Sulfided NiMo/Clinoptilolite Catalysts for Selective Sulfur Removal from Naphtha Stream without Olefin Hydrogenation

The natural clinoptilolite zeolite has been modified by acid leaching with HNO3 in order to obtain economic material for supporting NiMoS hydrotreating catalysts. The most optimized zeolite material was obtained by leaching with HNO3 at 80°C during 24 h. The bimetallic NiMo catalysts prepared by wet impregnation of a zeolite support, followed by calcination and sulfidation, were characterized by several physico-chemical techniques and tested in the hydrodesulfurization (HDS) of 3-methyl-thiophene (3-MT) model feed at atmospheric H2 pressure and T = 280°C. For all catalysts, the 3-MT transformation mainly occurs via direct desulfurization reaction route being diminished the catalyst hydrogenation function. This was linked with the formation of highly stacked layers of MoS2 particles having a low amount of “brim sites,” as demonstrated by HRTEM. The cause of the best performance of Ni-Mo(H)/Z-1 sulfide catalyst in the HDS of 3-MT can be the presence of K+ impurities on the support surface which forces the formation of highly stacked layers of MoS2 particles.


Introduction
The use of suitable natural zeolites for supporting heterogeneous catalysts is economically attractive option in many countries possessing abundance of natural zeolites [1]. Among these zeolites, the clinoptilolite is of considerable interest due to its effective high cation exchange capacity, unique crystal and pore structure, chemical stability in corrosive media, and thermostability [2]. Clinoptilolite has a cage-like structure consisting of SiO 4 and AlO 4 tetrahedral units joined by oxygen atoms. The native charges of the AlO 4 units are balanced by Mg, Ca, Na, K, and/or Fe cations. Moreover, its textural and acid properties should be improved by elimination of the extraframework cations, for example, by chemical leaching [3][4][5].
Clinoptilolite is crystalline aluminosilicate mineral which exhibits large number of acid sites distributed through the network of channels and cavities 2. Experimental

Modification of the original Clinoptilolite by acid treatment
The natural zeolite used for supporting NiMo catalysts was a natural clinoptilolite zeolite from the Cuitzeo area deposit (Michoacán, Mexico). For more details on the physicochemical features of this natural mineral, the reader is addressed to Ostrooumov et al. and Huirache-Acuña et al. [3,23]. Prior to acid leaching, the clinoptilolite zeolite was crushed and sieved to obtain particle size <297 mesh. Then, the zeolite was washed with deionized water and dried at 80°C overnight. Element composition of the natural zeolite was investigated by Huirache-Acuña et al. [23].
The acid leaching with 1 M nitric acid (with a proportion of 10 mL of solution per gram of zeolite) was performed at 80°C under stirring for either 24or 48 h. Those zeolite materials will be denoted hereafter as Z-1 and Z-2, respectively. After filtering, the solid was washed repeatedly with excess of distilled water until all traces of nitric acid were removed. Then, the solids were dried at 110°C for 14 h and calcined at static air conditions at 500°C for 5 h.

Preparation of bimetallic NiMo (x) /Clinoptilolite catalysts
All oxide catalyst precursors were prepared by co-impregnation taking into account the isoelectric points (PIZ) of Z-1 and Z-2 supports. The measurements of isoelectric points of the clinoptilolite zeolite confirmed that zeolite leaching with HNO 3 during different times (24 and 48 h) led to very small change of the isoelectric point (Figure 1). An aqueous solutions of ammonium molybdate tetrahydrate (H 24 Mo 7 N 6 O 24 .4H 2 O) and nickel acetate tetrahydrate (C 4 H 6 NiO 4 ·H 2 O) were used as molybdenum and nickel precursors, respectively. The corresponding amount of the metal salts of Mo and Ni were dissolved separately at room temperature in 5 mL of deionized water taking into account the isoelectric point of each zeolite. After impregnation, the catalysts were dried overnight in air at 110°C and then calcined at 500°C for 3 h. The catalysts were prepared with similar nickel loading and different Mo contents ( Table 1). The samples with low, medium, and high molybdenum loadings are denoted hereafter as NiMo (L) /Z-1(2), NiMo (M) /Z-1(2), and NiMo (H) /Z-1(2), respectively.

