Catalysis Science &

The decomposition of formic acid to obtain hydrogen has been studied using molybdenum carbides supported on an activated carbon and two high surface area graphites, H 200 (200 m 2 /g) and H 400 (400 m 2 /g). Particular attention is paid to the effect of Mo loading. The catalysts were prepared in situ using a mixture of CH 4 and H 2 up to 700°C. Under these conditions carburization was mostly complete. We observed, that the support influenced the Mo x C phase obtained so that it seems that the ratio of defective carbon influences the phase. However, for these materials the C/Mo ratio did not influence the obtained crystal phase. The characterization by XRD showed that while  -Mo 2 C phase was obtained over activated carbon and over H 200 . In contrast MoO x C y was obtained over H 400 . These catalysts reached 100% conversion on the formic acid decomposition at temperatures in the range 190-250  C and were also highly selective under these mild conditions with values for CO 2 selectivity in the range 85.0-96.5%. The best results were achieved over a 10 wt% Mo loading on activated carbon that reached 96.5% selectivity to H 2 . Also, changes in the molybdenum phases were observed on the spent catalyst. Some redox transformations during reaction were resposible of the transformation of  -Mo 2 C into oxycarbide MoOxCy. In summary, the results of catalytic performance indicated that  -Mo 2 C phase was more active, selective and stable than MoOxCy


rials
15 July
2020

D H Carrales-Alvarado 
Catalysis Science & Technology Catalysis Science & Technology


A B Dongil 
Catalysis Science & Technology Catalysis Science & Technology


J M Fernández-Morales 
Catalysis Science & Technology Catalysis Science & Technology


M Fernández-García 
Catalysis Science & Technology Catalysis Science & Technology


A Guerrero-Ruiz 
Catalysis Science & Technology Catalysis Science & Technology


I Rodríguez-Ramos 
Catalysis Science & Technology Catalysis Science & Technology


Selective hydrogen production from formic acid decomposition over Mo carbides supported on carbon materials
15 July 2020DCF39B9514C3515ECE684F0ABCB9798E10.1039/x0xx00000xReceived 00th January 20xx, Accepted 00th January 20xx
The decomposition of formic acid to obtain hydrogen has been studied using molybdenum carbides supported on an activated carbon and two high surface area graphites, H 200 (200 m 2 /g) and H 400 (400 m 2 /g).Particular attention is paid to the effect of Mo loading.The catalysts were prepared in situ using a mixture of CH 4 and H 2 up to 700°C.Under these conditions carburization was mostly complete.We observed, that the support influenced the Mo x C phase obtained so that it seems that the ratio of defective carbon influences the phase.However, for these materials the C/Mo ratio did not influence the obtained crystal phase.The characterization by XRD showed that while -Mo 2 C phase was obtained over activated carbon and over H 200 .In contrast MoO x C y was obtained over H 400 .These catalysts reached 100% conversion on the formic acid decomposition at temperatures in the range 190-250C and were also highly selective under these mild conditions with values for CO 2 selectivity in the range 85.0-96.5%.The best results were achieved over a 10 wt% Mo loading on activated carbon that reached 96.5% selectivity to H 2 .Also, changes in the molybdenum phases were observed on the spent catalyst.Some redox transformations during reaction were resposible of the transformation of -Mo 2 C into oxycarbide MoOxCy.In summary, the results of catalytic performance indicated that -Mo 2 C phase was more active, selective and stable than MoOxCy under the studied conditions.

