selectivity toward CO₂ increases at the expense of hydrocarbon selectivity (Figure S7 and Table S1, entries 2–4).

The gravimetric rate of CO consumption and that of C₅⁺ production for β-Mo₂C₄₀₀, Mo₂CTₓ-500, Mo₂CTₓ-400-TOS₁h, and Mo₂CTₓ-400-TOS₈h are plotted in Figure 2e and presented in Table S2. More specifically, Mo₂CTₓ-400-TOS₈h and Mo₂CTₓ-500 convert CO with similar rates, i.e., 58 and 62 mmol CO gcat·h⁻¹, at 88 and 94% CO conversion, respectively. These rates are ca. 7 and 45 times higher relative to Mo₂CTₓ-400-TOS₁h and β-Mo₂C₄₀₀, at 16 and 2% CO conversion, respectively. Interestingly, the gravimetric formation rate to C₅⁺ alkanes (15.7 mmol C₅⁺ gcat·h⁻¹) displayed by Mo₂CTₓ-400-TOS₈h is ca. 25 times higher than that of Mo₂CTₓ-500. In what follows, we will rationalize the *in situ* activation results by correlating the activities of Mo₂CTₓ-400
and Mo₂CTₓ-500 to the *ex situ* XPS analysis of the activated catalysts.

Next, we compared the XPS spectra of Mo₂CTₓ-400 and Mo₂CTₓ-500 to that of active Mo₂CTₓ-400-TOS₂h and Mo₂CTₓ-500-TOS₂h. Here, Mo₂CTₓ-400 and Mo₂CTₓ-500 were tested in FT conditions (25 bar, 330 °C, CO:H₂ ratio of 1:2 for 2 h), followed by their recovery and XPS analysis without exposure to air. Mo₂CTₓ-400 displays an initial CO conversion of 13% that increases to 17% after 2 h TOS. We note that in this case, Mo₂CTₓ-400-TOS₂h has not yet reached the steady state. In contrast, Mo₂CTₓ-500 displays a stable CO conversion of 93%. The values of CO conversion displayed by Mo₂CTₓ-400-TOS₂h and Mo₂CTₓ-500-TOS₂h are close to those of Mo₂CTₓ-400 before and after its *in situ* activation, respectively, of the experiment described in Figure 2c; in addition, both experiments with Mo₂CTₓ-500 show similar steady-state conversions (94 and 93%) and no activation period (Figure 2b and Figure S11). Compared to the catalytic FT experiments, *in situ* activation of Mo₂CTₓ-400 is slower in the experiment designed to recover and characterize the activated catalyst. This is explained by a less efficient gas-solid contacting when using an undiluted (and therefore low volume) Mo₂CTₓ-400 bed and a larger diameter of the reactor used (see experimental section for details).

Mo 3d XPS analysis of Mo₂CTₓ-400-TOS₂h and Mo₂CTₓ-500-TOS₂h shows little changes when compared to fresh Mo₂CTₓ-400 and Mo₂CTₓ-500 (Figure 2f, Figure S4, and Table S7). Interestingly, Mo₂CTₓ-500 remains fully defunctionalized despite the presence of oxygenates (CO₂ and water) under FT conditions. For Mo₂CTₓ-400-TOS₂h, there is a minor increase in its carbidic Mo component, from 38 to 41% relative to Mo₂CTₓ-400, which is paralleled by a rise of 4% in its CO conversion during 2 h TOS. Turning to the C 1s XPS region, Mo₂CTₓ-400-TOS₂h shows an additional broad peak at a binding energy of ca. 288.9 eV, assigned to molecularly adsorbed CO*. A similar peak was observed by us previously on the active state of a 2D-Mo₂C₁-xO_y reverse water-gas shift catalyst.⁵⁰ In contrast, the peaks due to adsorbed CO*, C-O, and C=O are absent in Mo₂CTₓ-500-TOS₂h, which only shows a MXene peak due to carbidic carbon (Figure 2f).⁵⁰ This observation correlates with a notably higher CO conversion in Mo₂CTₓ-500 relative to Mo₂CTₓ-400. The atomic ratio of Mo to Ccarb in Mo₂CTₓ-400-TOS₂h is found to be 1.9:1 (Figure S12), which is the same as in Mo₂CTₓ-400, as discussed above. In contrast, fitting of Mo₂CTₓ-500-TOS₂h reveals a ratio of 2.6:1, which is slightly lower than 2.8:1 in Mo₂CTₓ-500. The result indicates that the content of carbidic carbon in Mo₂CTₓ-500 may increase slightly under FT conditions within 2 h of TOS. Overall, the substoichiometric ratio between Mo and carbidic carbon in Mo₂CTₓ-500-TOS₂h parallels the high and stable methanation selectivity (and low FT selectivity) displayed by Mo₂CTₓ-500. Although elucidating the origin of the high methanation selectivity of Mo₂CTₓ-500 is beyond the scope of this work, the methanation mechanism may involve carbon vacancy sites of Mo₂CTₓ-500.

SEM images of the as-prepared and activated catalysts show that the layered nanoplatelet morphology is preserved during the FT reaction (Figure S13). XRD analysis of Mo₂CTₓ-500-TOS₂h and Mo₂CTₓ-400-TOS₂h, both opened to air, confirms the maintenance of a 2D morphology (cell parameter *c* of 15.50 and 15.45 Å, respectively) and the absence of any new crystalline phases (Figure S14).

A note concerning the determination of the amount of Mo surface sites in our 2D catalysts is that determining the quantity of Mo surface sites by CO chemisorption is challenging because of the low temperature of CO desorption from Mo carbides; that is, 2D-Mo₂C features a broad CO desorption peak centered at ca. 24 °C,⁵⁰ necessitating the use of low-temperature CO chemisorption experiments to ensure that a full CO coverage is being measured (details about the CO chemisorption experiments are provided in the Supporting Information). However, performing CO chemisorption at -30 °C likely results in gas diffusion limitations into the interlayer space of MXenes, as can be seen from a (unexpected) higher CO chemisorption capacity of Mo₂CTₓ-400 relative to Mo₂CTₓ-500 (Table S3). Low-temperature gas diffusion limitation is a known issue for the determination of specific surface area of MXenes using N₂ physisorption (i.e., reported surface area values are notably lower than theoretically predicted values; see further details in the SI).

To conclude, the higher CO conversion displayed by Mo₂CTₓ-500 relative to Mo₂CTₓ-400 (prior to *in situ* activation) correlates with the absence of Tₓ passivating species in Mo₂CTₓ-500-TOS₂h and the presence of Tₓ species in Mo₂CTₓ-400-TOS₂h, as shown by the detection of Mo⁴⁺ and Mo⁵⁺ electronic states, in addition to the carbidic Mo²⁺ state, in Mo₂CTₓ-400-TOS₂h. The selectivity of Mo₂CTₓ-500 to C₅⁺ (i.e., FT products) is low, while its selectivity to methane is high, and this correlates with the substoichiometric ratio of Mo to carbidic carbon in both Mo₂CTₓ-500 and Mo₂CTₓ-500-TOS₂h, owing to a loss of carbidic carbon during the H₂ pretreatment at 500 °C. Carbon vacancies in Mo₂CTₓ-500 are not readily replenished under the FT testing conditions used in this work (i.e., there is only a small increase of carbidic carbon in Mo₂CTₓ-500-TOS₂h relative to Mo₂CTₓ-500 that is within the experimental uncertainty). In contrast, H₂ pretreatment of Mo₂CTₓ at 400 °C does not form significant amounts of carbon vacancies while exposure of Mo₂CTₓ-400 to the FT conditions leads to the *in situ* removal of the remaining Tₓ passivating species (without the concomitant formation of carbon vacancies). The active state of Mo₂CTₓ-400 after *in situ* activation can therefore be described as 2D-Mo₂C, while the active state of Mo₂CTₓ-500 is more correctly described as 2D-Mo₂C₁-x (Figure 3). These results underline the importance of optimized reductive surface defunctionalization protocols to achieve the full potential of Mo₂CTₓ-derived catalysts in FT. In the following, we rationalize the selectivities displayed by 2D-

<figure><img src="image_11.png" /><figcaption>**Figure 3.** Schematic representation of the likely routes of reductive defunctionalization of Mo₂CTₓ in H₂ and under FT conditions and implications for FT selectivity.</figcaption></figure>
and Mo₂CTₓ⁻₅₀₀ to the *ex situ* XPS analysis of the activated catalysts.