Characterization techniques
The isoelectric points (PIZ) of the clinoptilolite zeolite modified with different treatments were measured on a Zeta-Meter System 3.0 containing a cell electrophoretic acrylic type II-grape and platinum electrodes. Surface morphology analysis of the pure zeolites and oxide catalysts precursors was studied by SEM technique using a JEOL JSM-6060 LV microscope. The accelerating voltage employed was 15 kV. Elemental analysis was performed by Energy Dispersive X-ray Spectroscopy (EDS) Oxford Inca X-Sight coupled to a MT 1000, Hitachi apparatus. The textural properties of the oxide precursors and bare supports were determined from the adsorption-desorption isotherms of nitrogen at −196°C, recorded with an ASAP 2420 Micromeritics V2.09 gas sorption Analyzer. Prior to the experiments, the samples were degassed under a flow of argon at 350°C for 16 h. The acidity of the oxide precursors was determined by temperature-programmed desorption (TPD) of ammonia measurements conducted on a Micromeritics 2900 equipment provided with a TCD and interfaced to a data station. The morphology of fresh sulfided catalysts was investigated by high resolution transmission electron microscopy (HRTEM) using a JEOL JEM 2000FX microscope. XPS spectra of the sulfided (10% H 2 S in H 2 , 673 K) catalyst samples were measured at room temperature using a VG Scientific LTD system equipped with a hemispherical electron analyzer and a Mg Kα (hν = 1253.6 eV) X-ray source and ultrahigh vacuum chamber. Details of the XPS measurements by this spectrometer are reported by Huirache-Acuña et al. [23].

Catalytic activity measurements
The catalyst activity was evaluated in the reaction of hydrodesulfurization of 3-methyl-thiophene (3MeT) carried out in a micro-flow reactor at 280°C upon atmospheric hydrogen pressure. The reactor was loaded with 100 mg of catalyst (particle size between the 80 and 120 mesh) diluted with 1 g of SiC. Before reaction, the catalyst was pre-sulfided at 400°C for 1 h using a gas mixture of 15% H 2 S/H 2 (flow rate of 40 mL/min). After catalyst activation, the sample was cooled down and stabilized at reaction temperature. Then, the saturation of hydrogen with 3MeT was obtained by bubbling hydrogen (70 mL min −1 ) through a saturator containing 3MeT liquid at 20°C. The flow of 3-MeT through reactor was 1.134 × 10 −6 moles × s −1 . The products obtained at steady state conditions were analyzed on line by GC. For each catalyst studied, steady state conditions were reached after 1 h of time on-stream reaction. All reaction products were analyzed online with gas chromatograph Agilent-7820, FID equipped with an Agilent 30 m HP-5 capillary column. The catalytic activity was expressed as total 3-MeT conversion obtained at steady-state conditions.