Introduction

The need of substituting fossil sources with other more environmentally friendly alternatives that match current energy schemes, has prompted research on more sustainable energy sources.One of the possibilities is to use hydrogen as energy vector as it is well known to own a high energy density per mass, and it only produces water upon combustion.However, hydrogen actually holds a low energy per unit volume in gas phase, so it would occupy a large volume which limits its widespread application.Alternatively, hydrogen can be stored in other molecules that are more easily handled and that decompose in hydrogen when required [1].Among them, formic acid, HCOOH, represents an interesting alternative since it offers a high content of hydrogen 4.3 wt%, it is safe and it is produced in large quantities in biorefineries as a subproduct of the Biofine process [2].Its attractiveness is also due to the soft conditions required to decompose in hydrogen and carbon dioxide in the presence of a catalyst.However, upon reaction conditions the catalyst may also promote the dehydration reaction of formic acid, producing carbon monoxide and water which is an undesirable reaction path, not only because of the lower hydrogen production but also because carbon monoxide is a poison of catalysts, specially those most commonly employed in fuel cells such as Pt [3].Formic acid decomposition over heterogeneous catalysts has been studied over metals in their reduced state [4], metal oxides and more recently using immobilized noble metal complexes [5].Despite the clear potential of these latter systems that could provide a high atom efficiency, their high cost and low stability complicates industrial application.Moreover, an attractive catalyst should also be easy to synthetize using an environmentally safe process and cost effective.Some works using oxides such as -Fe 2 O 3 , pure Al 2 O 3 and MgO doped Al 2 O 3 appeared, however their activity and selectivity is low even working at temperatures above 200°C [6 7].In this context, the use of trans

ion metal carbides emer
es as an interesting alternative since they have proven to be very active and selective in several reactions.The reason for these results seems to be their structural similarity to Pt group metals.The potential of molybdenum carbide on the production of hydrogen by decomposition of several starting molecules such as methanol or formic acid has already been assessed [8,9,10].It was demonstrated that decomposition of formic acid over molybdenum carbide surfaces was enhanced compared to metallic molybdenum even at low temperatures [9].Indeed, the selectivity obtained over C-Mo (110) was 15 times higher than over Mo (110).

Other authors studied the effect of carbon source on unsupported molybdenum carbide structure and its relation to formic acid decomposition [11].One of the challenges of molybdenum carbide to be used in heterogeneous catalysis is obtaining a high surface area material to maximize the activity.In this respect, some alternative synthetic procedures such as using other carbon precursors have been studied, but still surface areas below 40 m 2 /g were obtained [12].Another possibility is to support the carbide onto a high surface area material.In this sense, the use of carbon supports can be beneficial for several reasons.The carbon support may favour the formation of the carbide by providing additional carbon source for the synthesis.Also, since water might be produced during the reaction, a hydrophobic and stable support under such conditions is preferred.

The effect of the nature of carbon support and its influence on the catalytic performance on reactions like steam reforming of methanol or dry reforming of methane has been reported [13].

Still, the catalytic behaviour of carbon-supported molybdenum carbide on formic acid decomposition has been scarcely investigated and assessing the effect of its structure is highly challenging and not fully understood.Hence, we have studied the synthesis of molybdenum carbide using a mixture of CH 4 and H 2 over two commercial high surface area graphites and we have compared their performance with the activated carbon supported counterpart to evaluate the effect of the graphitic structure.