Next, we compared the XPS spectra of Mo₂CTₓ⁻₄₀₀ and Mo₂CTₓ⁻₅₀₀ to that of active Mo₂CTₓ⁻₄₀₀-TOS₂h and Mo₂CTₓ⁻₅₀₀-TOS₂h. Here, Mo₂CTₓ⁻₄₀₀ and Mo₂CTₓ⁻₅₀₀ were tested in FT conditions (25 bar, 330 °C, CO:H₂ ratio of 1:2 for 2 h), followed by their recovery and XPS analysis without exposure to air. Mo₂CTₓ⁻₄₀₀ displays an initial CO conversion of 13% that increases to 17% after 2 h TOS. We note that in this case, Mo₂CTₓ⁻₄₀₀-TOS₂h has not yet reached the steady state. In contrast, Mo₂CTₓ⁻₅₀₀ displays a stable CO conversion of 93%. The values of CO conversion displayed by Mo₂CTₓ⁻₄₀₀-TOS₂h and Mo₂CTₓ⁻₅₀₀-TOS₂h are close to those of Mo₂CTₓ⁻₄₀₀ before and after its *in situ* activation, respectively, of the experiment described in Figure 2c; in addition, both experiments with Mo₂CTₓ⁻₅₀₀ show similar steady-state conversions (94 and 93%) and no activation period (Figure 2b and Figure S11). Compared to the catalytic FT experiments, *in situ* activation of Mo₂CTₓ⁻₄₀₀ is slower in the experiment designed to recover and characterize the activated catalyst. This is explained by a less efficient gas-solid contacting when using an undiluted (and therefore low volume) Mo₂CTₓ⁻₄₀₀ bed and a larger diameter of the reactor used (see experimental section for details).

Mo 3d XPS analysis of Mo₂CTₓ⁻₄₀₀-TOS₂h and Mo₂CTₓ⁻₅₀₀-TOS₂h shows little changes when compared to fresh Mo₂CTₓ⁻₄₀₀ and Mo₂CTₓ⁻₅₀₀ (Figure 2f, Figure S4, and Table S7). Interestingly, Mo₂CTₓ⁻₅₀₀ remains fully defunctionalized despite the presence of oxygenates (CO₂ and water) under FT conditions. For Mo₂CTₓ⁻₄₀₀-TOS₂h, there is a minor increase in its carbidic Mo component, from 38 to 41% relative to Mo₂CTₓ⁻₄₀₀, which is paralleled by a rise of 4% in its CO conversion during 2 h TOS. Turning to the C 1s XPS region, Mo₂CTₓ⁻₄₀₀-TOS₂h shows an additional broad peak at a binding energy of ca. 288.9 eV, assigned to molecularly adsorbed CO*. A similar peak was observed by us previously on the active state of a 2D-Mo₂C₁⁻ₓOᵧ reverse water-gas shift catalyst.⁵⁰ In contrast, the peaks due to adsorbed CO*, C-O, and C=O are absent in Mo₂CTₓ⁻₅₀₀-TOS₂h, which only shows a MXene peak due to carbidic carbon (Figure 2f).⁵⁰ This observation correlates with a notably higher CO conversion in Mo₂CTₓ⁻₅₀₀ relative to Mo₂CTₓ⁻₄₀₀. The atomic ratio of Mo to Ccarb in Mo₂CTₓ⁻₄₀₀-TOS₂h is found to be 1.9:1 (Figure S12), which is the same as in Mo₂CTₓ⁻₄₀₀, as discussed above. In contrast, fitting of Mo₂CTₓ⁻₅₀₀-TOS₂h reveals a ratio of 2.6:1, which is slightly lower than 2.8:1 in Mo₂CTₓ⁻₅₀₀. The result indicates that the content of carbidic carbon in Mo₂CTₓ⁻₅₀₀ may increase slightly under FT conditions within 2 h of TOS. Overall, the substoichiometric ratio between Mo and carbidic carbon in Mo₂CTₓ⁻₅₀₀-TOS₂h parallels the high and stable methanation selectivity (and low FT selectivity) displayed by Mo₂CTₓ⁻₅₀₀. Although elucidating the origin of the high methanation selectivity of Mo₂CTₓ⁻₅₀₀ is beyond the scope of this work, the methanation mechanism may involve carbon vacancy sites of Mo₂CTₓ⁻₅₀₀.

SEM images of the as-prepared and activated catalysts show that the layered nanoplatelet morphology is preserved during the FT reaction (Figure S13). XRD analysis of Mo₂CTₓ⁻₅₀₀-TOS₂h and Mo₂CTₓ⁻₄₀₀-TOS₂h, both opened to air, confirms the maintenance of a 2D morphology (cell parameter *c* of 15.50 and 15.45 Å, respectively) and the absence of any new crystalline phases (Figure S14).

A note concerning the determination of the amount of Mo surface sites in our 2D catalysts is that determining the quantity of Mo surface sites by CO chemisorption is challenging because of the low temperature of CO desorption from Mo carbides; that is, 2D-Mo₂C features a broad CO desorption peak centered at ca. 24 °C,⁵⁰ necessitating the use of low-temperature CO chemisorption experiments to ensure that a full CO coverage is being measured (details about the CO chemisorption experiments are provided in the Supporting Information). However, performing CO chemisorption at -30 °C likely results in gas diffusion limitations into the interlayer space of MXenes, as can be seen from a (unexpected) higher CO chemisorption capacity of Mo₂CTₓ⁻₄₀₀ relative to Mo₂CTₓ⁻₅₀₀ (Table S3). Low-temperature gas diffusion limitation is a known issue for the determination of specific surface area of MXenes using N₂ physisorption (i.e., reported surface area values are notably lower than theoretically predicted values; see further details in the SI).

To conclude, the higher CO conversion displayed by Mo₂CTₓ⁻₅₀₀ relative to Mo₂CTₓ⁻₄₀₀ (prior to *in situ* activation) correlates with the absence of Tₓ passivating species in Mo₂CTₓ⁻₅₀₀-TOS₂h and the presence of Tₓ species in Mo₂CTₓ⁻₄₀₀-TOS₂h, as shown by the detection of Mo⁴⁺ and Mo⁵⁺ electronic states, in addition to the carbidic Mo²⁺ state, in Mo₂CTₓ⁻₄₀₀-TOS₂h. The selectivity of Mo₂CTₓ⁻₅₀₀ to C₅⁺ (i.e., FT products) is low, while its selectivity to methane is high, and this correlates with the substoichiometric ratio of Mo to carbidic carbon in both Mo₂CTₓ⁻₅₀₀ and Mo₂CTₓ⁻₅₀₀-TOS₂h owing to a loss of carbidic carbon during the H₂ pretreatment at 500 °C. Carbon vacancies in Mo₂CTₓ⁻₅₀₀ are not readily replenished under the FT testing conditions used in this work (i.e., there is only a small increase of carbidic carbon in Mo₂CTₓ⁻₅₀₀-TOS₂h relative to Mo₂CTₓ⁻₅₀₀ that is within the experimental uncertainty). In contrast, H₂ pretreatment of Mo₂CTₓ at 400 °C does not form significant amounts of carbon vacancies while exposure of Mo₂CTₓ⁻₄₀₀ to the FT conditions leads to the *in situ* removal of the remaining Tₓ passivating species (without the concomitant formation of carbon vacancies). The active state of Mo₂CTₓ⁻₄₀₀ after *in situ* activation can therefore be described as 2D-Mo₂C, while the active state of Mo₂CTₓ⁻₅₀₀ is more correctly described as 2D-Mo₂C₁⁻ₓ (Figure 3). These results underline the importance of optimized reductive surface defunctionalization protocols to achieve the full potential of Mo₂CTₓ-derived catalysts in FT. In the following, we rationalize the selectivities displayed by 2D-

<figure><img src="image_11.png" /><figcaption>**Figure 3.** Schematic representation of the likely routes of reductive defunctionalization of Mo₂CTₓ in H₂ and under FT conditions and implications for FT selectivity.</figcaption></figure>
<figure><img src="image_12.png" /><figcaption>**Figure 4.** (a) Top and side views of the 2D-Mo₂C DFT model showing 3-fold hollow sites over a Mo atom (*H*<sub>Mo</sub>) and over a carbon atom (*H*<sub>C</sub>). (b) Energy profile for ethane formation including the C*–CH* coupling steps. (c) Key steps of the calculated reaction mechanism on 2D-Mo₂C with selected transition states and intermediates. Energies are referenced against the sum of the reactants' energy (4 CO and 3 H₂) and the catalytic surface in eV (*G*<sub>rel</sub>). The pathway connecting intermediates 1 and 4 is repeated also between intermediates 7 and 8.</figcaption></figure>

Mo₂C using DFT calculations and map out the most likely FT reaction pathway.

