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Article

Properties of Carbon-supported Precious Metals Catalysts under Reductive Treatment and Their Influence in the Hydrodechlorination of Dichloromethane

by
Alejandra Arevalo-Bastante
,
Maria Martin-Martinez
*,
M. Ariadna Álvarez-Montero
,
Juan J. Rodriguez
and
Luisa M. Gómez-Sainero
Departamento de Ingeniería Química, Facultad de Ciencias, Universidad Autónoma de Madrid, Cantoblanco, 28049 Madrid, Spain
*
Author to whom correspondence should be addressed.
Catalysts 2018, 8(12), 664; https://doi.org/10.3390/catal8120664
Submission received: 27 November 2018 / Revised: 13 December 2018 / Accepted: 14 December 2018 / Published: 18 December 2018
(This article belongs to the Special Issue Catalysis by Precious Metals, Past and Future)
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Versions Notes

Abstract

:
This study analyzes the effect of the reduction temperature on the properties of Rh, Pt and Pd catalysts supported on activated carbon and their performance in the hydrodechlorination (HDC) of dichloromethane (DCM). The reduction temperature plays an important role in the oxidation state, size and dispersion of the metallic phase. Pd is more prone to sintering, followed by Pt, while Rh is more resistant. The ratio of zero-valent to electro-deficient metal increases with the reduction temperature, with that effect being more remarkable for Pd and Pt. The higher resistance to sintering of Rh and the higher stability of electro-deficient species under thermal reductive treatment can be attributed to a stronger interaction with surface oxygen functionalities. Dechlorination activity and a TOF increase with reduction temperature (250–450 °C) occurred in the case of Pt/C catalyst, while a great decrease of both was observed for Pd/C, and no significant effect was found for Rh/C. Pt0 represents the main active species for HDC reaction in Pt/C. Therefore, increasing the relative amount of these species increased the TOF value, compensating for the loss of dispersion. In contrast, Pdn+ appears as the main active species in Pd/C and their relatively decreasing occurrence together with the significant decrease of metallic area reduces the HDC activity. Rh/C catalyst suffered only small changes in dispersion and metal oxidation state with the reduction temperature and thus this variable barely affected its HDC activity.