Physicochemical characterization of oxide precursors
The surface morphology of the pure Z-1 and Z-2 zeolites and their respective oxide catalyst precursors were investigated by scanning electron microscopy (SEM). The SEM micrographs in Figure 2 illustrate the influence of the different zeolite pretreatment conditions and Mo loading on the particle size and morphology of the prepared catalysts. In general, irrespectively of the time of HNO 3 treatment (24 or 48 h), both pure Z-1 and Z-2 substrates exhibit irregular and compact structure with white points resulting from the different cations impurities. After Ni and Mo oxide loading, all samples exhibit non-uniform distribution of Ni and Mo on the catalyst surface. The NiMo (H) /Z-1 appeared to have a much better distribution of the metal oxides on the support surface than its Z-2-supported counterpart. Besides its highest metal oxide loadings, the surface of both NiMo (H) /Z-1 and NiMo (H) /Z-2 catalysts were not completely covered with Ni and Mo oxides. This was confirmed by the energy-dispersive X-ray spectroscopy (EDS) analysis on the different points of the samples. SEM/EDS have shown that NiMo (H) /Z-1 and NiMo (L) /Z-2 samples are characterized by the high Al/Si ratio (5.5 and 4.7, respectively), which might indicate that mean crystalline phase is clinoptilolite [3].
The textural properties of pure Z-1 and Z-2 substrates and both oxide catalysts with highest Mo loading was studied by the N 2 physisorption at −196°C. The N 2 adsorption-desorption isotherms of both parent zeolites were similar before and after metal loadings. Figure 3(A) shows the N 2 isotherms of both catalysts. According to IUPAC classification, all samples exhibit a combination of a type I and IV isotherms which are typical for hierarchical materials having both microand meso-porous structure [24]. Indeed, the H4-type of hysteresis loop is generally observed with complex materials containing both micropores and mesopores [24]. The adsorption branch of N 2 isotherm, which does not show any limiting adsorption at high P/P 0 , is typical for natural zeolites having both micro-and meso-pores [3]. However, in case of natural zeolites, an increase of the relative pressure might favor also multilayer adsorption of nitrogen on the surface of impurities [3].
The natural acid-modified clinoptilolite zeolite contains micropores, as deduced from the shape of the N 2 sorption isotherms ( Table 2). However, the relatively low volume of micropores (in range 0.002-0.011 cm 3 ·g −1 ) point out that their large amount cannot be detected because the micropores are occupied by exchangeable cations [2].
As expected, an increase of leaching time of pristine zeolite from 24 to 48 h led to an increase of specific surface area (S BET ) from 44 to 55 m 2 ·g −1 and the total pore volume from 0.066 to 0.071 cm 3 ·g −1 ( Table 2). Simultaneously, the two-fold increase of volume of micropores occurs (from 0.006 to 0.011 cm 3 ·g −1 ) suggesting that the nitrogen access was enhanced by elimination of blocking of the pores by impurities. However, the BET specific area and total pore volume decreased again after metal loading onto surface of zeolite. In addition, the micropore volume decreases after metal oxide incorporation into both Z-1 and Z-2 supports suggesting the modification of pore opening by deposition of the large amount of the Mo species on the carrier surface ( Table 2). Figure 3(B) shows the pore size distributions (PSD) evaluated from the adsorption branch of nitrogen isotherm by using BJH method. For all catalysts, pore size distribution shows two distinct peaks: the first one, located about 3.6 nm, is due to the tensile strength effect (TSE) [25]. The second broad peak centered at 9.5 and 20.9 nm for NiMo (H) /Z-2 and NiMo (H) /Z-1, respectively, represents the Advances in Microporous and Mesoporous Materials 6 mesopores, probably intra particle porosity [26]. Noticeably, the contribution of the mesoporosity to overall catalyst porous structure is small being all catalysts mainly microporous, as deduced from the comparison of the V total and V micro values in Table 2. A comparison of the loss of S BET and normalized S BET values of the calcined NiMo (H) /Z-1 catalyst with that of NiMo (H) /Z-2 strongly suggest that the former catalyst exhibits a lower pore occlusion by guest molecules than the latter.
The acidity of the calcined catalysts was studied by temperature-programmed desorption of ammonia (TPD-NH 3 ). The TPD-NH 3 profiles of the most active catalysts are shown in Figure 4. Depending on the ammonia desorption temperature, the TPD-NH 3 profiles were mathematically fitted (Gaussian function) assuming temperature desorption ranges of 100-250°C, 250-400°C and 400-500°C, respectively, as indicative of weak, medium, and strong strength acid sites [27]. The  weak and moderate acidity are probably linked with Brønsted acid sites, whereas the strong acid sites are probably originated by Lewis acid sites [28,29]. As seen in Figure 4, the Ni-Mo (L) /Z-2 and NiMo (M) /Z-2 catalysts exhibited a larger amount of strong strength acid sites than their Z-1-supported counterparts suggesting the poorer metal oxides dispersion on the surface of those catalysts. The total concentration of acid sites (expressed as μmol NH3 per g of substrate) is shown in Table 1. In general, the catalysts supported on Z-2 zeolite exhibit larger total acidity than their counterparts supported on Z-1 zeolite. The total acidity of the oxide precursors follows the trend: NiMo (M) /Z-2 ≈ NiMo (L) /Z-2 >> others. Irrespectively of the support, the strong acid sites disappeared after loading the largest Mo amount. According to Del Arco et al. [26], XRD measurements suggest that this is probably due to