## ■ DFT STUDY

**Model Surface.** For our DFT model, we used a fully defunctionalized surface of 2D-Mo₂C (i.e., absence of any O*) species as a representative model of the Mo₂CT<sub>x-400</sub> catalyst in the steady state, to calculate the Gibbs energy profile and obtain mechanistic insights. As discussed above, the choice of this model is consistent with the presence of only carbidic Mo in the Mo 3d XPS spectrum of active Mo₂CT<sub>x-500-TOS2h</sub>, as well as the lack of peaks due to CO* species in the C 1s XPS region, which excludes the presence of a CO* adlayer. The model corresponds to the Mo₂C (0001) surface and consists of two exterior Mo layers and a central carbon layer sandwiched by two Mo layers.<sup>56,60</sup> First, we examined the adsorption of carbon, hydrogen, and oxygen on the 3-fold hollow, bridge, and on-top sites (Figure 4a and Figure S17). The adsorption energies and reference energies are given in Table S6. The DFT results show that H* and C* adsorb preferentially on 3-fold hollow sites above a Mo atom (denoted *H*<sub>Mo</sub>, Figure 4a), whereas O* adsorbs preferentially on 3-fold hollow sites above a C atom (denoted *H*<sub>C</sub>, Figure 4a). The calculated Gibbs energy profiles and snapshots of selected transition states for ethane formation are shown in Figure 4b and c, respectively.

**Dissociation of CO and H₂ and O* Removal.** Adsorption of carbon monoxide on a *H*<sub>Mo</sub> site is exergonic by 1.07 eV. CO binds via carbon in a µ<sub>3</sub>-η<sup>1</sup> fashion orthogonal to the surface. This interaction weakens the C–O bond that elongates by 0.05 Å, consistent with a decrease in the calculated stretching frequency from 2129 to 1670 cm<sup>-1</sup> owing to π-back-donation and rehybridization of CO.<sup>61</sup> In the unassisted dissociation pathway, CO* species 1 tilts toward the surface and forms C* and O* species in vicinal 3-fold hollow sites (*H*<sub>Mo</sub> and *H*<sub>C</sub>, respectively; Figure S18). This state is denoted 2 (Figure S19). The associated transition state TS1 has a Gibbs energy barrier of 1.51 eV. The direct CO dissociation step is exergonic by 1.02 eV, which is similar to

the values reported for the (100) surface of β-Mo₂C.<sup>35</sup> The dissociative chemisorption of H₂ on the 2D-Mo₂C surface starts from a physisorbed state with a shallow minimum of –20 meV and proceeds to dissociated H₂ via a small energy barrier (0.15 eV).<sup>62,63</sup> In this process, the distance from the surface to the center-of-mass of H₂ decreases from 3.1 to 1.4 Å while *d*<sub>H-H</sub> increases from 0.74 to 3.03 Å (two H*), corresponding to the distance between two adjacent *H*<sub>Mo</sub> sites. The Gibbs energy barrier for the recombination of C* and O* species on 2D-Mo₂C is 2.53 eV, which is considerably higher than the Gibbs energy barrier for the hydrogenation of C* to CH* (0.90 eV), indicating that the direct dissociation of CO* is essentially irreversible in our reaction conditions (330 °C and 25 bar).

Next, we evaluated the energetics of the H₂-assisted pathways for CO activation and they were found to be less favorable than TS1, owing to the higher energy barriers of 1.77 and 2.18 eV for the formyl and hydroxycarbonyl routes, respectively (Figure S19). Further details on the H₂-assisted pathways are discussed in the Supporting Information. The O* species formed via the direct dissociation of CO* can be removed as CO₂ through its reaction with CO* or as H₂O via the reaction with 2H*. The formation of CO₂ requires CO* to adopt a distorted µ<sup>3</sup>-η<sup>2</sup> coordination in the intermediate 3, located at –3.35 eV with respect to initial reactants. In the transition state TS2, O* migrates from a vicinal *H*<sub>C</sub> site atop the intersecting Mo atom (that is, the Mo atom that separates the *H*<sub>Mo</sub> and *H*<sub>C</sub> sites, Figure S18) with a barrier of 2.05 eV. In the product, the C atom of CO₂* is on a bridge position and the O atoms are located on top positions (atop) of adjacent Mo atoms (4). The Gibbs desorption energy of a CO₂ molecule under reaction conditions is 0.44 eV. Therefore, the Gibbs energy required to remove O* through a reaction with CO* (intermediate 3) and regenerate the active site is 2.02 eV. The removal of O* species via the hydrogenation of a hydroxyl yielding water has a barrier of 2.56 eV and is, therefore, less favorable. O* removal via proton transfer between neighboring hydroxyls has an even higher energy barrier of 2.66 eV. These kinetically less favorable routes are
<figure><img src="image_12.png" /><figcaption>**Figure 4.** (a) Top and side views of the 2D-Mo₂C DFT model showing 3-fold hollow sites over a Mo atom (*H*<sub>Mo</sub>) and over a carbon atom (*H*<sub>C</sub>). (b) Energy profile for ethane formation including the C*–CH* coupling steps. (c) Key steps of the calculated reaction mechanism on 2D-Mo₂C with selected transition states and intermediates. Energies are referenced against the sum of the reactants' energy (4 CO and 3 H₂) and the catalytic surface in eV (*G*<sub>rel</sub>). The pathway connecting intermediates 1 and 4 is repeated also between intermediates 7 and 8.</figcaption></figure>

Mo₂C using DFT calculations and map out the most likely FT reaction pathway.

## DFT STUDY

**Model Surface.** For our DFT model, we used a fully defunctionalized surface of 2D-Mo₂C (i.e., absence of any O*) species as a representative model of the Mo₂CT<sub>x-400</sub> catalyst in the steady state, to calculate the Gibbs energy profile and obtain mechanistic insights. As discussed above, the choice of this model is consistent with the presence of only carbidic Mo in the Mo 3d XPS spectrum of active Mo₂CT<sub>x-500-TOS2h</sub>, as well as the lack of peaks due to CO* species in the C 1s XPS region, which excludes the presence of a CO* adlayer. The model corresponds to the Mo₂C (0001) surface and consists of two exterior Mo layers and a central carbon layer sandwiched by two Mo layers.<sup>56,60</sup> First, we examined the adsorption of carbon, hydrogen, and oxygen on the 3-fold hollow, bridge, and on-top sites (Figure 4a and Figure S17). The adsorption energies and reference energies are given in Table S6. The DFT results show that H* and C* adsorb preferentially on 3-fold hollow sites above a Mo atom (denoted *H*<sub>Mo</sub>, Figure 4a), whereas O* adsorbs preferentially on 3-fold hollow sites above a C atom (denoted *H*<sub>C</sub>, Figure 4a). The calculated Gibbs energy profiles and snapshots of selected transition states for ethane formation are shown in Figure 4b and c, respectively.

**Dissociation of CO and H₂ and O* Removal.** Adsorption of carbon monoxide on a *H*<sub>Mo</sub> site is exergonic by 1.07 eV. CO binds via carbon in a μ<sub>3</sub>-η<sup>1</sup> fashion orthogonal to the surface. This interaction weakens the C–O bond that elongates by 0.05 Å, consistent with a decrease in the calculated stretching frequency from 2129 to 1670 cm<sup>-1</sup> owing to π-back-donation and rehybridization of CO.<sup>61</sup> In the unassisted dissociation pathway, CO* species 1 tilts toward the surface and forms C* and O* species in vicinal 3-fold hollow sites (*H*<sub>Mo</sub> and *H*<sub>C</sub>, respectively; Figure S18). This state is denoted 2 (Figure S19). The associated transition state TS1 has a Gibbs energy barrier of 1.51 eV. The direct CO dissociation step is exergonic by 1.02 eV, which is similar to

the values reported for the (100) surface of β-Mo₂C.<sup>35</sup> The dissociative chemisorption of H₂ on the 2D-Mo₂C surface starts from a physisorbed state with a shallow minimum of –20 meV and proceeds to dissociated H₂ via a small energy barrier (0.15 eV).<sup>62,63</sup> In this process, the distance from the surface to the center-of-mass of H₂ decreases from 3.1 to 1.4 Å while *d*<sub>H-H</sub> increases from 0.74 to 3.03 Å (two H*), corresponding to the distance between two adjacent *H*<sub>Mo</sub> sites. The Gibbs energy barrier for the recombination of C* and O* species on 2D-Mo₂C is 2.53 eV, which is considerably higher than the Gibbs energy barrier for the hydrogenation of C* to CH* (0.90 eV), indicating that the direct dissociation of CO* is essentially irreversible in our reaction conditions (330 °C and 25 bar).