Graphical Abstract

1. Introduction

Catalysis plays a crucial role on the path of building a more sustainable industrial chemistry and diminishes the impact of the industrial processes in the environment. Synthesizing novel, more stable, active and selective catalysts, or effectively improving the existing ones, is a fundamental task.
Chloromethanes are chlorinated volatile organic compounds with serious environmental impact, due to their carcinogenic and highly toxic character, in addition to the production of photochemical smog, the depletion of ozone and global warming [1,2,3,4]. Regardless of their noxious effects, some of these compounds, like dichloromethane (DCM) and chloroform (TCM), remain irreplaceable in some of their applications because of their singular chemical and physical properties (high stability, volatility and solvent capacity, and low flammability). Hence, they are still extensively used in industry, and large amounts are discharged into the environment through gaseous and liquid streams.
Catalytic hydrodechlorination (HDC) is a promising technology for the treatment of these contaminated streams. It allows the conversion of organochlorinated species like chloromethanes into harmless chlorine-free compounds under relatively mild conditions. It is effective within a wide range of concentrations, and thus presents environmental and economic advantages over other techniques [5,6,7]. Furthermore, it may be applied ‘in situ’, in combination with other physical separation processes like adsorption, for the end-of-pipe treatment of residual streams generated in different industries [8].
A wide diversity of catalysts has been used in the HDC of several chlorocarbons and chlorofluorocarbons. Those based on noble metals supported by a porous material like alumina, silica or activated carbon, are the most common [6,9,10]. Among the publications related to the HDC with activated carbon-based catalysts, metals like Pd, Pt, Rh, Ru or Ni are the most frequent active phases found, with Pd being by far the most preferred one, due to its high capacity for the hydrogenolysis of C-Cl bonds [11,12,13]. This metal, as well as Pt and Rh, have demonstrated high activity and dechlorination capacity [12,14,15,16,17,18,19,20,21,22,23]. Several authors have reported relationships between the catalyst performance and different properties, like metal particles structure, catalyst porosity or surface chemistry. However, there is no consensus on the trends observed, being highly dependent on the reactants and the catalytic systems used. Several authors relate better HDC performances to small metal particle sizes [24,25,26,27,28,29]. On the contrary, higher turnover frequency (TOF) values were obtained when increasing metal particle size in other HDC studies [30,31,32,33]. The optimum particle size seems to depend on the particular reaction. Diaz et al. [25] associated Pd and Rh particles of sizes within 3–4 nm with higher activities in the HDC of 4-chlorophenol. The same reaction was studied by Baeza et al. [28] using size-controlled Rh nanoparticles within the 1.9–4.9 nm range. They reported the highest activity with the smaller nanoparticles, in agreement with the optimum size found by Ren et al. [27], who claimed that small and uniform Rh particles of 1.7 nm induced higher activity. Dantas Ramos et al. [30], found a decrease of TOF with increasing dispersion in the HDC of CFC-12 and TCM, and Bedia et al. [31] observed a TOF decrease in the HDC of DCM when decreasing metal particle size (from 2.26 to 1.86 nm). The metal oxidation state also affects the catalyst performance. A higher proportion of zero-valent Rh0 has been associated with higher activity and selectivity towards cyclohexanol in the HDC of 4-chlorophenol, while a higher proportion of electro-deficient Rhn+ induced a higher selectivity to phenol [28]. Cobo et al. [34] also found that a higher Rh0/Rhn+ ratio favors the HDC of trichloroethane with catalysts supported on CeO2. But with reduced graphene oxide, Rhn+ better interacts with the surface functional groups of the support, favoring the HDC [27]. In previous studies of our group [12,19,35], four different activated carbon-supported catalysts (Ru/C, Rh/C, Pd/C and Pt/C) were compared for the gas phase HDC of chloromethanes, finding attractive results in terms of catalytic activity. All the catalysts were considerably active, showing Rh/C, Pd/C and Pt/C have the best dechlorination capacity, although with significant differences in terms of activity, selectivity and stability. Pt/C led mainly to methane formation, while Rh/C and Pd/C were more selective to higher hydrocarbons (C2 and C3). Besides, with Rh/C higher amounts of olefins were obtained [12,14,16,19]. On the other hand, while Pt/C showed itself to be highly stable (demonstrated in long-term experiments up to 26 days on stream), the other two metallic catalysts experienced a progressive loss of activity [16,19,36]. This exceptional stability was also found for a catalyst supported on sulfated zirconia with a bimetallic Pd-Pt active phase during the HDC of dichloromethane (DCM) [37]. In all of the cases, the characterization of the catalysts revealed important differences in their physico-chemical properties. In particular, the oxidation state and particle size of the metallic active phase were revealed as determinant properties on the selectivity, activity and stability of the catalysts [19,36,37]. Higher proportions of electro-deficient metallic (Mn+) species combined with lower metal dispersions favored the selectivity to olefins and alkanes other than methane. On the contrary, higher proportions of zero-valent species (M0) and high metal dispersions promoted better stability. Understanding how these properties are conferred to the catalysts and their optimization to achieve a better performance in the HDC reaction is of crucial interest. These properties can be, to some extent, modulated varying the reduction conditions during the preparation of the catalysts, which may be used as an easy strategy for improving the catalytic activity or tuning the reaction selectivity.
Hence, in the current study, the effect of the reduction temperature (Tred) of Rh/C, Pd/C and Pt/C catalysts on their properties and behavior in the HDC of cloromethanes is analyzed, using DCM as the target compound.

