MoS2 hydrodesulfurization (HDS) catalysts promoted with Co supported on SBA-15 were synthesized from sulfur-containing Mo sources [ammonium thiomolybdate (ATM), and tetramethylammonium thiomolybdate (TMATM)] and Co complexes cobalt dimethylthiocarbamate by using different synthesis strategies in order to achieve active catalysts. The (Co)-MoS2/SBA-15 catalysts were characterized with X-ray diffraction, N2-physisorption and High-Resolution Transmission Electron Microscopy. The catalytic performance in the HDS reaction of dibenzothiophene was examined at T = 623 K and P H2 = 3.4 MPa. The results of the experiments suggest that the sequence of impregnation steps has no significant influence on the HDS activity. On the other hand, the use of different thiomolybdate precursors significantly affects the catalytic activity. The catalysts derived from TMATM show lower HDS activities compared to the catalysts synthesized from ATM which is probably due to the presence of pronounced pore blocking as well as the generation of big needle-like aggregates of the Co–MoS2 phase. It seems that the formation of intermediate MoS3 is not a prerequisite for the generation of catalytic active CoMoS phases. The high activity and high selectivity for the direct desulfurization pathway of catalysts prepared with ATM despite the large MoS2 stacking could be due to the generation of a large number of coordinately unsaturated sites.
Cobalt promoted molybdenum sulfide catalysts supported on mesoporous SBA-15 were prepared by an all sulfide route using sulfur-containing Mo and Co complexes. High catalytic activity at high Mo loading is observed for Co–MoS2/SBA-15 catalysts derived from ammonium thiomolybdate despite a pronounced stacking of MoS2 slabs. The catalysts prepared with tetramethylammonium thiomolybdate show lower HDS activities probably due to a pronounced pore blocking as well as the generation of big needle-like aggregates of the Co–MoS2 phase. The sequence of impregnation steps has no significant influence on the HDS activity. It seems that the occurrence of intermediate MoS3 is not necessary for the generation of catalytic active Co–MoS phases.
Environmental regulation requires lower content of sulfur in diesel engine fuel to 50 ppm by the year 2005 and the sulfur content will be probably reduced even further in the near feature. This worldwide environmental pressure on fuel manufacturing has awoken a renewed interest in the preparation of more efficient hydrotreating catalysts. Various preparation methods have been applied to obtain hydrotreating catalysts including comaceration , homogenous sulfide precipitation  and thiosalt decomposition . Traditionally, hydrodesulfurization (HDS) catalysts contain Mo or W sulfides supported on alumina and promoted with Co or Ni. Recently, mesoporous SBA-15 has been studied as catalyst support material due to the larger pores, thicker pore walls and higher hydrothermal stability compared to other silica molecular sieves such as HMS or MCM-41 . Indeed, Vradman et al. demonstrated the excellent potential of high loading Ni-W/SBA-15 catalysts for deep hydrotreatment of petroleum feedstocks . These catalysts were prepared by ultrasonication deposition of WS2. SBA-15 supported Mo, CoMo and NiMo catalysts was also found by Rao et al. to present higher HDS activity compared to alumina supported catalysts prepared in a similar manner . Further, SBA-15 can be easily modified with various hetero-atoms like Al, Ti and Zr. It was reported by Klimova et al., Rao et al. and Fierro et al. that modified SBA-15 supports exhibit stronger metal–support interactions with respect to pure SBA-15 yielding a high dispersion of the deposited Ni(Co) and Mo active species and consequently greater activity in the HDS [7–10]. In the majority of cases these catalysts were prepared via an oxide route, i.e., SBA-15 was impregnated with transition metal salts like ammonium heptamolybdate, nickel (cobalt) nitrate or nickel (cobalt) acetate and these materials were the calcined to produce stable oxides. Finally, the oxide catalysts were then activated either prior to (ex situ) or during the start-up (in situ) of the hydrotreatment process. However, the calcination step can cause a loss of active metals on the support and a complete sulfidation of the active phase is difficult to achieve . Recently, we reported the synthesis and catalytic performance of SBA-15 supported Co–Mo sulfide catalysts derived from ammonium thiomolybdate (ATM) . The catalysts activated by a gas mixture H2/N2 (H2 = 10%) showed a higher HDS activity compared to a commercial CoMo/γ-Al2O3 material, despite the pronounced MoS2 stacking and the presence of long MoS2 slabs. Cobalt acetate has been applied as the Co source and the precursor was sulfided in a H2S atmosphere to form CoS x /SBA-15 prior to the impregnation with the Mo compound. Moreover, the cobalt sulfide Co9S8 was easily detected by X-ray powder diffractometry. In the literature [13–15] it has been reported that the sequence of the formation of the metal sulfides has an important effect onto the development of HDS catalysts. Complexation of Co and Ni with a chelating agent retards the sulfidation of Co and Ni promoters beyond the sulfidation of the Mo species, leading to efficient promotion of the MoS2 phase and a reduced formation of bulk Co or Ni sulfides. These observations encouraged us to apply a cobalt complex (cobalt dimethylthiocarbamate, CoDMTC) as a precursor instead of Co acetate or Co nitrate for the synthesis of Co promoted MoS2 catalysts hoping that the generation of less active binary Co sulfide phases will be inhibited by this new approach.