Next, we evaluated the energetics of the H₂-assisted pathways for CO activation and they were found to be less favorable than TS1, owing to the higher energy barriers of 1.77 and 2.18 eV for the formyl and hydroxycarbonyl routes, respectively (Figure S19). Further details on the H₂-assisted pathways are discussed in the Supporting Information. The O* species formed via the direct dissociation of CO* can be removed as CO₂ through its reaction with CO* or as H₂O via the reaction with 2H*. The formation of CO₂ requires CO* to adopt a distorted μ<sup>3</sup>-η<sup>2</sup> coordination in the intermediate 3, located at –3.35 eV with respect to initial reactants. In the transition state TS2, O* migrates from a vicinal *H*<sub>C</sub> site atop the intersecting Mo atom (that is, the Mo atom that separates the *H*<sub>Mo</sub> and *H*<sub>C</sub> sites, Figure S18) with a barrier of 2.05 eV. In the product, the C atom of CO₂* is on a bridge position and the O atoms are located on top positions (atop) of adjacent Mo atoms (4). The Gibbs desorption energy of a CO₂ molecule under reaction conditions is 0.44 eV. Therefore, the Gibbs energy required to remove O* through a reaction with CO* (intermediate 3) and regenerate the active site is 2.02 eV. The removal of O* species via the hydrogenation of a hydroxyl yielding water has a barrier of 2.56 eV and is, therefore, less favorable. O* removal via proton transfer between neighboring hydroxyls has an even higher energy barrier of 2.66 eV. These kinetically less favorable routes are
endergonic by 2.15 eV and are discussed in detail in the SI (Figure S20).

**C–C Coupling and Hydrogenation.** Subsequently, we calculated the energetics of the potential C–C coupling and hydrogenation steps for ethane formation to investigate the chain growth mechanism. The calculated Gibbs energies are given in Table S4, and the optimized geometries of the initial, transition, and final states are presented in Figures S21–S24. Figure S25 shows the Gibbs energy of the respective energy barriers plotted against the Gibbs reaction energy for the elementary steps. Generally, hydrogenation steps have lower activation barriers to form CₓHᵧ species with larger y. In contrast, the C–C coupling steps have lower activation barriers for lower y with one exception that is the coupling between two C\* species, which has an energy barrier of 1.43 eV, higher than the coupling barrier between C\* and CH\* (1.20 eV). The average barrier for the hydrogenation of various CₓHᵧ species via reactions presented in Table S4 (reactions 19–34) is ca. 1.00 (±0.29) eV. Therefore, since the hydrogenation of CₓHᵧ\* involves lower barriers than the one calculated for the H\*-assisted activation of CO\* (1.77 and 2.18 eV for the formyl and hydroxycarbonyl routes, respectively), H\* will be consumed preferentially through the hydrogenation of CₓHᵧ\* rather than through the H-assisted activation of CO\*. The average barrier for C–C coupling, presented in Table S4 (reactions 10–18), is ca. 1.35 (±0.22) eV, i.e., higher than the average barrier for the hydrogenation of CₓHᵧ\* species. However, although the coupling of two CH\* species (14 in Figure S26) is energetically favored, with the lowest Gibbs energy barrier of 0.85 eV among the possible coupling steps, the high bonding energy of CHCH\* species to the surface (−2.75 eV) leads to a high Gibbs energy barrier of 1.41 eV (TS11) for transferring H\* to convert CHCH\* into CHCH₂\* (16 in Figure S26). The high energy barrier to form CHCH₂\* and consequently also CH₂CH₂\* species is consistent with the absence of ethene in the experimental product distribution.

An alternative FT pathway involves the coupling between two CH\* species and the H\*-assisted transformation of acetylene to ethylidyne (i.e., ≡CCH₃\*).⁶⁴ In this alkylidyne mechanism, H\* adsorbed on an *H*<sub>C</sub> site in close proximity to the bound acetylene (15 in Figure S27), induces a hydrogen transfer from one CH group of acetylene to another. The barrier for this process is 2.26 eV (TS24 in Figure S27). The formed vinylidene (i.e., =C=CH₂\*) species features the sp carbon residing over an *H*<sub>Mo</sub> site and the methylenedene fragment over a Mo atom. At this point, the transfer of H\* from the *H*<sub>C</sub> site to the Mo atom interacting with the methylenedene fragment converts the =C=CH₂\* species to ≡CCH₃\* (11 in Figure S27). Overall, this alternative route is not only associated with a high barrier (i.e., it is kinetically unfavorable) but also endergonic by 1.24 eV and is therefore an unlikely FT pathway on 2D-Mo₂C.

The C–C coupling route with the second lowest barrier occurs between C\* and CH\* species (8, Figure 4). Between states 7 (that corresponds to methylidyne, CH\*) and 8 in Figure 4, states 1 to 4 are repeated to account for the deposition of an additional C\* on the surface. This step involves the migration of C\* and CH\* species from vicinal *H*<sub>Mo</sub> sites to a bridge position, via a TS4 with an energy barrier of 1.20 eV, forming CCH\* (9). The CCH\* species adsorbs parallel to the surface, and the H atom of CCH\* does not interact with the surface. The barrier for adding adsorbed H\*

species to CCH\* yielding CCH₂\* is 0.98 eV (TS5), i.e., 0.43 eV, lower than for the hydrogenation of CCH\* to give CHCH\* species. This low energy barrier suggests that ethane formation occurs on 2D-Mo₂C via the CCH\* and CCH₂\* intermediates. The hydrogenation of CCH\* species proceeds in the bridge position, such that the C–C axis of the resulting CCH₂\* is nearly parallel to the surface (10). Adding a third H\* to CCH₂\* to form CCH₃\* requires a reorientation of the molecular axis of CCH₂\* toward a configuration orthogonal to the surface with the hydrogenated C on top of a Mo atom and the bare C still over an *H*<sub>C</sub> site. In the transition state (TS6), the H–C–H angle (as seen from above, Figure S23) decreases from ca. 180° to ca. 120°, with an energy cost of 0.70 eV. After H\* addition, only one of the H atoms of the formed ethylidyne interacts with the Mo atom in intermediate 11, as seen from the significant elongation of the C–H bond of the interacting atom (1.18 Å) compared to the other two C–H bonds (1.09 Å).

No notable geometrical change occurs, while a further hydrogen migrates from an *H*<sub>Mo</sub> site over a Mo atom to yield the CHCH₃\* species, associated with an energy barrier of 0.75 eV (TS7). In the CHCH₃\* species, the methine hydrogen interacts with one of the two remaining vicinal Mo atoms. Adding a further H\* to CHCH₃\* to form CH₂CH₃\* via TS8 has a Gibbs energy barrier of 0.81 eV and preserves the geometry of the CHCH₃\* species. Both H atoms of the CH₂ group interact with Mo atoms (intermediate 12). For the final hydrogenation step, this interaction breaks such that only one H of CH₂ interacts with the surface (intermediate 13). In the transition state TS9 (1.28 eV), the methylene carbon decoordinates from the 3-fold hollow site and moves atop the neighboring Mo atom while the H–C–H angle decreases from 180 to 120° (Figure S23). The hydrogenation of the CH₂CH₃\* species to ethane has a Gibbs energy barrier equal to 1.28 eV (TS9), which is lower than the barrier to form CH₄ from CH₃\* species (1.57 eV, Figure S28). Note that the energetic cost to form CH₄ from CH₃\* also exceeds the average barrier for the C–C coupling steps discussed above. Therefore, our DFT results suggest that chain propagation is favored over methanation, in agreement with the experimental observations.