2. Results and Discussion

2.1. Characterization of the Catalysts

The reducibility of the metallic phase in each catalyst was determined in a previous work by temperature-programmed reduction (TPR) [14]. In that study, it was shown to be a single reduction peak for Pd and Pt corresponding to the reduction of M2+ to M0, centered at 233 and 244 °C, respectively. Rh/C displayed three peaks, centered at 86, 125 and 222 °C. From these results, 250 °C was selected as the minimum reduction temperature to be tested and the range of 250–450 °C was covered.
The metal content of the non-reduced and reduced catalysts, as determined by mass spectrometry with inductive coupling plasma (ICP-MS), was always close to the nominal value (1.0% w/w) and no significant loss of metal occurred at any of the reduction temperatures. The reduction of the catalyst even at the highest temperature did not alter significantly the amount of metallic phase.
As can be seen in Table 1, all the catalysts showed an important BET surface area (SBET), above 1200 m2 g−1, and no considerable differences were observed after reduction at any of the temperatures tested.
The most significant effects associated with the reduction temperature were observed in the dispersion and the oxidation state of the metal on the surface of the catalyst (Table 2). The metal dispersion values, as determined by CO chemisorption, prove that Rh was well dispersed with only some slight dispersion decrease at the highest reduction temperature. Pt/C and Pd/C yielded significantly lower dispersion values, although were still quite good at the lowest reduction temperatures. Increasing reduction temperature caused a gradual dispersion decrease, more marked in the case of Pd/C. The lowest reduction temperature led in the three cases to the highest dispersion. This temperature allows the reduction of most of the metal particles, as confirmed by the TPR profiles [14].
Table 2 also presents the relative distribution of the surface metallic species (zero-valent and electro-deficient) at the different reduction temperatures tested. These results were achieved from the deconvolution of the Pt 4f, Pd 3d, and Rh 3d X-ray photoelectron spectroscopy (XPS) profiles (see Figures S1–S3 in the supplementary material). Both metallic species exist in all of the reduction temperatures tested, even at the highest one, although, as expected, the relative occurrence of M0 increased with the reduction temperature. However, this effect is of a significantly different intensity depending on the catalyst, being much more noticeable in the case of Pt/C and Pd/C, and showing lower significance for Rh/C. Moreover, in the latter, the electro-deficient species always remains the most abundant. This can be attributed to a different interaction of the metal precursor with the support, as pointed out by the TPR results, where three peaks of H2 consumption were observed with Rh/C, in comparison with the single peak of Pd/C and Pt/C. The higher amount of Mn+ species points to a solid interaction of rhodium particles with the activated carbon, allowing a higher stability of Mn+ species even at the highest reduction temperature. This would also explain the very low change of dispersion upon reduction. It is noteworthy that in Pt/C, most of the metal appears as zero-valent species, even at the lowest reduction temperature, in good agreement with other carbon-supported platinum catalysts reported in previous works, where platinum was reduced at 250 and 300 °C [14,16,19,38].