The objectives of the present work are to explore the HDS activity of Co–Mo catalysts supported on mesoporous SBA-15, which were synthesized from S containing Mo sources ATM (TMATM) and the S containing Co complex CoDMTC. The synthesis strategy presented here allows the decomposition of the precursor materials in a H2/N2 (H2 10%) gas flow avoiding the usage of toxic H2S. In general, consecutive impregnation of the support with Co and Mo sources was carried out whereas first CoDMTC was applied followed by the Mo source. Experiments were also performed with impregnation of the material with CoDMTC after the formation of (Co)Mo sulfides on SBA-15. The different syntheses should allow monitoring the influence of the impregnation order onto the HDS activity of the materials. The supported catalysts were characterized by X-ray diffractometry (XRD), nitrogen physisorption using the Brunauer, Emmett and Teller method (BET) and High-Resolution Transmission Electron Microscopy (HRTEM).
Synthesis of Pristine Mesoporous SBA-15
Eight grams of poly(ethyleneglycol)-block-poly(propyleneglycol)-block-poly(ethyleneglycol) triblock copolymer (Aldrich, pluronic, P-123) was dissolved in 240 g of water and 28.6 g of concentrated hydrochloric acid at 303 K on a water bath. After drop wise addition of 16 g of tetraethyl-orthosilicate, the reaction mixture was stirred for 24 h at 303 K. The resulting gel was transferred into a Teflon bottle and heated to 353 K to obtain SBA-15 with 6 nm pores. The resulting white powder was filtered and washed with deionized water, and the surfactant was removed by Soxhlet extraction at 351 K with a mixture of 970 mL of ethanol and 30 mL of concentrated hydrochloric acid. After washing with ethanol, the white powder was dried at room temperature under vacuum for about 1 week.
Synthesis of Co–MoS2/SBA-15
Typically, 2 g of SBA-15 was stirred for 4 h in 100 mL of a saturated CoDMTC chloroform solution. Afterwards, the solid was obtained by filtration and the product CoDMTC/SBA-15 was dried under vacuum over night. The precursor material CoDMTC/SBA-15 was stirred in 150 mL of saturated aqueous solutions of ATM at 298 K or (TMATM at 328 K). After 4 h of stirring the products were filtered without washing and then they were activated at 773 K for 3 h under a H2/N2 (H2, 10%) gas flow at atmospheric pressure. The impregnation/activation cycle was carried out twice to prepare Co–MoS2/SBA-15 catalysts with higher Co and Mo loading. Catalysts are named according to their metal loading and type of precursors employed as, e.g., Co(X)Mo(Y)/SBA-15(A) (X is wt% Co and Y is wt% Mo loading, respectively, and A means catalysts prepared from ATM). Co(X)Mo(Y)/SBA-15(B) (B means catalysts synthesized from TMATM).