Lastly, to provide a rationale for the lower CO conversion rate of Mo₂CTₓ₄₀₀–TOS₁h relative to Mo₂CTₓ₄₀₀–TOS₈h (i.e., prior to and after *in situ* activation), we considered a 2D-Mo₂C-0.67 O ML model and calculated also for this model the key elementary steps identified for the 2D-Mo₂C model (*vide supra*). Results show that the lower activity of the surface with 0.67 O\* ML compared to the pristine surface can be attributed to the significantly higher barrier for the dissociation of CO on 2D-Mo₂C-0.67 O ML relative to 2D-Mo₂C. Further details and results for the 2D-Mo₂C-0.67 O ML model are provided in the SI (Table S5 and Figure S29).

## DISCUSSION

Since the first catalytic applications of Mo₂C, its reactivity was generally compared to that of Ru.⁶⁵ More recently, it has been reported that the adsorption energies of C-containing intermediates on the Mo-terminated (100) surface of 3D-Mo₂C are indeed similar to that of Ru (in particular the (211) surface).³⁵ However, the adsorption energies of O-containing intermediates on the β-Mo₂C (100) surface are significantly
endergonic by 2.15 eV and are discussed in detail in the SI (Figure S20).

**C–C Coupling and Hydrogenation.** Subsequently, we calculated the energetics of the potential C–C coupling and hydrogenation steps for ethane formation to investigate the chain growth mechanism. The calculated Gibbs energies are given in Table S4, and the optimized geometries of the initial, transition, and final states are presented in Figures S21–S24. Figure S25 shows the Gibbs energy of the respective energy barriers plotted against the Gibbs reaction energy for the elementary steps. Generally, hydrogenation steps have lower activation barriers to form CₓHᵧ species with larger y. In contrast, the C–C coupling steps have lower activation barriers for lower y with one exception that is the coupling between two C\* species, which has an energy barrier of 1.43 eV, higher than the coupling barrier between C\* and CH\* (1.20 eV). The average barrier for the hydrogenation of various CₓHᵧ species via reactions presented in Table S4 (reactions 19–34) is ca. 1.00 (±0.29) eV. Therefore, since the hydrogenation of CₓHᵧ\* involves lower barriers than the one calculated for the H\*-assisted activation of CO\* (1.77 and 2.18 eV for the formyl and hydroxycarbonyl routes, respectively), H\* will be consumed preferentially through the hydrogenation of CₓHᵧ\* rather than through the H-assisted activation of CO\*. The average barrier for C–C coupling, presented in Table S4 (reactions 10–18), is ca. 1.35 (±0.22) eV, i.e., higher than the average barrier for the hydrogenation of CₓHᵧ\* species. However, although the coupling of two CH\* species (14 in Figure S26) is energetically favored, with the lowest Gibbs energy barrier of 0.85 eV among the possible coupling steps, the high bonding energy of CHCH\* species to the surface (−2.75 eV) leads to a high Gibbs energy barrier of 1.41 eV (TS11) for transferring H\* to convert CHCH\* into CHCH₂\* (16 in Figure S26). The high energy barrier to form CHCH₂\* and consequently also CH₂CH₂\* species is consistent with the absence of ethene in the experimental product distribution.

An alternative FT pathway involves the coupling between two CH\* species and the H\*-assisted transformation of acetylene to ethylidyne (i.e., ≡CCH₃\*).⁶⁴ In this alkylidyne mechanism, H\* adsorbed on an *H*<sub>C</sub> site in close proximity to the bound acetylene (15 in Figure S27), induces a hydrogen transfer from one CH group of acetylene to another. The barrier for this process is 2.26 eV (TS24 in Figure S27). The formed vinylidene (i.e., =C=CH₂\*) species features the sp carbon residing over an *H*<sub>Mo</sub> site and the methylenedene fragment over a Mo atom. At this point, the transfer of H\* from the *H*<sub>C</sub> site to the Mo atom interacting with the methylenedene fragment converts the =C=CH₂\* species to ≡CCH₃\* (11 in Figure S27). Overall, this alternative route is not only associated with a high barrier (i.e., it is kinetically unfavorable) but also endergonic by 1.24 eV and is therefore an unlikely FT pathway on 2D-Mo₂C.

The C–C coupling route with the second lowest barrier occurs between C\* and CH\* species (8, Figure 4). Between states 7 (that corresponds to methylidyne, CH\*) and 8 in Figure 4, states 1 to 4 are repeated to account for the deposition of an additional C\* on the surface. This step involves the migration of C\* and CH\* species from vicinal *H*<sub>Mo</sub> sites to a bridge position, via a TS4 with an energy barrier of 1.20 eV, forming CCH\* (9). The CCH\* species adsorbs parallel to the surface, and the H atom of CCH\* does not interact with the surface. The barrier for adding adsorbed H\*

species to CCH\* yielding CCH₂\* is 0.98 eV (TS5), i.e., 0.43 eV, lower than for the hydrogenation of CCH\* to give CHCH\* species. This low energy barrier suggests that ethane formation occurs on 2D-Mo₂C via the CCH\* and CCH₂\* intermediates. The hydrogenation of CCH\* species proceeds in the bridge position, such that the C–C axis of the resulting CCH₂\* is nearly parallel to the surface (10). Adding a third H\* to CCH₂\* to form CCH₃\* requires a reorientation of the molecular axis of CCH₂\* toward a configuration orthogonal to the surface with the hydrogenated C on top of a Mo atom and the bare C still over an *H*<sub>C</sub> site. In the transition state (TS6), the H–C–H angle (as seen from above, Figure S23) decreases from ca. 180° to ca. 120°, with an energy cost of 0.70 eV. After H\* addition, only one of the H atoms of the formed ethylidyne interacts with the Mo atom in intermediate 11, as seen from the significant elongation of the C–H bond of the interacting atom (1.18 Å) compared to the other two C–H bonds (1.09 Å).

No notable geometrical change occurs, while a further hydrogen migrates from an *H*<sub>Mo</sub> site over a Mo atom to yield the CHCH₃\* species, associated with an energy barrier of 0.75 eV (TS7). In the CHCH₃\* species, the methine hydrogen interacts with one of the two remaining vicinal Mo atoms. Adding a further H\* to CHCH₃\* to form CH₂CH₃\* via TS8 has a Gibbs energy barrier of 0.81 eV and preserves the geometry of the CHCH₃\* species. Both H atoms of the CH₂ group interact with Mo atoms (intermediate 12). For the final hydrogenation step, this interaction breaks such that only one H of CH₂ interacts with the surface (intermediate 13). In the transition state TS9 (1.28 eV), the methylene carbon decoordinates from the 3-fold hollow site and moves atop the neighboring Mo atom while the H–C–H angle decreases from 180 to 120° (Figure S23). The hydrogenation of the CH₂CH₃\* species to ethane has a Gibbs energy barrier equal to 1.28 eV (TS9), which is lower than the barrier to form CH₄ from CH₃\* species (1.57 eV, Figure S28). Note that the energetic cost to form CH₄ from CH₃\* also exceeds the average barrier for the C–C coupling steps discussed above. Therefore, our DFT results suggest that chain propagation is favored over methanation, in agreement with the experimental observations.

Lastly, to provide a rationale for the lower CO conversion rate of Mo₂CT<sub>x-400-TOS<sub>8h</sub></sub> relative to Mo₂CT<sub>x-400-TOS<sub>8h</sub></sub> (i.e., prior to and after *in situ* activation), we considered a 2D-Mo₂C-0.67 O ML model and calculated also for this model the elementary steps identified for the 2D-Mo₂C model (*vide supra*). Results show that the lower activity of the surface with 0.67 O\* ML compared to the pristine surface can be attributed to the significantly higher barrier for the dissociation of CO on 2D-Mo₂C-0.67 O ML relative to 2D-Mo₂C. Further details and results for the 2D-Mo₂C-0.67 O ML model are provided in the SI (Table S5 and Figure S29).