The values of oxygen atomic concentrations on the surface of the catalysts are also included in Table 2. A higher amount of surface oxygen can be observed for Rh/C, which also remains more stable under reduction, while some significant decrease is observed in Pd/C and Pt/C at increasing reduction temperatures. O 1s orbital was also deconvoluted according to literature [39] as shown in Figure 1. The following groups were assessed: C=O (531.1 eV), C-OH (532.3 eV), C-O-C (533.3 eV), C-OOH (534.2 eV) and H2O (535.9 eV) [39]. All the XPS profiles are included in Figures S4–S6 of supplementary material. The OCOOH/Ototal ratio (Table 2) represents the proportion of carboxylic groups (C-OOH) with respect to the total concentration of surface oxygenated groups. It provides information of the surface acidity of the catalysts. The amount of surface groups of the catalysts and their acid-base character may have some important effects on the changes occurring during the H2 treatment. A higher amount of surface oxygen groups favors the interaction between metal and support [40,41], avoiding the sintering of particles. On the other hand, the low ratios of carboxylic groups (Table 2) indicate that all the catalysts have a basic character on the surface, suggesting the prominent role of basic groups in the formation of electro-deficient species. Furthermore, Rh/C catalyst, which show the higher distribution of electro-deficient species, presents the higher amount of surface oxygen (OXPS) and the lowest OCOOH/Ototal ratio, which does not vary with reduction temperature, suggesting a stronger interaction of Rh precursor with the support that results in a higher resistance of Rh particles to sintering, in accordance with the results obtained. In contrast, Pt/C and Pd/C show a lower amount of surface groups and a lower basic character, observing some variations with reduction temperature.
Some representative transmission electron microscopy (TEM) images and the corresponding metal particle size distributions of the catalysts reduced at 450 °C, are shown in Figure 2. The images reveal smaller metallic particles in Rh/C, showing a mean particle diameter of 1.9 nm and a narrower distribution. These results agrees with the dispersion values calculated from CO chemisorption included in Table 2. The mean metal particle size obtained for Pd/C (6.0 nm) after reduction at 450 °C was significantly higher than the one previously reported [38] after reduction at 250 °C (1.9 nm), consistent with the loss of dispersion at increasing reduction temperatures (Table 2). Other authors have reported similar behavior in carbon-supported Pd catalysts [30]. With regard to Pt/C, the mean particle size after reduction at the highest temperature is 2.5 nm, also higher than the 1.6 and 1.7 nm previously obtained for the catalyst reduced at 250 °C [23,38]. Therefore, it can be concluded that sintering of metallic particles takes place during reduction at increasing temperatures, although to different extents, in the cases of Pt and Pd catalysts.
The X-ray diffraction (XRD) profiles of the catalysts reduced at different temperatures (Figure 3) show the characteristic peaks of the carbon support (dash lines) at 2θ values nearly 26° (planes 002), 43° (planes 100, 101 and 102, indistinguishable) and 80° (planes 110) [42,43,44]. As can be seen, XRD profiles were similar regardless of the reduction temperature. The peaks associated with zero-valent metal, which should be centered at 39.9°, 40.1° and 41.1°, respectively [12,14,44,45], were not observed in these patterns, supporting the small particle size of these metals for all the reduction temperatures investigated, as observed by TEM (Figure 2). In addition, in all cases, one peak appeared at 35° (*) at the lowest reduction temperature (250 °C), associated with the presence of metal chlorides (PtCl2, PdCl2, and RhCl3) from the precursors used in the preparation of the catalysts. Furthermore, these compounds seem to disappear at higher reduction temperatures, since this favors the desorption of Cl from the surface of the activated carbon.