N2 adsorption-desorption isotherms of the calcined Ni-Mo (H) /Z-1(Z-2) catalysts (A) and their BJH adsorption pore size distribution (B).
formation of large MoO 3 crystallites on the support surface affecting the acidity associated with surface -OH groups.
Summarizing, taking in account all characterization data of the oxide catalyst precursors, zeolite leaching with HNO 3 during 24 h led to better support than its leaching during 48 h. This is probably because an increase of leaching time increased the support microporosity leading to a decrease of the average pore diameter ( Table 2). After zeolite leaching and further metal loading, the structure of zeolite material was maintained, as confirmed by XRD studies by Khoshbin et al. [5]. SEM mapping analysis confirmed that main part of the metal ion impurities of natural zeolite had been displaced by H + ions after zeolite leaching with HNO 3 solution at 24 and 48 h. NiMo (H) /Z-1 was the only catalyst having K + impurities on its support surface, as confirmed by SEM mapping (data not shown here) and chemical surface analysis by XPS (vide infra). Finally, the zeolite leaching with HNO 3 led to modification of the number of acid sites and their strength, as confirmed by TPD-NH 3 analysis, being more acidic the catalysts supported on zeolites leached during 24 h ( Table 1).

TEM characterizations
The HRTEM micrographs of both sulfided catalysts with highest Mo content are compared in Figure 5. Noticeably, the NiMo (H) /Z-1 exhibit a larger density of Mo sulfide particles on the surface of Z-1 zeolite than its NiMo  Table 3). Noticeably, the NiMo (H) /Z-2 exhibit much lower stacking of the MoS 2 slabs than its NiMo (H) /Z-1 counterpart (see Figure 5(B) and Table 3). Thus, both catalysts might exhibit different amounts of Mo atoms in the edge surface of molybdenum sulfide crystals [30]. To confirm this, the average fraction of Mo atoms in the edge surface of MoS 2 /MoS 1.95 crystals was calculated (see f Mo Table 3) following the method used by Gutierrez and Klimova [31]. The comparison of the f ' Mo   highly stacked and broken at the point of highest torsion. It is hypnotized that this can be due to the presence of impurities on the surface of Z-2 zeolite forcing the formation of the "onion-type" MoS 2 phase.