## DISCUSSION

Since the first catalytic applications of Mo₂C, its reactivity was generally compared to that of Ru.⁶⁵ More recently, it has been reported that the adsorption energies of C-containing intermediates on the Mo-terminated (100) surface of 3D-Mo₂C are indeed similar to that of Ru (in particular the (211) surface).³⁵ However, the adsorption energies of O-containing intermediates on the β-Mo₂C (100) surface are significantly
higher (i.e., more negative) due to the oxophilicity of Mo.³⁵
Interestingly, DFT studies of Ru surfaces have shown that in
the absence of a dense CO* adlayer, CO* undergoes a direct
dissociation to C* and O* species on stepped sites.⁶⁶⁻⁶⁸ DFT
results presented here also suggest the direct dissociation of
CO on the 2D-Mo₂C surface in the absence of a CO* adlayer,
showing further similarities with Ru surfaces.

Our DFT calculations identify notable differences between
the reaction barriers and the stability of intermediates on 2D-
Mo₂C and those reported for 3D-Mo₂C. For instance, on 3D-
Mo₂C, it has been suggested that the H-assisted CO
dissociation pathway prevails. In this route, HCO* is formed
first, which subsequently dissociates into CH* and O*. The
formation of the HCO* intermediate was associated with a low
barrier for different facets of 3D-Mo₂C (energies ranging from
0.12 to 0.36 eV; note that these reported energies are total
energy or electronic energy with a zero-point-energy
correction),⁶⁹,⁷⁰ compared to 1.04 eV for the 2D-Mo₂C
(0001) surface. Furthermore, the formation of HCO* is
strongly endergonic for 2D-Mo₂C (1.04 eV) and can vary from
exergonic (−0.32 eV) to mildly endergonic (0.13 eV) on 3D-
Mo₂C.⁶⁹,⁷⁰ Therefore, the hydrogenation of CO* to HCO* is
both kinetically and thermodynamically less favorable on 2D-
Mo₂C than on surfaces of 3D-Mo₂C. The high endothermicity
of steps associated with the formation of HCO* and COH*
intermediates (1.04 and 1.17 eV, respectively) on the 2D-
Mo₂C (0001) surface is generally consistent with the absence
of oxygenates in the reaction products, suggesting the
prevalence of the carbidic chain growth mechanism.

The O* removal from the 2D-Mo₂C (0001) surface is endergonic, with barriers as high as ca. 2 and 2.7 eV for CO₂ and H₂O, respectively, owing to the high Mo–O bond strength.⁷¹⁻⁷⁴ In contrast to the desorption of H₂O, steps associated with the dissociation of hydrogenated oxygen-containing species (OH* and H₂O*) have lower energy barriers, that is, reactions OH* → O* + H* and H₂O → OH* + H* proceed via transition states that are only 0.98 and 0.77 eV high, respectively. This indicates that the dissociation of hydrogenated oxygen-containing species occurs faster than the removal of water (assuming similar pre-exponential factors). Remembering that H* has lower barriers for its reaction with C-containing species than with O* or OH* species (Figure S20), one can conclude that CO₂ is the preferred oxygenate product, which agrees well with the high experimental CO₂ selectivity. A high rate of CO₂ formation on 2D-Mo₂C indicates a high activity for the water gas shift reaction. Interestingly, WGS occurs in FT conditions already at 330 °C, a significantly lower temperature than previously observed for Mo₂CTₓ (ca. 450–500 °C).⁴⁹ This is explained by the fully functionalized surface of Mo₂CTₓ in WGS conditions and a (fully) defunctionalized surface under FT conditions.³²

In conclusion, a MXene-derived 2D-Mo₂C-based catalyst,
prepared via *in situ* activation under FT conditions, enables the
hydrogenation of CO to higher alkanes with a chain growth
probability coefficient α of 0.87. The value of α is ca. two times
higher than reported previously for other molybdenum
carbides. The CO conversion rate of MXene-based catalysts
depends strongly on the extent of defunctionalization of the
surface passivating groups (Tₓ) such that fully defunctionalized
2D-Mo₂C and 2D-Mo₂C₁₋ₓ catalysts show notably higher
gravimetric CO conversion rates relative to only a partially
defunctionalized catalyst (i.e., initial Mo₂CTₓ₋₄₀₀). However,
the gravimetric CO consumption rates of 2D catalysts are

significantly higher, for both fully and partially defunctionalized
catalysts, relative to a reference 3D β-Mo₂C₄₀₀, underlining a
yet unharnessed potential of 2D materials such as MXenes in
heterogeneous catalysis. In the FT synthesis conditions used
here, the partially defunctionalized catalyst Mo₂CTₓ₋₄₀₀
undergoes a strong *in situ* activation explained by the reductive
defunctionalization of the Tₓ groups in Mo₂CTₓ₋₄₀₀ to form a
2D-Mo₂C state. Progressive defunctionalization of Mo₂CTₓ₋₄₀₀
leads also to an increase in the WGS activity (evidenced by a
higher CO₂ selectivity). The concomitant increase in CO
conversion leads to an overall higher hydrocarbon productivity,
in particular for C₅⁺ products. H₂ pretreatment at 500 °C does
not only fully defunctionalize the passivating Tₓ groups in
Mo₂CTₓ but also partly removes carbidic carbon of Mo₂CTₓ
yielding a 2D-Mo₂C₁₋ₓ catalyst active in CO methanation. In
contrast, a 2D-Mo₂C catalyst prepared via the *in situ* activation
of Mo₂CTₓ₋₄₀₀ does not feature a depleted content of carbidic
carbon and is selective in FT. DFT calculations identified
feasible energy profiles for the chain growth mechanism on a
2D-Mo₂C (0001) surface under reaction conditions and in the
absence of a CO adlayer. In particular, according to DFT
results, CO directly dissociates into C* and O*, consistent
with the absence of oxygenate products (beyond CO₂). The
high barrier for the hydrogenation of CH₃* species to methane
relative to the lower chain growth barrier explains the
formation of higher alkanes. Oxygen removal is the rate-
limiting step, owing to the high oxophilicity of the carbidic
surface, with CO₂ being the major reaction product (WGS
reaction).

ASSOCIATED CONTENT

**Supporting Information**

The Supporting Information is available free of charge at
https://pubs.acs.org/doi/10.1021/acscatal.3c03956.

Experimental procedures, characterization, computa-
tional details, additional computational results, XPS
and Raman spectra, TPD and CO chemisorption results,
XRD diffractograms, and catalytic results (PDF)

AUTHOR INFORMATION

**Corresponding Authors**

Vitaly V. Ordomsky — University of Lille, CNRS, Centrale
Lille, University of Artois, UMR 8181 — UCCS — Unité de
Catalyse et Chimie du Solide, Lille 59000, France;

● orcid.org/0000-0002-4814-5052;

Email: *vitaly.ordomsky@univ-lille.fr*

Aleix Comas-Vives — Institute of Materials Chemistry,

Technische Universität Wien, Vienna 1060, Austria;

Departament de Química, Universitat Autònoma de
Barcelona, Cerdanyola del Valles 08193 Catalonia, Spain;

● orcid.org/0000-0002-7002-1582; Email: aleix.comas@tuwien.ac.at, aleix.comas@uab.cat

Alexey Fedorov — Department of Mechanical and Process
Engineering, ETH Zürich, Zürich CH-8092, Switzerland;

● orcid.org/0000-0001-9814-6726; Email: fedoroal@ethz.ch

Authors

Evgenia Kountoupi — Department of Mechanical and Process Engineering, ETH Zürich, Zürich CH-8092, Switzerland;

● orcid.org/0000-0002-7766-6172
higher (i.e., more negative) due to the oxophilicity of Mo.³⁵
Interestingly, DFT studies of Ru surfaces have shown that in
the absence of a dense CO* adlayer, CO* undergoes a direct
dissociation to C* and O* species on stepped sites.⁶⁶⁻⁶⁸ DFT
results presented here also suggest the direct dissociation of
CO on the 2D-Mo₂C surface in the absence of a CO* adlayer,
showing further similarities with Ru surfaces.