2.2. Hydrodechlorination Results

Figure 4 shows the results obtained in the HDC of DCM with the Pt/C catalyst reduced at different temperatures, within the range of 150–250 °C reaction temperature. As can be seen, increasing the reduction temperature improves moderately overall dechlorination, in spite of the decrease of Pt dispersion. Therefore, some other effect must be compensating for the loss of dispersion. As shown in Table 2, the relative amount of zero-valent Pt (Pt0) rises significantly with the reduction temperature. These Pt0 species have proven to be the most active on the HDC of DCM with Pt/C catalyst in previous studies [16,23]. Figure 4 includes the evolution of TOF with the reduction temperature of the catalyst. The TOF values are compared at a 150 °C reaction temperature, where conversion throughout the reactor becomes low so that initial reaction rate values can be taken. A significant increase in TOF can be observed with the reduction temperature, the higher proportion of Pt0 then compensating the activity loss due to the dispersion downturn. This effect is clearly observed in Figure 4, which shows the TOF, metal dispersion and Pt0/Ptn+ ratio values of Pt/C reduced at different temperatures.
As in previous works with platinum catalysts [14,16,19], the HDC of DCM with Pt/C only yielded methane (selectivity > 85%) and methyl chloride (MCM) (see also Table S1 of supplementary material), independently of the reduction temperature used, due to the high zero-valent proportion of platinum. No significant variations of selectivity with the reduction temperature were found other than some slight increase towards methane, in accordance with the higher contribution of the Pt0 species in the dissociation of hydrogen during HDC.
Figure 5 shows the results with the Pd/C catalyst. Substantially different trends are observed with respect to Pt/C. As can be seen, in contrast with Pt/C, overall dechlorination decreased dramatically at an increasing reduction temperature, with the effect being more pronounced at higher reaction temperatures. This can be attributed to the combination of two negative effects (see Table 2): (i) the decrease of the concentration of electro-deficient species, which are known to be the most active species in the HDC of DCM with palladium catalysts [12,19,38], and (ii) the decrease of palladium dispersion. Among the catalysts tested in this study, Pd/C has been proven to be the most prone to sintering. Then, raising the reduction temperature of Pd/C results in an important loss of accessible metallic surface, and the subsequent loss of activity observed. This results in a decrease in DCM conversion (Table S2 in Supplementary Material). In previous studies, it was stablished the optimum Pd0/Pdn+ ratio around 1 for HDC reactions with Pd/C catalysts [19,36]. This is the value found in this study for the catalyst reduced at the lowest temperature. Despite the important loss of metal dispersion, no change in TOF is detected at reduction temperatures higher than 400 °C, where Pd0/Pdn+ ratio also remains constant.
With Pd/C, the HDC of DCM yielded mainly methane, ethane and MCM. At the highest reaction temperatures, small amounts of propane were also formed (Table S2 of supplementary material). The catalyst reduced at the lowest temperature yielded small amounts of hydrocarbons higher than methane (C1+), as can be observed in Figure 5. According to previous studies, this is favored by a higher electro-deficient to zero-valent palladium proportion [14,19], due to the particular ability of electro-deficient Pd to dissociate H2. This was evidenced by molecular simulation studies [46], where the preferred adsorption of hydrogen in electro-deficient Pdn+ species was reported when studying DCM and H2 interactions with Pd clusters by DFT. This would explain the decrease in methane selectivity. Hence, the concentration of MCM increases, it negatively affected the dechlorination obtained.
The results obtained with Rh/C are depicted in Figure 6. No significant effects of the reduction temperature can be pointed out, consistently with the almost unaltered characteristics given in Table 2. This catalyst yielded by far the best performance in terms of dechlorination, being almost complete at a 250 °C reaction temperature. The selectivity towards hydrocarbons higher than methane (C1+) was much higher than the obtained with the other two catalysts. Ethane was the most abundant among those hydrocarbons, but propane and even some smaller amounts of butane were also formed (see Table S3 of supplementary material).

3. Materials and Methods

3.1. Catalysts Preparation

The catalysts were synthesized by incipient wetness impregnation. A commercial activated carbon (Erkimia S.A., SBET = 1200 m2 g−1, pH slurry = 6.4 [42]), was impregnated with aqueous solutions of H2PtCl6, PdCl2, and RhCl3 (all supplied by Sigma-Aldrich, Madrid, Spain) to get 1 wt.% active phase nominal concentration. After 12 h at room temperature, the catalysts were dried at 100 °C (20 °C h−1), for 2 h. They were named Pt/C, Pd/C, and Rh/C.
The catalysts were activated by heating (10 °C min−1) up to the desired temperature (reduction temperatures between 250 °C and 450 °C were tested) under H2 flow (50 Ncm3 min−1, delivered by Praxair, Madrid, Spain, minimum purity of 99.999%) for 2 h.