Results and discussion

External surface area of the catalysts was measured for each sample and results are summarized on Table 1.The S BET of the parent supports is 950, 400 and 200 m 2 /g for AC, H 400 and H 200 respectively.It can be observed that S BET decreases as the amount of carbide increases.The reduction of S BET for the high surface area graphite-based catalysts is higher than the expected value due to the weight percentage of carbide on the surface.The loss of surface area in carbon supports upon carburization has been well reported and ascribed to the poreblocking due to the carbon growth during the carburization and/or the metal nanoparticles or to partial gasification of the support [14].However, considering the structure of high surface area graphites, the observed decrease on surface area is likely due to the agglomeration of the graphite particles upon thermal treatment.The higher loss of surface area on active carbon could be ascribed either to the easier gasification of carbon on that material and particularly, to its large proportion of porous in the microporous range which are easily blocked.The external surface area of the activated carbon without microporous is 400 m 2 /g.There are several reports with different assignations for the XRD and no clear consensus exists.In order to assess for the carburisation mechanism taking place and the obtained structures, we followed the synthesis of 10Mo x C/H 400 using in situ Mo K-edge X-ray absorption near-edge spectroscopy (XANES).The Mo K-edge spectra, in Please do not adjust margins Please do not adjust margins (obtained using the derivatives of the spectra) were used to estimate the oxidation state of each species by using the linear correlation obtained with the reference Mo compounds (see Figures SI2 and SI3).In figure 2B the two Mo 6+ species spectra exhibit similar characteristics to those of the AHM reference with a pre-edge feature in the spectra that does not appear in the other Mo species.So, the sample initially contains the supported ammonium heptamolybdate (AHM), in which Mo +6 is in six-fold coordinated sites (see reference spectra in Figure SI3).It is possible to observe three characteristics XANES resonances whose relative intensity is influenced by the local order around Mo atoms in octahedral symmetry [16].Upon heating, the supported AHM is transformed into another Mo 6+ species also in octahedral coordination, molybdenum oxide type structure, whose XANES spectrum shows higher intensity of the second XANES resonance relative to the first and third.This indicates changes in the specific surrounding environment of Mo atoms, likely an increase in the cluster size of the molybdenum oxide [16].This process takes up to 350°C when the first Mo 6+ is mostly absent.Meanwhile, a Mo +2 species ascribed to molybdenum oxycarbide [16], MoO x C y, starts to appear at 300°C while the second Mo 6+ species decreases.In the temperature range of ca.400-600°C, the fraction of MoO x C y is mostly constant indicating that simultaneous formation and consumption of MoO x C y takes place with parallel formation of a Mo 1+ species with XANES spectrum similar to that corresponding to the molybdenum carbide phase -Mo 2 C (Figure SI2).Upon heating up to 700°C, it resulted in further carburisation with a final proportion of ca.90% of -Mo 2 C and 10% of MoO x C y .Based on XANES experiments we can now assign the XRD peaks as foll ws.The diffraction peaks observed for the catalyst 10Mo x C/AC correspond to the (100), (002), ( 101) and (110) planes of the -Mo 2 C hcp phase (JCPDS-PDF 77-0720).The higher angle at which the maximum is observed for the other catalysts, would be in agreement with the presence of MoO x C y phase that holds a face-centered-cubic (fcc) structure with diffraction peaks at 37.1°, 44.1° and 62.9° [17,18].It must be noted, however, that XANES showed a higher proportion of -Mo 2 C on the selected 10Mo x C/H 400 sample than what is observed by XRD.This can be attributed to the small size of the supported carbide particles which would be below the detection limit of XRD, i.e. < 5 nm, as also the TEM images, in Fig. 3 and Fig. SI4, confirmed.On the contrary for 10Mo x C/AC, both large and small particles are carburised as the XRD and HRTEM images showed.For this sample, the well-resolved lattice fringes of 0.23 nm that correspond to the -Mo 2 C (101) planes are observed in particles as small as 2 nm.Similar findings are observed for 10Mo x C/H 400 for which also -Mo 2 C (101) is observed in small particles.Hence, it can as well be inferred that larger particles are more difficult to carburise.This is agreement with the diffraction peaks ascribed to MoO 3 observed on 20Mo x C/H 200 which is the sample with the largest particle size, ca.8.1 nm as estimated by TEM in Table 1.With the aim of gaining more information on the synthesis mechanism and the effect of the support, additional XANES experiments were performed with 20Mo x C/H 400 sample but using a H 2 /He atmosphere.The analysis of the in situ Mo k-edge XANES spectra (Figure SI5) showed that the same MoO 3 , MoOxCy and -Mo 2 C species are btained as when CH 4 /H 2 /He is employed over the 10Mo x C/H 400 sample (see Figures 2 and 4).These results suggest that under the studied conditions, the carbon source to obtain the carbide is the support itself i dependently of the reaction atmosphere.Similar results were reported previously for temperatures below 600°C [19].The slight differences between samples, i.e. the 20Mo x C/H 400 is somewhat more resistant to reduction in agreement with XRD experiments, may be attributed to effects of the different particle size in the samples (Table 1).The 20Mo x C/H 400 sample with larger particles is more difficult to carburize.Also, considering these stages it is reasonable to presume that the availability of more reactive carbon atoms from the support would aid on the formation of -Mo 2 C. In this sense, the carbon supports are characterized by their different proportion of edges to basal planes, i.e. the size of the graphitic layers, so that, a higher proportion of edges means more reactive carbon.This feature is given by the Raman spectra that allows comparison by using the intensity of the so-called D and G bands [20].The Raman spectra of the supports, in  Please do not adjust margins Plea e do not adjust margins of m/z 18-16 are observed in a proportion that suggest that they correspond to H 2 O.The same masses are observed at ca. 600°C but the intensity of these latter peaks is lower.Small intense signals for m/z 28 and 44 at ca. 290°C and 415°C are also observed.The samples 10Mo x C/H 200 and 10Mo x C/H 400 also display contributions of m/z 18-16 which can be ascribed to H 2 O.However, the maxima appeared at 400°C and 660°C, this latter being the most intense peak.Also, simultaneous evolution of m/z 28 due to CO is also observed, although its intensity is very low.