Two additional samples were prepared through post-impregnation with CoDMTC. The first one was prepared to enhance the Co concentration of Co–MoS2/SBA-15. Co–MoS2/SBA-15 which has been prepared in the above described way using ATM as precursor was treated with 100 mL of a saturated CoDMTC chloroform solution and the product was then activated under the above mentioned conditions. The second catalyst was prepared as follows: 2 g SBA-15 was stirred in 150 mL of saturated aqueous solution of ATM at 298 K. After filtration, the catalyst was calcined at 773 K for 3 h in a H2/N2 (H2, 10%) gas flow at atmospheric pressure. The MoS2/SBA-15 was treated with a saturated chloroform solution of CoDMTC. After filtration the catalyst was activated applying the above mentioned conditions. These two catalysts are denoted as Co(X)Mo(Y)/SBA-15(C).
For comparative purposes, two unsupported catalysts were prepared as follows: mixtures of the ATM (TMATM) and CoDMTC were manually ground in an agate mortar and Co/Mo ratios were kept at 0.2. The products were then decomposed in a H2/N2 (H2, 10%) atmosphere at 773 K for 3 h. These two catalysts are designed as CoMo(ATM) and CoMo(TMATM).
X-ray diffraction patterns were measured on a Siemens D5000 diffractometer at room temperature using CuKα radiation (λ = 0.154056 nm). Nitrogen adsorption measurements were carried out at 77 K on a Quantachrom Autosorb-1. Samples were degassed under flowing argon at 473 K for 2 h before N2 adsorption. The BET surface areas were calculated from p/p 0 = 0.03-0.3 in the adsorption branch. The chemical composition of the catalysts (in wt%, average of five measurements at different points of the sample) was determined with energy dispersive X-ray spectroscopy (EDS) analysis with a Philips ESEM XL 30 microscope.
High-Resolution Transmission Electron Microscopy and SAED were performed with a Philips CM 30ST microscope (300 kV, LaB6 cathode, C S = 1.15 mm). A perforated carbon/copper net served as support of the particles of Co–MoS2/SBA-15 (6 nm). SAED patterns were obtained using a diaphragm which limited the diffraction to a circular selected area (diameter 250 nm). All images were recorded with a Gatan Multiscan CCD camera and evaluated (including Fourier analyses) with the program Digital Micrograph 3.6.1 (Gatan). EDS analyses were performed in the nanoprobe mode of CM30ST with a Si/Li detector (Noran, Vantage System).
Hydrodesulfurization of dibenzothiophene (DBT) was carried out in a Parr model 4522 high-pressure batch reactor. 1.0 g of the catalyst and 150 mL of the freshly prepared solution of DBT in decaline (5% wt/wt., [DBT]0 = 0.2388 mol/L) were introduced in the reactor. The reactor was then purged and pressurized to 3.4 MPa (490 psi) with hydrogen and then heated up to 623 K at a rate of 10 K/min and continuous stirring of 600 rpm. After reaching the working temperature, the products were collected for chromatographic analysis every half an hour to determine the conversion-time dependence during 5 h. After the reaction, the used catalysts were filtered, washed and stored in inert atmosphere. The reaction products were analyzed using a Perkin-Elmer Auto-system chromatograph with a 9 feet long × 1/8 inch diameter packed column containing chromosorb W-AW 80/100 mesh 3% OV-17 (phenyl methyl silicone 50% phenyl) as a separating phase.
The HDS of DBT occurs by two parallel reaction pathways : (I) direct desulfurization (DDS) via C–S bond cleavage and (II) hydrogenation (HYD). The obtained main products are biphenyl (BP, via DDS), cyclohexylbenzene (CHB, via HYD) and tetrahydrodibenzothiophene (TH-DBT, via HYD). The ratio between HYD and DDS can be approximated in terms of the experimental selectivity according to the following equation:
The rate constant was determined from the DBT conversion as function of time assuming that DBT conversion being a pseudo-zero order reaction  by using of following equation:
where Χ DBT is the fraction conversion of DBT, η DBT = moles of DBT, k = pseudo zero order rate constant, t = time in seconds and k/η DBT,0 is the slope. The mean standard deviation for catalytic measurements was ca. 2.5%.