3.2. Catalysts Characterization

N2 adsorption-desorption analysis were performed at −196 °C (Tristar II 3020, Micromeritics, Alcobendas, Spain) to characterized the porous texture of the catalysts. Previously, the samples were outgassed for 12 h at 150 °C (VacPrep 061, Micromeritics, Alcobendas, Spain). The BET equation was used to determine the surface areas.
The metal content (platinum, palladium and rhodium) of the synthesized catalysts was determined by ICP-MS with an Elan 6000 (Perkin-Elmer, Tres Cantos, Spain). Previously, the samples were dissolved in HNO3:3HCl, and digested for 15 min at 180 °C in a microwave oven (Milestone Ethos Plus, Madrid, Spain).
Metal dispersion was determined by CO chemisorption (PulseChemiSorb 2705, Micromeritics, Alcobendas, Spain), assuming a stoichiometry of 1:1 for the adsorption of the CO molecules on the metallic atoms [43,44,45,47].
The elements present on the surface of the catalysts and their concentrations were determined by XPS (5700C Multitechnique System, Physical Electronics, Madrid, Spain), scanning up to a binding energy (BE) of 1200 eV, using Mg-Kα radiation (1253.6 eV). In order to rectify the shift in BE produced by sample charging, the C 1s peak (284.6 eV) was used as an internal standard. To estimate the chemical state of Pt, Pd, Rh and O on the catalyst surface, the BE of the O 1s, Pt 4f7/2, Pd 3d5/2, and Rh 3d5/2 core levels and the full width at half maximum data were used, deconvoluting the peaks by mixed Gaussian–Lorentzian functions (least-squares method) [48].
TEM was carried by a JEOL JEM-3000F microscope (300 kV, point resolution of 0.17 nm, Madrid, Spain), equipped with a high-angle annular dark field (HAADF) detector and a 1k x 1k ULTRASCAN multi sweep CCD camera. Chemical analysis was done by Energy Disperse X-ray Spectroscopy (XEDS) using an Oxford Instruments INCA Energy TEM 250 (Madrid, Spain). Previously, the catalysts were dispersed in ethanol and placed onto holey carbon-coated Cu grids (Aname, Madrid, Spain).
The XRD patterns of the catalysts at different reduction temperatures (250, 350 and 450 °C) were driven in a X’Pert PRO Panalytical Diffractometer (Madrid, Spain), scanning up to a 2θ of 100° (step size of 0.020°, 5s collection time), using CuKα monochromatic radiation (k = 0.15406 nm) and a Ge mono filter.

3.3. Catalytic Activity Experiments

The HDC experiments were performed in a Microactivity Pro (Tres Cantos, Spain) reaction system described previously [49], consisting of a quartz fixed bed micro-reactor operating under continuous flow. In order to analyze the reaction products, the system was coupled to a gas-chromatograph with a flame ionization detector (FID).
The experiments were conducted at atmospheric pressure. The total flow rate (DCM + H2 + N2) used was 100 Ncm3 min−1. Finally, a DCM inlet concentration of 1000 ppmv and a H2/DCM molar ratio of 100 were employed. Reaction temperatures of 150–250 °C were evaluated. All the experiments were performed by triplicate, using a space-time (τ) of 0.6 kg h mol−1.
The catalysts were evaluated in terms of overall dechlorination, metallic intrinsic activity or TOF, DCM conversion and selectivity to the different reaction products.

4. Conclusions

From the results obtained it follows that Pd is more prone than Pt and Rh to sintering and, therefore, increasing the reduction temperature provokes a dramatic decrease of activity, leading to poor dechlorination of DCM even at the highest reaction temperature investigated (250 °C). Sintering was of lower significance in the case of Pt and almost did not occur with Rh. On the other hand, by increasing the reduction temperature, the ratio of zero-valent to electro-deficient species increased significantly in the Pd/C catalyst and to a lower extent in Pt/C, while remaining basically unchanged in Rh/C. This led to a significant increase of TOF in Pt/C since in this catalyst Pt0 is the main active specie for HDC, thus compensating for the loss of dispersion at a higher reduction temperature. In contrast, the decrease of Pdn+ (main active center for Pd/C) together with the significant decrease of dispersion caused a remarkable drop of TOF and overall dechlorination. Meanwhile, no significant changes occurred in the case of Rh/C consistently with its stable properties upon reduction at different temperatures. This higher stability of Rh/C can be ascribed to a higher concentration of surface oxygen groups, particularly of basic character, which favors the metal-support interaction, avoiding metal sintering and protecting the electro-deficient species.
It can be concluded that 250 °C is the optimum reduction temperature for Pd/C, while for Pt/C better results were obtained after reduction at 450 °C, and no significant effects were observed in the case of Rh/C.