Our DFT calculations identify notable differences between
the reaction barriers and the stability of intermediates on 2D-
Mo₂C and those reported for 3D-Mo₂C. For instance, on 3D-
Mo₂C, it has been suggested that the H-assisted CO
dissociation pathway prevails. In this route, HCO* is formed
first, which subsequently dissociates into CH* and O*. The
formation of the HCO* intermediate was associated with a low
barrier for different facets of 3D-Mo₂C (energies ranging from
0.12 to 0.36 eV; note that these reported energies are total
energy or electronic energy with a zero-point-energy
correction),⁶⁹,⁷⁰ compared to 1.04 eV for the 2D-Mo₂C
(0001) surface. Furthermore, the formation of HCO* is
strongly endergonic for 2D-Mo₂C (1.04 eV) and can vary from
exergonic (−0.32 eV) to mildly endergonic (0.13 eV) on 3D-
Mo₂C.⁶⁹,⁷⁰ Therefore, the hydrogenation of CO* to HCO* is
both kinetically and thermodynamically less favorable on 2D-
Mo₂C than on surfaces of 3D-Mo₂C. The high endothermicity
of steps associated with the formation of HCO* and COH*
intermediates (1.04 and 1.17 eV, respectively) on the 2D-
Mo₂C (0001) surface is generally consistent with the absence
of oxygenates in the reaction products, suggesting the
prevalence of the carbidic chain growth mechanism.

The O* removal from the 2D-Mo₂C (0001) surface is endergonic, with barriers as high as ca. 2 and 2.7 eV for CO₂ and H₂O, respectively, owing to the high Mo–O bond strength.⁷¹⁻⁷⁴ In contrast to the desorption of H₂O, steps associated with the dissociation of hydrogenated oxygen-containing species (OH* and H₂O*) have lower energy barriers, that is, reactions OH* → O* + H* and H₂O → OH* + H* proceed via transition states that are only 0.98 and 0.77 eV high, respectively. This indicates that the dissociation of hydrogenated oxygen-containing species occurs faster than the removal of water (assuming similar pre-exponential factors). Remembering that H* has lower barriers for its reaction with C-containing species than with O* or OH* species (Figure S20), one can conclude that CO₂ is the preferred oxygenate product, which agrees well with the high experimental CO₂ selectivity. A high rate of CO₂ formation on 2D-Mo₂C indicates a high activity for the water gas shift reaction. Interestingly, WGS occurs in FT conditions already at 330 °C, a significantly lower temperature than previously observed for Mo₂CTₓ (ca. 450–500 °C).⁴⁹ This is explained by the fully functionalized surface of Mo₂CTₓ in WGS conditions and a (fully) defunctionalized surface under FT conditions.³²

In conclusion, a MXene-derived 2D-Mo₂C-based catalyst,
prepared via *in situ* activation under FT conditions, enables the
hydrogenation of CO to higher alkanes with a chain growth
probability coefficient α of 0.87. The value of α is ca. two times
higher than reported previously for other molybdenum
carbides. The CO conversion rate of MXene-based catalysts
depends strongly on the extent of defunctionalization of the
surface passivating groups (Tₓ) such that fully defunctionalized
2D-Mo₂C and 2D-Mo₂C₁₋ₓ catalysts show notably higher
gravimetric CO conversion rates relative to only a partially
defunctionalized catalyst (i.e., initial Mo₂CTₓ₋₄₀₀). However,
the gravimetric CO consumption rates of 2D catalysts are

significantly higher, for both fully and partially defunctionalized
catalysts, relative to a reference 3D β-Mo₂C₄₀₀, underlining a
yet unharnessed potential of 2D materials such as MXenes in
heterogeneous catalysis. In the FT synthesis conditions used
here, the partially defunctionalized catalyst Mo₂CTₓ₋₄₀₀
undergoes a strong *in situ* activation explained by the reductive
defunctionalization of the Tₓ groups in Mo₂CTₓ₋₄₀₀ to form a
2D-Mo₂C state. Progressive defunctionalization of Mo₂CTₓ₋₄₀₀
leads also to an increase in the WGS activity (evidenced by a
higher CO₂ selectivity). The concomitant increase in CO
conversion leads to an overall higher hydrocarbon productivity,
in particular for C₅⁺ products. H₂ pretreatment at 500 °C does
not only fully defunctionalize the passivating Tₓ groups in
Mo₂CTₓ but also partly removes carbidic carbon of Mo₂CTₓ
yielding a 2D-Mo₂C₁₋ₓ catalyst active in CO methanation. In
contrast, a 2D-Mo₂C catalyst prepared via the *in situ* activation
of Mo₂CTₓ₋₄₀₀ does not feature a depleted content of carbidic
carbon and is selective in FT. DFT calculations identified
feasible energy profiles for the chain growth mechanism on a
2D-Mo₂C (0001) surface under reaction conditions and in the
absence of a CO adlayer. In particular, according to DFT
results, CO directly dissociates into C* and O*, consistent
with the absence of oxygenate products (beyond CO₂). The
high barrier for the hydrogenation of CH₃* species to methane
relative to the lower chain growth barrier explains the
formation of higher alkanes. Oxygen removal is the rate-
limiting step, owing to the high oxophilicity of the carbidic
surface, with CO₂ being the major reaction product (WGS
reaction).

ASSOCIATED CONTENT

**Supporting Information**

The Supporting Information is available free of charge at
https://pubs.acs.org/doi/10.1021/acscatal.3c03956.

Experimental procedures, characterization, computa-
tional details, additional computational results, XPS
and Raman spectra, TPD and CO chemisorption results,
XRD diffractograms, and catalytic results (PDF)

AUTHOR INFORMATION

**Corresponding Authors**

Vitaly V. Ordomsky — University of Lille, CNRS, Centrale
Lille, University of Artois, UMR 8181 — UCCS — Unité de
Catalyse et Chimie du Solide, Lille 59000, France;

● orcid.org/0000-0002-4814-5052;

Email: *vitaly.ordomsky@univ-lille.fr*

Aleix Comas-Vives — Institute of Materials Chemistry,

Technische Universität Wien, Vienna 1060, Austria;

Departament de Química, Universitat Autònoma de
Barcelona, Cerdanyola del Valles 08193 Catalonia, Spain;

● orcid.org/0000-0002-7002-1582; Email: aleix.comas@tuwien.ac.at, aleix.comas@uab.cat

Alexey Fedorov — Department of Mechanical and Process
Engineering, ETH Zürich, Zürich CH-8092, Switzerland;

● orcid.org/0000-0001-9814-6726; Email: fedoroal@ethz.ch

Authors

Evgenia Kountoupi — Department of Mechanical and Process Engineering, ETH Zürich, Zürich CH-8092, Switzerland;

● orcid.org/0000-0002-7766-6172
Alan J. Barrios – University of Lille, CNRS, Centrale Lille, University of Artois, UMR 8181 – UCCS – Unité de Catalyse et Chimie du Solide, Lille 59000, France; Laboratory for Chemical Technology, Department of Materials, Textiles and Chemical Engineering, Ghent University, Ghent B-9052, Belgium

Zixuan Chen – Department of Mechanical and Process Engineering, ETH Zürich, Zürich CH-8092, Switzerland;

orcid.org/0000-0002-3882-3016

Christoph R. Müller – Department of Mechanical and Process Engineering, ETH Zürich, Zürich CH-8092, Switzerland;

orcid.org/0000-0003-2234-6902

Complete contact information is available at:
https://pubs.acs.org/10.1021/acscatal.3c03956

## Notes

The authors declare no competing financial interest.

## ACKNOWLEDGMENTS

This work was supported by ETH Zürich through a doctoral fellowship to E.K. (ETH-40 19-2) and Z.C. (ETH-40 17-2). We are grateful to Scientific Centre for Optical and Electron Microscopy (ScopeM, ETH Zürich) for providing access to electron microscopy facilities. We thank Prof. Dr. Victor Mougel for providing access to the XPS instrumentation and Dr. Agnieszka Kierzkowska for SEM analysis (both ETH Zürich). V.V.O. acknowledges support from ANR (project DEZECO ANR-22-CE05-0005). A.C.-V. thanks the Spanish "Ministerio de Ciencia e Innovación" for funding the "I + D Generación del Conocimiento" project (PID 2021-128416NB-100). This publication was created as a part of NCCR Catalysis (grant number 180544), a National Centre of Competence in Research funded by the Swiss National Science Foundation.

## REFERENCES

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(2) Rommens, K. T.; Saeys, M. Molecular Views on Fischer–Tropsch Synthesis. *Chem. Rev.* **2023**, *123*, 5798–5858.

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(10) Subramanian, V.; Cheng, K.; Lancelot, C.; Heyte, S.; Paul, S.; Moldovan, S.; Ersen, O.; Marinova, M.; Ordomsky, V. V.; Khodakov, A. Y. Nanoreactors: an Efficient Tool to Control the Chain-Length Distribution in Fischer–Tropsch Synthesis. *ACS Catal.* **2016**, *6*, 1785–1792.