X-ray photoelectron spectroscopy (XPS)
Since the objective of the zeolite leaching was unblocking of its channels through dealumination and decationation, the surface exposure of undesired elements of the fresh sulfided catalysts was evaluated by XPS. For all fresh sulfided catalysts, the binding energies (BE) of same components of the zeolite carrier were: Si 2p (103.4 eV), Al 2p (74.5-75.0 eV), Fe 2p 3/2 (710.6-711.1 eV), and F 1 s (685.5-685.8 eV). Interestingly, the Si 2p core level peak of all samples was close to 103.4 eV, which is characteristic of O-Si-O bonds in SiO 2 . Thus, the chemical environment of silicon ions was not affected by the presence of Al 3+ , Fe 3+ , F − , and K + ions. Considering data shown in Table 4, the impurities present on the support surface can be K 2 Table 3.
Some HRTEM data a of the selected sulfided catalysts.  Mo loading was evaluated by comparison of the Z-1-supported catalysts. The binding energies (eV) of the principal peaks are summarized in Table 5 and the percentages of different species are given in parentheses. Concerning the Mo 3d core level spectra (not shown here), two doublet peaks containing the corresponding 3d 5/2 and 3d 3/2 components from the spin-orbit splitting suggested the presence of two types of molybdenum species. For all catalysts, the lower Mo 3d 5/2 binding energy at 228.5-228.8 eV is similar to that reported for Mo 2 S 3 phase (228.7 eV) with a Mo oxidation state of +3 [32]. Noticeably, the binding energy of the S 2p 3/2 peak observed for the NiMo (H) catalysts at 161.6-161.9 eV is a little too low to be considered of sulfide (S 2− ) ions present in the MoS 2 phase (162.4 eV) [33]. Thus, regardless of the support (Z-1 or Z-2) and Mo loading, the XPS results suggest that the sulfidation of molybdenum species located on the support surface is complete. Conversely to Mo, an important proportion of nickel species remains unsulfided, as deduced from two contributions of the Ni 2p 3/2 component: one at 852.6-853.2 eV associated with nickel sulfide species and another one at 855.9-856.0 eV due to oxidized Ni 2+ ions [34].  Table 6). This is not surprising because Z-2 exhibits a larger specific surface area than Z-1 (55 m 2 /g vs. 44 m 2 /g). By comparison of surface atomic ratios of the impurities in the Z-1 and Z-2 catalysts, one can notice higher impurities of the Z-2-based catalysts.  In contrast to Mo species, the XPS results suggest that Ni species are partially sulfided. Considering the catalyst sulfidation degree, the comparison of the S/(Ni + Mo) ratios of both catalysts strongly suggest that, on the contrary to NiMo (H) /Z-2 catalyst, the NiMo (H) /Z-1 exhibits non stoichiometric molybdenum sulfide phase. Contrary to Z-1 supported catalysts, the results of the XPS analysis show that the S:Mo ratio on the samples supported on Z-2 zeolite is higher than that found for MoS 2 ( Table 6). The excess of sulfur in those samples corresponds to elemental sulfur. This is important observation because it can explain the much better catalytic response of the NiMo (H) /Z-1 sample with respect its Z-2 supported counterpart.
In conclusion, the interpretation of the catalyst structure by XPS results appears more straightforward than by HRTEM. The main reason for difficulty of the catalyst characterization by the latter technique is related to the fact that many impurities are still present of the catalyst surface after zeolite leaching with HNO 3 which leads to a limited number of TEM zones where molybdenum and nickel sulfides are both clearly visualized.