The XANES results suggested that the source of carbon is the support itself and that carburisation already starts at 300°C, with the formation of the oxycarbide which is then transformed into -Mo 2 C (reaction 1).
MoO 3 +C*+ H 2 →MoO x C Y + H 2 O -Mo 2 C + CO (1)
In this range of temperatures, carburisation must be preceded by the formation of gaseous carbon species, most likely CH 4 coming from the reaction with hydrogen and releasing H 2 O .However, the intensity of m/z 16-14 in the profiles up to 700°°C does not suggest the evolution of CH 4 and only above that temperature, an intense peak started to appear.We believe this is due to the consumption of the evolved CH 4 on the carburisation process.Also, the different intensity of the MS-TPD peaks at 400°C and 600°C for AC and the two H samples seem to indicate that the extent in which the first step occurs in AC is greater than on H 200 and H 400 samples.This is reasonable since in this first step the incorporation of carbon takes pla

and, as already
ointed out, activated carbon holds a larger proportion of reactive carbon atoms.In turn, it also suggests that carburisation took place in a larger extent, as also the XRD showed.

Regarding previous literature results, it has een reported that the synthesis of molybdenum carbide over carbon nanofibers and carbon nanotubes using the TPR method (CH 4 /H 2 ) also led to the formation of the -Mo 2 C and that above 700°C no molybdenum oxide was observed [21,22].Other authors also analysed the effect of surface chemistry and structural properties of the support using an oxidized graphite and oxidized activated carbon [23].Although a clear correlation of surface chemistry and structural properties with the formed molybdenum phase was diffi

lt
o obtain, the authors suggested that the defective carbon was somehow responsible for the formation of the Mo 2 C and that the controlled reduction of the molybdenum precursor was a critical factor to determine the formed crystal phase.Some authors proposed that Mo/C ratio on an ordered mesoporous carbon support controls the Mo x C phase [24].We observed that samples with different loading, mainly 10Mo x C/H 200 and 20Mo x C/H 200 displayed different XRD profile.However, this seems to be more related to the contribution of larger particles to the XRD profile, which are present in a higher ratio on samples with greater loading.

Our results are in agreement with some literature, that reported oxycarbide and Mo 2 C as the only detected phases.We can add that even in a CH 4 /H 2 atmosphere the source of carbon is the support itself.Also, the fact that the support is the source of carbon is in agreement with the easiness carburisation of smaller particles that would be in closer contact with the support.