Supplementary Materials

The following are available online at https://www.mdpi.com/2073-4344/8/12/664/s1, Figure S1. XPS deconvolution of Pt 4f on Pt/C catalyst reduced at: 250 °C (A), 300 °C (B), 350 °C (C), 400 °C (D) and 450 °C (E); Figure S2. XPS deconvolution of Pd 3d on Pd/C catalyst reduced at: 250 °C (A), 300 °C (B), 350 °C (C), 400 °C (D) and 450 °C (E); Figure S3. XPS deconvolution of Rh 3d on Rh/C catalyst reduced at: 250 °C (A), 300 °C (B), 350 °C (C), 400 °C (D) and 450 °C (E); Figure S4. XPS spectra of O 1s on Pt/C catalyst reduced at different temperatures; Figure S5. XPS spectra of O 1s on Pd/C catalyst reduced at different temperatures; Figure S6. XPS spectra of O 1s on Rh/C catalyst reduced at different temperatures; Table S1. Initial conversions and selectivities to reaction products in the HDC of DCM with Pt/C catalyst reduced at different temperatures; Table S2. Initial conversions and selectivities to reaction products in the HDC of DCM with Pd/C catalyst reduced at different temperatures; Table S3. Initial conversions and selectivities to reaction products in the HDC of DCM with Rh/C catalyst reduced at different temperatures.

Author Contributions

Conceptualization, J.J.-R. and L.M.G.-S.; investigation, A.A.-B. and M.M.-M.; methodology, A.A.-B., M.M.-M. and M.A.Á.-M.; data analysis, A.A.-B., M.M.-M, M.A.A.-M, J.J.-R. and L.M.G.-S.; supervision, M.A.Á.-M., J.J.-R. and L.M.G.-S.; writing—original draft preparation, A.A.-B. and M.M.-M.; writing—review and editing, M.A.Á.-M., J.J.-R. and L.M.G.-S.

Funding

The authors gratefully acknowledge financial support from the Spanish Ministerio de Economía y Competitividad (MINECO) through the projects CTM 2014-53008 and CTM2017-85498-R. A. Arevalo Bastante acknowledges MINECO for her research grant. M. Martín Martínez acknowledges the postdoc grant 2017-T2/AMB-5668 from Comunidad de Madrid, Programme “Atracción de talento investigador”.

Conflicts of Interest

The authors declare no conflict of interest.