Hydrodesulfurization of gasoline model compound
The current desulfurization technology for gasoline production requires highly selective catalysts to remove S-compounds without excessive olefins hydrogenation. The latter requirement is especially important for preservation of the research octane number (RON) [1,2]. Thus, the catalyst needed to the hydrotreating of naphtha stream needs to possess moderate hydrogenation properties. In this work, the activity and selectivity of the sulfided NiMo ( x ) /Clinoptilolite catalysts were evaluated in the hydrodesulfurization (HDS) of 3-methylthiophene (3-MeT) as gasoline model compound. The reaction was carried out in a flow reactor under atmospheric hydrogen pressure and reaction temperature of 280°C. The 3-MeT conversion was low (0.8-5.3%) in order to avoid diffusional problems and to compare the catalysts under kinetic conditions. The intrinsic 3-MeT HDS activities at 360°C of the NiMo (x) /Z-1 and NiMo (x) /Z-2 catalysts (expressed as moles of 3-MeT converted per second and gram of catalyst), under steady-state conditions and reaction temperature of 280°C, are compared in Figure 7(A). The specific reaction rate of the best catalyst (NiMo (H) /Z-1) was close to that of Ni-W/SiO 2 (60 × 10 −8 mol 3MT g −1 s −1 vs. 70 × 10 −8 mol 3MT g −1 s −1 ) tested at the same reaction temperature (280°C) [35].
Regardless of the support and metal loading, the reaction products identified by GC were; 3-methyltetrahydrothiophene (3MTHT); 2-methylbutane-1-thiol (2MBT1); 2-methyl-1,3-butadiene (isoprene); 3-methyl-1-butene (3M1B); 2-methyl-1-butene (2M1B); and 2-methyl-2-butene (2M2B). The main products detected were 2-methyl-1-butene and isoprene. The HYD/DDS selectivities ratios of the catalysis are compared in Figure 7(B). Noticeably, the hydrogenation of olefins to paraffin's did not occur because 2-methyl-1-butane (2 MB) was not produced. The possible reaction path network for the HDS of 3MeT over catalysts studied is shown in Figure 8. As seen in Figure 8 the 3-MeT transformation occurs via hydrogenation (HYD) and direct desulfurization (DDS) reaction routes. Considering the first HYD step, the double bond of 3MeT is saturated leading to formation of 3-methyl-2,3-dihydrothiophene (3M2,3DHT). This product was not detected in this work because it was quickly transformed to 3-methyl-tetrahydrothiophene (3-MTHT) and then to a mixture of 2-methyl-butane-1-tiol (2M1BT) and 3-methyl-butane-1-tiol (3M1BT) products. On the other hand, the DDS path leads to the formation of isoprene and its subsequent transformation to mixture of olefins (3M1B, 2M1B, and 2M2B). Interestingly, the formation of 2-methylbutane via hydrogenation olefins did not occur. It is important finding of this work because such hydrogenation is not desired reaction during hydroprocessing of naphtha feedstocks. Contrary to the NiW supported on SiO 2 and γ-Al 2 O 3 [35], the formation of pentenes via isomerization of the olefin mixture compounds (3M1B, 2M1B, and 2M2B) was not observed in this work. The formation of mixed olefin compounds (3M1B, 2M1B, and 2M2B) was higher over the NiMo catalysts supported on Z-1 zeolite than over the counterpart Z-2 zeolite. In general, the Z-1-supported catalysts exhibit a larger formation of those mixed olefins than their counterparts supported on Z-2. Noticeably, none of the catalyst studied exhibited the formation of totally hydrogenated products. This fact is of paramount importance for production of FCC gasoline which needs the sulfur removal without excessive olefin saturation. In general, all catalysts exhibit a decrease in HYD selectivity with increasing 3-MeT conversion, as it was observed previously for sulfided Ni-Mo catalysts supported on silica-alumina [36]. This means that in the absence of thermodynamic effects, the hydrogenolysis of 3-MeT is more favorable than hydrogenation of aromatic ring. By comparing the activity and HYD/DDS selectivities ratio of the NiMo (H) /Z-1 and NiMo (L)/ Z-1 samples in reaction at 280°C, it is clear that the increase of Mo loading led to increase of 3-MeT conversion but without changing the HYD/DDS selectivity ratio (Figure 7(B)). Interestingly, the largest HYD/DDS selectivities ratio is found by catalysts supported on zeolite Clinoptilolite leached during 48 h than their counterparts leached at 24 h.