(11) Chen, Y.; Batalha, N.; Marinova, M.; Impéror-Clerc, M.; Ma, C.; Ersen, O.; Baaziz, W.; Stewart, J. A.; Curulla-Ferré, D.; Khodakov, A. Y.; et al. Ruthenium Silica Nanoreactors with Varied Metal–Wall Distance for Efficient Control of Hydrocarbon Distribution in Fischer–Tropsch Synthesis. *J. Catal.* **2018**, *365*, 429–439.

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(16) Griboval-Constant, A.; Giraudon, J. M.; Leclercq, G.; Leclercq, L. Catalytic Behaviour of Cobalt or Ruthenium Supported Molybdenum Carbide Catalysts for FT Reaction. *Appl. Catal. A: Gen.* **2004**, *260*, 35–45.

(17) Woo, H. C.; Park, K. Y.; Kim, Y. G.; Nam, I. S.; Chung, J. S.; Lee, J. S. Mixed Alcohol Synthesis from Carbon Monoxide and Dihydrogen over Potassium-Promoted Molybdenum Carbide Catalysts. *Appl. Catal. A* **1991**, *75*, 267–280.

(18) Wu, Q.; Christensen, J. M.; Chiarello, G. L.; Duchstein, L. D. L.; Wagner, J. B.; Temel, B.; Grunwaldt, J.-D.; Jensen, A. D. Supported Molybdenum Carbide for Higher Alcohol Synthesis from syngas. *Catal. Today* **2013**, *215*, 162–168.

(19) Li, T.; Virginie, M.; Khodakov, A. Y. Effect of Potassium Promotion on the Structure and Performance of Alumina Supported Carburized Molybdenum Catalysts for Fischer–Tropsch Synthesis. *Appl. Catal. A: Gen.* **2017**, *542*, 154–162.

(20) Vo, D.-V. N.; Nguyen, T.-H.; Kennedy, E. M.; Dlugogorski, B. Z.; Adesina, A. A. Fischer–Tropsch Synthesis: Effect of Promoter Type on Alumina-Supported Mo Carbide Catalysts. *Catal. Today* **2011**, *175*, 450–459.

(21) Fischer, F.; Tropsch, H. Über die Direkte Synthese von Erdöl-Kohlenwasserstoffen bei Gewöhnlichem Druck. (Zweite Mitteilung.). *Ber. Dtsch. Chem. Ges.* **1926**, *59*, 832–836.

(22) Biloen, P.; Sachtler, W. M. H. Mechanism of Hydrocarbon Synthesis over Fischer–Tropsch Catalysts. In *Adv. Catal.*, Eley, D. D., Pines, H., Weisz, P. B., Eds.; Vol. 30; Academic Press, 1981; pp 165–216.

(23) Craxford, S. R.; Rideal, E. K. 338. The Mechanism of the Synthesis of Hydrocarbons from Water Gas. *J. Chem. Soc.* **1939**, 1604–1614.

(24) Brady, R. C., III; Pettit, R. Reactions of Diazomethane on Transition-Metal Surfaces and Their Relationship to the Mechanism of the Fischer–Tropsch Reaction. *J. Am. Chem. Soc.* **1980**, *102*, 6181–6182.

(25) Joyner, R. W. Mechanism of Hydrocarbon Synthesis from Carbon Monoxide and Hydrogen. *J. Catal.* **1977**, *50*, 176–180.

(26) Maitlis, P. M.; Zanotti, V. Organometallic Models for Metal Surface Reactions: Chain Growth Involving Electrophilic Methylidynes in the Fischer–Tropsch Reaction. *Catal. Lett.* **2008**, *122*, 80–83.

(27) Ciobică, I. M.; Kramer, G. J.; Ge, Q.; Neurock, M.; van Santen, R. A. Mechanisms for Chain Growth in Fischer–Tropsch Synthesis over Ru(0001). *J. Catal.* **2002**, *212*, 136–144.

(28) Weststrate, C. J.; Sharma, D.; Garcia Rodriguez, D.; Gleeson, M. A.; Fredriksson, H. O. A.; Niemantsverdriet, J. W. Mechanistic Insight into Carbon-Carbon Bond Formation on Cobalt under
**Alan J. Barrios** — University of Lille, CNRS, Centrale Lille, University of Artois, UMR 8181 — UCCS — Unité de Catalyse et Chimie du Solide, Lille 59000, France; Laboratory for Chemical Technology, Department of Materials, Textiles and Chemical Engineering, Ghent University, Ghent B-9052, Belgium

**Zixuan Chen** — Department of Mechanical and Process Engineering, ETH Zürich, Zürich CH-8092, Switzerland;

● orcid.org/0000-0002-3882-3016

**Christoph R. Müller** — Department of Mechanical and Process Engineering, ETH Zürich, Zürich CH-8092, Switzerland;

● orcid.org/0000-0003-2234-6902

Complete contact information is available at:
https://pubs.acs.org/10.1021/acscatal.3c03956

### Notes

The authors declare no competing financial interest.

## ACKNOWLEDGMENTS

This work was supported by ETH Zürich through a doctoral fellowship to E.K. (ETH-40 19-2) and Z.C. (ETH-40 17-2). We are grateful to Scientific Centre for Optical and Electron Microscopy (ScopeM, ETH Zürich) for providing access to electron microscopy facilities. We thank Prof. Dr. Victor Mougel for providing access to the XPS instrumentation and Dr. Agnieszka Kierzkowska for SEM analysis (both ETH Zürich). V.V.O. acknowledges support from ANR (project DEZECO ANR-22-CE05-0005). A.C.-V. thanks the Spanish "Ministerio de Ciencia e Innovación" for funding the "I + D Generación del Conocimiento" project (PID 2021-128416NB-100). This publication was created as a part of NCCR Catalysis (grant number 180544), a National Centre of Competence in Research funded by the Swiss National Science Foundation.

## REFERENCES

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(2) Rommens, K. T.; Saeys, M. Molecular Views on Fischer–Tropsch Synthesis. *Chem. Rev.* **2023**, *123*, 5798–5858.

(3) Fratalocchi, L.; Visconti, C. G.; Groppi, G.; Lietti, L.; Tronconi, E. Intensifying Heat Transfer in Fischer–Tropsch Tubular Reactors through the Adoption of Conductive Packed Foams. *Chem. Eng. J.* **2018**, *349*, 829–837.

(4) Filot, I. A. W.; Broos, R. J. P.; van Rijn, J. P. M.; van Heugten, G. J. H. A.; van Santen, R. A.; Hensen, E. J. M. First-Principles-Based Microkinetics Simulations of Synthesis Gas Conversion on a Stepped Rhodium Surface. *ACS Catal.* **2015**, *5*, 5453–5467.

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(9) Ordomsky, V. V.; Luo, Y.; Gu, B.; Carvalho, A.; Chernavskii, P. A.; Cheng, K.; Khodakov, A. Y. Soldering of Iron Catalysts for Direct Synthesis of Light Olefins from syngas under Mild Reaction Conditions. *ACS Catal.* **2017**, *7*, 6445–6452.

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(13) Patterson, P. M.; Das, T. K.; Davis, B. H. Carbon Monoxide Hydrogenation over Molybdenum and Tungsten Carbides. *Appl. Catal. A: Gen.* **2003**, *251*, 449–455.

(14) Schaidle, J. A.; Thompson, L. T. Fischer–Tropsch Synthesis over Early Transition Metal Carbides and Nitrides: CO Activation and Chain Growth. *J. Catal.* **2015**, *329*, 325–334.

(15) Kim, H.-G.; Lee, K. H.; Lee, J. S. Carbon Monoxide Hydrogenation over Molybdenum Carbide Catalysts. *Res. Chem. Intermed.* **2000**, *26*, 427–443.

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(19) Li, T.; Virginie, M.; Khodakov, A. Y. Effect of Potassium Promotion on the Structure and Performance of Alumina Supported Carburized Molybdenum Catalysts for Fischer–Tropsch Synthesis. *Appl. Catal. A: Gen.* **2017**, *542*, 154–162.

(20) Vo, D.-V. N.; Nguyen, T.-H.; Kennedy, E. M.; Dlugogorski, B. Z.; Adesina, A. A. Fischer–Tropsch Synthesis: Effect of Promoter Type on Alumina-Supported Mo Carbide Catalysts. *Catal. Today* **2011**, *175*, 450–459.

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