Reaction results

The conversion of formic acid decomposition measured at each temperature is given in  In order to minimize the effect of Mo loading, the activities at 150 °C were estimated and the results are displayed in Regarding molybdenum-based catalysts, previous literature reported that 100% formic acid conversion was achieved at temperatures above 250°C for unsupported molybdenum carbide systems [11] and over 200°C for supported systems over activated carbon with selectivity around 98% [26].However, the catalysts employed in Ref. 11 and 26, were prepared using liquid phase mixture with organic compounds that is less attractive from an industrial point of view and may leave impurities on the catalysts.Nevertheless, the reported catalytic performance using molybdenum carbide and our own results are better than other reported for non-noble metal systems like metal oxides, -Fe 2 O 3 for which maximum conversion was around 24% at temperatures of 200°C with low selectivity to H 2 [27,7] and other systems where Ag and Mg were used as dopants for Mo x C that reached 90% selectivity [28].Interestingly, the selectivity profiles with temperature shown in Fig 6B are similar.All the catalysts prepared over high surface area graphite, showed an initial selectivity decrease up to 140-180°C which corresponds to formic acid conversions in the range 10-12 % followed by a selectivity increase, up to temperatures above 200-260°C, i.e. when conversion reached 90%.These results are in agreement with previously reported selectivity profiles where other authors observed that CO 2 selectivity decreased with temperature in the temperature range 100-150°C [6].However, the evaluation of the catalysts at higher temperatures performed in the present work shows that selectivity increased from conversions above 15%, and at 95% conversion the selectivity decreased again.

As long as the stability is concerned, additional experiments in time on stream at temperatures of 180-190°C for all the catalysts and at 22 °C for the 20Mo x C/H 200 were performed during 12 hours.Both conversion and selectivity profiles, in Fig. 7, remain stable with time for all the catalysts, except for the conversion achieved with 20Mo x C/H 200 that showed a continuous decrease with time, while selectivity was constant.

It is known that the decomposition of formic acid may take place through two paths: dehydrogenation (HCOOH H 2 + CO 2 ) and dehydration (HCOOH  CO + H 2 O).Also, water gas shift and/or the reverse reaction may take place producing CO 2 +H 2 or CO and H 2 O respectively [1].Please do not adjust margins


Please do not adjust margins

On the other hand, for the catalysts presenting also MoO x C y , it is plausible that both FA dehydrogenation and dehydration occur at the beginning of the experiment and when conversion reaches 10% the formed CO and H 2 O through dehydration, react to produce CO 2 and H 2 via the water gas shift reaction, this increasing the selectivity.If this happens it is plausible that only limited oxidation of molybdenum carbide occurs since water would be consumed by WGS.Hence, we performed the XRD of the spent catalysts to assess for potential changes and are shown in Fig 8 labelled as "catalyst-PR".However, different results were observed.On the one hand, 10Mo x C/H 400 -PR displayed diffractions at 2θ of 34.4°, 37.7°, 39.6° and 61.5° and sharper than those of the fresh catalyst that correspond to sintered particles of the -Mo 2 C phase.On the other hand, 20Mo x C/H 400 -PR shows diffractions at 2θ of 35.2°, 36.7° and at 2θ of 53.
° which can be ascribed to MoO 2 [30,31].For 5Mo x C/H 400 -PR, no diffractions other than those of the support were observed.This is probably due to the small particle size and/or the low concentration of species, below the detection limit.

In any case, the detected changes on the catalysts phase, either conversion to -Mo 2 C or to oxycarbide agree with the selectivity profiles observed for 10Mo x C/H 400 -PR and 20Mo x C/H 400 -PR since both new phases may promote the CO 2 selectivity either by direct transformation of FA to CO 2 or through WGS.A different case is that of the catalyst 20Mo x C/H 200 .This catalyst initially presented both carbide and oxide phases and the selectivity to CO 2 is below the other tested catalysts but it also showed the selectivity increase at around 10% conversion.The XRD of the spent catalyst, shows diffractions at 2θ of 34.4°, 37.8°, and 39.8° from the -Mo 2 C along with peaks at 35.7°, 38.2° and 60.1°.The position of these latter peaks seems to indicate that they correspond to oxycarbide.Again, it seems that oxycarbide is formed during the reaction and, although -Mo 2 C phase is still detected, the intense and sharp diffraction ascribed to oxycarbide seems to indicate that large particles of these species have been formed on the surface.Despite these new nanoparticles appeared, the selectivity remained stable with time probably due to the positive effect of the new oxycarbides species which are active in WGS.However, the larger particle size inferred from the sharp XRD peaks would be responsible of the conversion decrease with time.