Catalyst activity structure-correlation
The above activity results demonstrated clearly that the best catalyst was that prepared with largest Mo loading and supported on Z-1 carrier (NiMo (H) /Z-1). This raise the question of why this catalyst shows higher HDS activity than its counterpart NiMo (H) /Z-2 despite their similar nickel and molybdenum contents. To answer this question, the oxide precursors and fresh sulfided catalysts were characterized by different techniques to investigate their morphology, textural properties, acidity, and sulfidability.
In this work, the necessity of natural zeolite modification by leaching was clearly demonstrated. The objective of such leaching was to open porous structure of the natural zeolite by elimination of undesirable cations occluding the pores. For all catalysts studied, the zeolite leaching with HNO 3 during 24 h led to much better support material than its leaching during 48 h. In this sense, the pore size distribution (from N 2 physisorption measurements) confirmed that an increase of leaching time from 24 to 48 h led to an increase of the support mesoporosity, clearly observed  in the 5-35 nm region of the pore size distribution (Figure 2(A)). Both Ni and Mo sulfide phases are poorly dispersed and distributed mainly on the external zeolite surface (from XPS), although small amounts of molybdenum sulfides can be also located within the internal support porous structure. The selected zeolite leaching conditions were not so strong in order to avoid destruction of the zeolite structure. Unfortunately, the XPS characterization confirmed that using those mild leaching conditions (HNO 3 , 80°C, 24/48 h), it was impossible to eliminate totally Al 3+ , K + , Fe 3+ , and F − ions from the internal porous structure of the Clinoptilolite zeolite. In this sense, it was observed that not all ions have inhibition effect on the catalyst activity.
The higher activity shown by Ni-Mo (H) /Z-1 can be attributed to the lowest amount of extraframework (EXFAL) Al atoms occluded in the internal cavities of, as shown by lowest Al/Si atomic ratio among the catalysts studied (Table 4). Interestingly, the 3-MeT conversion at 280°C decreased linearly with an increase of Al/Si atomic ratio of Z-1-supported samples. This is probably because the occlusion of Al atoms in the cavities of zeolite increased the catalyst acidic properties favoring the catalyst deactivation induced by acid sites. The best catalytic response of the NiMo (H) /Z-1 catalyst can be linked also to the presence of K + cations decorating support surface, as this was unique sample among all catalysts studied having K + ions on the support surface ( Table 4). Similar observation was reported previously for the CoMo HDS catalysts supported on aluminosilicate doped with Na [37]. In addition, the presence of potassium species on the catalyst surface might increase the dispersion of Mo phase as well as to influence the coordination state of Mo 6+ and Ni 2+ ions in this sample, as it was observed by Raman spectroscopic study [38]. In this sense, it was found that the Ni-Mo/γ-Al 2 O 3 sample doped with K + exhibited a lower amount of polymeric Mo-O species because potassium provoked their partial transformation into monomeric Mo 6+ (Th) ones. The formation of new complex K-Ni-Mo-O species was proposed [38]. In line with this, it has been found that, contrary to tetrahedral nickel species, the formation of octahedral nickel species in the oxide precursor was beneficial for catalyst activity. Finally, the SEM characterization of the fresh sulfided NiMo (H) /Z-1 catalyst suggested the formation of the nonstoichiometric MoS 1.95 phase, which was postulated as be far more active than the stoichiometric MoS 2 [39]. This is because of anionic vacancies in the molybdenum sulfide lattice of the latter compound with respect to the stoichiometric one. Thus, the deliberate synthesis of a nonstoichiometric MoS 2 is desirable. In addition, the NiMo (H) Z-1 catalyst contain a larger amount of Mo atoms in the edge surface of the MoS 2 /MoS 1.95 crystals than its Z-2-supported counterpart, as deduced from HRTEM ( Table 3). As a consequence, the DDS route of 3MeT transformation have been favored without excessive olefins hydrogenation, as deduced from its lowest HYD/DDS ratio among the catalysts studied (Figure 7(B)).

Conclusions
The HDS of 3-methylthiophene (3MeT) over NiMo sulfide catalysts supported on natural Mexican zeolite (Clinoptilolite) modified by treatment with HNO 3 during 24 and 48 h was performed in a flow reactor under atmospheric hydrogen pressure. The best catalyst was the one loaded with a largest Mo wt.% and supported on HNO 3treated zeolite during 24 h. The HDS activities of the catalysts were clearly influenced by the forms of MoS 2 slabs, being formation of "onion-type" MoS 2 negative for the catalyst activity. Respect to selectivity, the results indicated that catalysts prepared on Z-1 zeolite had lowest hydrogenation ability, in comparison with the counterpart catalysts supported on Z-2 zeolite. The higher olefin formation on catalysts supported on Z-1 zeolite could be interesting for the tailoring novel catalysts since they could be catalysts for the production of gasolines with a greater octane number.