X-ray diffraction patterns of SBA-15 and Co–Mo sulfide catalysts supported on SBA-15 are displayed in Fig. 1. For all samples a prominent diffraction peak at about 1.0° 2θ and two distinct weaker reflections between 1.5° and 2.0° 2θ are observed which are the characteristic reflections (100), (110) and (200) of SBA-15 with space group p6 mm. The occurrence of the characteristic peaks for all catalysts indicates that loading with Co and Mo species does not deteriorate the primary mesostructure of the SBA-15 support. In addition, the intensity of these diffraction peaks (Fig. 1) decreases after the Co and Mo incorporation. The reduction of the intensity can be explained by the strong absorption of X-rays by Mo(Co) and/or a partial loss of the high order of the mesostructure. The same phenomenon was observed in previous studies [9, 12, 19].
In Fig. 2 the XRD patterns of Co–Mo sulfide catalysts supported on SBA-15 are displayed for the 2θ range from 7° to 75°. The broad modulation at about 22° 2θ is caused by the amorphous silica. For all catalysts typical diffraction patterns of poorly crystalline 2H–MoS2 with the characteristic reflections at 14.4, 33, 40 and 58° 2θ are observed. The asymmetric shape on the low angle side of the reflections at 33°, 40° and 58° 2θ is a typical feature of layered materials with a partial turbostratic disorder [12, 20]. The average MoS2 particle size can be determined from the peak width (full width at half maximum, FWHM) and the reflection position using the Scherrer formula, d = 0.941λ/B cosθ B, where d is the mean diameter of the particle, λ is the wavelength of the Cu Kα1 line, θ B is the angle between the incident beam and the reflecting lattice plane and B is the width of the diffraction peak. Using the (002) reflection, the mean MoS2 particle size is estimated to be 3–4 nm (Table 1), which corresponds to an average of five to six stacked MoS2 layers along the c-axis assuming 0.613 nm for the MoS2 slabs. The size of the MoS2 nanocrystals is smaller than the pore diameter of the SBA-15 material (ca. 6 nm) and it can be assumed that the MoS2 particles are located inside the channels of SBA-15. From the data compiled in Table 1 it is obvious that the size of the MoS2 nanocrystals increases with increasing Mo loading. Interestingly, the catalysts derived from the TMATM precursor present somewhat smaller MoS2 particles compared to the catalysts obtained from ATM. Furthermore, the introduction of Co by post-impregnation seems to have minor influence onto the crystallinity of the MoS2 particles (Fig. 2d). Independent of the Co content no reflections corresponding to cobalt sulfides can be detected (Fig. 2), indicating that Co is very well-dispersed on the catalytically active material.
The N2 adsorption–desorption isotherms (77 K) of the materials are illustrated in Fig. 3. For all Co–MoS2/SBA-15 catalysts a type IV isotherm is observed, which is the typical feature for mesoporous materials, evidencing that the incorporation of Co and Mo species does not destroy the mesoporous structure of SBA-15. Particularly, the loading of Co–Mo sulfides derived from TMATM led to a typical ink-bottle shape  [Fig. 3c, Co(1.5)Mo(11)/SBA-15(B)] caused by small Co–Mo sulfide particles settling within the mesopores. The mean pore diameter is shifted marginally toward higher values after introduction of Mo and Co in SBA-15 suggesting minor changes occurring after the introduction of Mo and Co. A similar phenomenon was described in previous reports [8, 12]. The specific surface areas of SBA-15 and the Co–MoS2/SBA-15 catalysts are summarized in Table 1. The normalized surface areas were calculated considering dilution effects of the metal loading as described in . The impregnation of the SBA-15 pores with Co–Mo sulfides results in a decrease of surface areas which is caused by a partial pore blocking by the Co–MoS2 phases, because the formation of Mo and Co sulfides inside the channels of the SBA-15 material should not significantly affect the surface areas due to their high density. A more pronounced blocking of the pores is observed for the catalysts prepared with TMATM, which exhibit the lowest normalized surface areas (Table 1). Moreover, comparing the results obtained for Co(1.5)Mo(11)/SBA-15(A) and Co(1.5)Mo(11)/SBA-15(C) it is obvious that the sequence of the impregnation steps has only a small influence onto the alteration of the surface area. An increase of the Co promoter concentration from 2.5 wt% (Co(2.5)Mo(20)/SBA-15(A)) to 4 wt% (Co(4)Mo(20)/SBA-15 (C)) yields no significant change of the surface area (Table 1).