In contrast, the XRD pattern of the 10Mo x C/AC sample after reaction also corresponds to the -Mo 2 C and no other diffraction is envisaged, in agreement with the higher selectivity to CO 2 and better stability.Nonetheless, the selectivity below 100% could also suggest that small undetected amounts of another phase are present.So, even in the presence of oxidants, H 2 O or CO 2 , this catalyst resulted to be highly stable under the reaction conditions.The change of molybdenum phase under reaction conditions have already been reported.For example, during dry reforming of methane reaction, deactivation of Mo 2 C catalysts due to oxidation to MoO 2 has been reported [32].Ledoux et al. also found that Mo 2 C changed to MoO 2 , while -Mo x C was transformed into MoO 2 and eventually to Mo 2 C [19].

Similarly, phase changes were also observed in the spent catalysts after steam reforming of methanol reaction [33].Some authors, have reported that other phase such as -MoC is more active on formic acid decomposition than -Mo 2 C [5].However, chloro and nitrogen containing compounds were used as carbon source to prepare the catalysts and the effect of those elements should have been considered.Indeed, in the same report it is also shown that a conventional -Mo 2 C prepared from a CH 4 /H 2 mixture was the most active and selective catalyst.In line with our results, molybdenum carbide prepared over activated carbon was more active and selective than when carbon nanotubes were used as support [6].Even though the crystallographic phase of the molybdenum carbides were not shown, it is likely that the -Mo 2 C pha

r activated carbon as a
ready shown in several literature and in the present work [23,26].As demonstrated by XRD, in the present work the main phase on the catalysts was Mo 2 C, although MoO x C y could be found on H 400 and H 200 based catalysts, so our results are in quite good agreement with literature, showing that -Mo 2 C is more active and selective.

Very recently, the reaction mechanisms of both dehydration and dehydrogenation reaction of formic acid on molybdenum carbide have been studied [34].The authors proposed that the target reaction leading to CO 2 and H 2 takes place through bridged formate species that evolve into monodentate formate, and transformed to CO 2 and H* following a Langmuir-Hinshelwood mechanism.On the other hand, the dehydration reaction follows an Eley-Rideal path in which gaseous HCOOH reacts w

h adsorbed H* to
orm H 2 O and CO.Considering these paths, the rate in which dehydrogenation occurs might depend on the easiness of the bridge type adsorption of the formate.The carbon/molybdenum ratio influences the physico-chemical properties of the carbides and so the catalytic properties.In this sense, it has already been reported that a higher C/Mo ratio has a negative impact on the reactivity.In this respect, the MoOxCy surface would be more saturated and less metallic than the unsaturated Mo 2 C surface [35].Following this argument, it is plausible that the cleavage of the O-H bond and adsorption of the formate on the less saturated surface of -Mo 2 C would be energetically favoured than over MoO x C y .Please do not adjust margins Please do not adjust margins


Experimental


Synthesis of materials

Metal carbides were prepared by wetness impregnation followed by carburization treatment.Activated carbon (Type CO-850 from Petrochil S.A) was used as support and was first grounded and sieved to < 150 µm particle size, and then dried at 110°C for 2 h before impregnation.Commercial high surface area graphite (H400 and H200, from Timcal Graphite).An aqueous solution of the precursor (NH4)6Mo7O24 (99% from Aldrich) was impregnated on the support using the corresponding amount to obtain the metal loading, left for maturation for 6 h, and dried overnight at 80°C.The carburization was carried out in situ prior to the reaction, under the mixture composition at 80/20 of H2/CH4 (%vol) at 700 °C, (5°C.min-1) for 2 h.Resulting catalysts will be labelled according to the metal composition, loading and support.