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Catalysts 08 00664 g001 550
Figure 1. Deconvolution of O 1s spectra of Pd/C catalyst reduced at 300 °C.
Figure 1. Deconvolution of O 1s spectra of Pd/C catalyst reduced at 300 °C.
Catalysts 08 00664 g001
Catalysts 08 00664 g002 550
Figure 2. TEM images (left) and metal particles size distributions (right) of catalysts reduced at 450 °C: (A) Pt/C; (B) Pd/C; (C) Rh/C.
Figure 2. TEM images (left) and metal particles size distributions (right) of catalysts reduced at 450 °C: (A) Pt/C; (B) Pd/C; (C) Rh/C.
Catalysts 08 00664 g002
Catalysts 08 00664 g003 550
Figure 3. XRD diffractograms of: (A) Pt/C; (B) Pd/C; (C) Rh/C.
Figure 3. XRD diffractograms of: (A) Pt/C; (B) Pd/C; (C) Rh/C.
Catalysts 08 00664 g003
Catalysts 08 00664 g004 550
Figure 4. Results on the HDC of DCM within 150–250 °C reaction temperatures, at 0.6 kgcat·h·mol−1 space-time, with the Pt/C catalyst reduced at different temperatures.
Figure 4. Results on the HDC of DCM within 150–250 °C reaction temperatures, at 0.6 kgcat·h·mol−1 space-time, with the Pt/C catalyst reduced at different temperatures.
Catalysts 08 00664 g004
Catalysts 08 00664 g005 550
Figure 5. Results on the HDC of DCM within 150–250 °C reaction temperatures, at 0.6 kgcat·h·mol−1 space-time, with the Pd/C catalyst reduced at different temperatures.
Figure 5. Results on the HDC of DCM within 150–250 °C reaction temperatures, at 0.6 kgcat·h·mol−1 space-time, with the Pd/C catalyst reduced at different temperatures.
Catalysts 08 00664 g005
Catalysts 08 00664 g006 550
Figure 6. Results on the HDC of DCM within 150–250 °C reaction temperatures, at 0.6 kgcat·h·mol−1 space-time, with the Rh/C catalyst reduced at different temperatures.
Figure 6. Results on the HDC of DCM within 150–250 °C reaction temperatures, at 0.6 kgcat·h·mol−1 space-time, with the Rh/C catalyst reduced at different temperatures.
Catalysts 08 00664 g006
Table
Table 1. BET surface area (m2·g−1) of the catalysts reduced at different temperatures.
Table 1. BET surface area (m2·g−1) of the catalysts reduced at different temperatures.
Tred (°C)Pt/CPd/CRh/C
250123612001210
350126612461253
450124712511209
Table
Table 2. Dispersion values, surface metal (MXPS) and oxygen (OXPS) atomic concentrations, relative distribution of the surface metallic species (M0/Mn+) and OCOOH/Ototal ratios of the catalysts reduced at different temperatures.
Table 2. Dispersion values, surface metal (MXPS) and oxygen (OXPS) atomic concentrations, relative distribution of the surface metallic species (M0/Mn+) and OCOOH/Ototal ratios of the catalysts reduced at different temperatures.
CatalystTredDispersionMXPSM0/Mn+OXPSOCOOH/Ototal
Pt/C250280.062.85.050.20
300260.072.96.700.21
350230.053.24.110.20
400190.065.14.110.22
450120.077.54.350.23
Pd/C250230.081.05.650.28
300220.091.34.960.29
350160.131.54.960.27
400130.092.44.890.34
450100.082.43.930.36
Rh/C250511.50.76.860.12
300481.50.86.640.11
350491.40.86.860.12
400481.40.97.000.12
450451.30.96.460.13

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Arevalo-Bastante, A.; Martin-Martinez, M.; Álvarez-Montero, M.A.; Rodriguez, J.J.; Gómez-Sainero, L.M. Properties of Carbon-supported Precious Metals Catalysts under Reductive Treatment and Their Influence in the Hydrodechlorination of Dichloromethane. Catalysts 2018, 8, 664. https://doi.org/10.3390/catal8120664

AMA Style

Arevalo-Bastante A, Martin-Martinez M, Álvarez-Montero MA, Rodriguez JJ, Gómez-Sainero LM. Properties of Carbon-supported Precious Metals Catalysts under Reductive Treatment and Their Influence in the Hydrodechlorination of Dichloromethane. Catalysts. 2018; 8(12):664. https://doi.org/10.3390/catal8120664

Chicago/Turabian Style

Arevalo-Bastante, Alejandra, Maria Martin-Martinez, M. Ariadna Álvarez-Montero, Juan J. Rodriguez, and Luisa M. Gómez-Sainero. 2018. "Properties of Carbon-supported Precious Metals Catalysts under Reductive Treatment and Their Influence in the Hydrodechlorination of Dichloromethane" Catalysts 8, no. 12: 664. https://doi.org/10.3390/catal8120664

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