Transmission Electron Microscopy
The hexagonal mesostructure of the SBA-15 support is preserved after all impregnation procedures, however, the samples prepared from ATM and TMATM exhibit distinct real structure phenomena. Both Co(4)Mo(20)/SBA-15(A) and Co(2.5)Mo(20)/SBA-15(A) obtained from ATM are characterized by a high density of slabs with a low aspect ratio dispersed on the SBA-15 support (Fig. 4). EDS analyses indicate the presence of the slabs by strong peaks of Mo–K and S–K (coinciding with Mo–L) and weak intensity assigned to Co–K. The ratio of Mo:S was calculated to be close to 0.5 in many cases. SAED patterns recorded on the SBA-15 particles show broad diffuse rings with the diameters in good agreement to calculated values based on the metrics of Co–MoS2 slabs. Bright-field images of these selected areas display a high density of Co–MoS2 slabs with a typical thickness of ca. 4 nm along the c-axis of a MoS2-type structure. As evidenced by HRTEM these slabs are built from five to eight consecutive (001) layers. With respect to their length, the MoS2 slabs can be separated in two groups, furthermore a characteristic spatial distribution of short and long slabs is observed (Fig. 4).
(1) Very long slabs which cover the edges of the SBA-15 particles (see arrow in Fig. 4a). The long slabs are frequently bent and exhibit prominent stacking faults. (2) Short slabs with an estimated aspect ratio between 1.5 and 3. They are usually observed apart from the edges of the support, see Fig. 4a (right) and b. HRTEM micrographs (see Fig. 4c) indicate a high density of rotationally disordered slabs with a preferred orientation along the zone axes [uv0]. Like electron diffraction patterns, the FFTs of the micrographs contain the high-intensity (002) peak of the Co–MoS2 phases, see intensity on circle 1 in Fig. 4c, right. For the Co-rich sample Co(4)Mo(20)/SBA-15(A) the slabs do not exhibit a higher Co content. The combined approach of electron diffraction and EDS analyses demonstrate that the Co excess covers wide areas of the SBA-15 support.
The distribution of short and long slabs was not observed for the samples prepared from TMATM, particularly not for the sample Co(2.5)Mo(20)/SBA-15(B). As a rule, areas like the one presented in Fig. 5a with a high density of short slabs are rarely observed. The Co–MoS2 species preferably form big needle-like aggregates of slabs (Fig. 5b). The single slabs are oriented perpendicular to the needles’ axes which coincide with the c axis of the MoS2–type structure. Figure 5c displays the HRTEM micrograph recorded on the edge of one needle shown in Fig. 5b. The attached SAED pattern was oriented like the Fourier transform of the HRTEM micrograph. The low resolution of the SAED pattern correlates with the low crystalline perfection of the needle perpendicular to c axis. Such phenomenon can be rationalized taking into account the strong bending of adjacent (001) layers which compensates stacking faults.
Catalytic Activity and Selectivity
The results of HDS activity test reactions for Co–MoS2/SBA-15 catalysts expressed as conversion of DBT as function of the reaction time are displayed in Fig. 6. The curves show an approximate linear relationship between conversion of DBT and reaction time supporting the assumption of pseudo-zero order kinetics occurring under the experimental conditions. However, deviations from the linear behavior is observed at the end of the reaction for the catalyst with high activity (Fig. 6, Co(4)Mo(20)/SBA-15(C)). Such deviations are due to an inhibiting effect of H2S accumulated in the reactor. Table 2 presents the calculated pseudo-zero order rate constants for DBT and the selectivity expressed as the ratio HYD/DDS. The results demonstrate that the impregnation order has a smaller influence onto the activity than the nature of the thiomolybdate precursor. For both supported and unsupported catalysts the materials derived from ATM reveal about 40% higher activity than the analogous samples achieved from TMATM (Fig. 6). In addition, all catalysts, regardless of the type of the thiomolybdate source, show a high selectivity at DBT conversions of ca. 30% (HYD/DDS ~ 0.2), being in good agreement with the results published in a previous study . The total DBT conversions after 5 h reaction time for all catalysts are displayed in Fig. 7 together with data taken from [12, 22] for comparison. Analyzing the results it is obvious that an increase of Mo and Co loading leads to an increase of the activity, and the catalyst with the highest Co content is the most active in the HDS reaction. With the exception of Co(1.5)Mo(20)/SBA-15(B), all SBA-15 supported catalysts exhibit higher catalytic activity than the commercial CoMo/γ-Al2O3 sample. The unsupported catalyst CoMo(ATM) has a higher HDS performance compared to the catalyst prepared from TMATM, indicating that the Mo source seems to be important also for unsupported catalysts.