Characterization

Textural properties were measured from the adsorption isotherm of N 2 at -196°C using a 3Flex instrument from Micromeritics.Around 100 mg were previously degassed at 4 h at 110°C under vacuu t from Micromeritics.The surface area was calculated from the adsorption branch in the range 0.02 ≤ p/p 0 ≤ 0.25 using the Brunauer-Emmett-Teller (BET) theory.Total pore volume was defined as the single-point pore volume at p/p 0 =0.99.X-ray diffraction (XRD) patterns of the passivated catalysts were acquired in the 2Ɵ range between 4° and 90° with a step of 0.04°/s using a Polycristal X'Pert Pro PANalytical diffractometer with Ni-filtered Cu Kα radiation (λ = 1.54 Å) operating at 45 kV and 40 mA.XPS measurements were performed with an energy analyser (PHOIBOS 150 9MCD, SPECS GmbH) using non-monochromatic Al radiation (200 W, 1486.61 eV).The samples were pelletized and transferred to the outgassed chamber.Prior to the experiments, samples were outgassed

-situ for
24 h to achieve a dynamic vacuum below 10-10 mbar.The binding energy (BE) was measured by reference to the C 1s peak at 284.6 eV, with an equipment error of less than 0.01 eV in the energy determinations.

Information about the supported metal particles was acquired by TEM in a JEOL 2100F field emission gun electron microscope operated at 200 kV and equipped with an Energy-Dispersive X-Ray detector.The sample was ground until powder and a small amount was suspended in ethanol solution using an ultrasonic bath.Some drops were added to the copper grid (Aname, Lacey carbon 200 mesh) and the ethanol was evaporated at room temperature before introduce in the microscope.The Scanning Transmission Electron Microscopy (STEM) was done using a spot size of 1 nm.Average particle size area (d TEM ) was calculated as
d TEM = ∑ n i d 3 i ∑ n i d 2 i
Mo K-edge (20.000 eV) X-ray absorption near edge spectra (XANES) were reco ded in dispersive mode at the BM23 beamline at the European Synchrotron Radiation Facility (ESRF, Grenoble, France).The catalysts were pressed into pellets and sieved to a size between 0.090 a

0.140 mm.The samples (ca.15
g) were loaded in a quartz plug-flow microreactor system developed at BM23.The reactor was contin

usly fed wit
: a) 30 mL min −1 of the mixture composition 20/5/75 of H 2 /CH 4 /He for the temperature-programmed carburization experiment or b) 30 mL min −1 of 20% hydrogen in helium during temperatureprogrammed reduction experiment.The temperature was raised by 3 °C min −1 up to 700 °C.XANES spectra were collected every 30 °C or 10 min during the heating.


Reaction

The measurements of the catalyst activity in vapor phase formic acid decomposition were carried out in a fixed-bed flow reactor.

The catalysts (0.075 g) were placed in a U-tube reactor with an internal diameter of 4 mm.All the samples were in situ carburized in CH 4 /H 2 (20:80 vol) at 700 °C for 2 h and cooled in N 2 to a reaction temperature prior to testing (in situ reduction).The mixture of 5.5 vol % formic acid/N 2 at a total flow rate of 25 cm 3 (STP)/ min was fed to the reactor by a saturator.The reactants and products were analysed by a gas chromatograph (Varian 3400) fitted with a 60/80 Carboxen TM 1000 column and a thermal conductivity detector.At each temperature, a few measurements were performed to be sure in reaching of steady-state activity.During the test, the unique products determined were CO, CO 2 and H 2 .The concentrations of these compounds were calculated by following equations.(1) X HCOOH =

[CO] + [CO 2 ]

[HCOOH] 0 × 100

In addition, the selectivity to CO 2 was calculated.The catalysts were s

died in two heating cy
les.The stability of the catalyst w