The thermal decomposition of molybdenum thiosalts was applied as an alternative method for the preparation of HDS catalysts. Using Mo precursors containing alkyl groups instead of the small ammonium ion yield a new type of sulfide materials during the thermal decomposition which could be called “amorphous mesoporous sulfide” catalysts with a remarkable increase of the HDS catalytic activity [20, 23, 24]. Recently, the decomposition of ATM was successfully applied for the preparation of catalysts supported on SBA-15 . In the present study the catalytic active Co–Mo sulfides supported on SBA-15 were obtained using S containing Mo and Co sources ATM, TMATM, and CoDMTC, avoiding any step where an oxidic compound must transformed to a sulfide. In agreement with previous results , the catalysts derived from ATM exhibit interesting high activity at high metal loading despite the relatively pronounced MoS2 stacking (compare Fig. 4). Such a good HDS performance indicates the presence of a large amount of catalytic active sites, “vacancies” or co-ordinatively unsaturated sites (“CUS”). Nowadays, the most widely accepted model for the structure of promoted HDS catalysts is the model developed by Topsøe . It was reported that Co substitutes Mo atoms at the S edge creating a tetrahedral environment of Co (Co–Mo–S edge) , and it was shown for CoMoS phases that a S atom having bonds to Mo and Co is less strong bound than a S atom with bonds to two Mo atoms and therefore such a S atoms can be removed easily creating a vacancy . The presence of Co located on the MoS2 slabs confirmed by EDS analyses (see HRTEM) indicates the formation of the CoMoS phase. On the other hand it may be possible that more CUS are generated during the thermal decomposition of the ATM precursor in a H2/N2 atmosphere. A high catalytic activity of WS2 catalysts prepared by decomposition of ammonium tetrathiotungstate in H2 was reported by Wilkinson et al. to be attributed probably to the presence of more anion vacancies (or more CUS) . However, an improvement of the HDS performance could not be observed compared with the catalysts which were studied by us very recently containing crystalline Co9S8 . This finding is somewhat surprising because in the X-ray powder patterns of the present catalysts no hints for crystalline Co sulfides are found (Fig. 2). But it was also reported in the literature that segregated Co9S8 might play a distinct catalytic role according to the “Remote Control” concept . This would explain that the present catalysts exhibit a HDS activity comparable to catalysts containing crystalline Co sulfide . But the relatively high HDS activity is in agreement with the results of the study of Eijsbouts et al. , who investigated the catalytic activity of unsupported liquid-phase-sulfided Type 2 commercial ULSD catalysts. They pointed out that MoS2 stacking is not a prerequisite for a good performance and also not a sign of deactivation or lower activity.
The decomposition of TMATM leads to a somewhat lower stacking number of MoS2 slabs compared to that of ATM (Table 1, Fig. 2). But in addition, the TMATM precursor causes a more pronounced pore blocking (Table 1, Fig. 3) and this effect may be of importance for the catalytic activity. A partial blocking of the pore entrance may lead to a decrease in accessibility of the reactants to the active sites [30, 31]. Moreover, the unsupported CoMo catalyst derived from ATM presents a higher HDS activity than the material prepared from TMATM (Figs. 6, 7 histograms G and H). To explain this result one should therefore consider the different behavior of the two precursors during the thermal decomposition reaction. It was suggested that intermediately formed MoS3 plays an important role in the formation of the active catalyst supported on so-called activated-carbon . It is well-established that the thermal decomposition of ATM proceeds via intermediately formed MoS3, whereas TMATM is decomposed directly to a carbon containing Mo sulfide . In the case of Co–MoS2/SBA-15(A), CoDMTC is decomposed simultaneously during the generation of MoS2 from ATM and Co–MoS2/SBA-15(C) was prepared by post-impregnation of (Co)MoS2/SBA-15 with CoDMTC. Both synthesis methods yield catalysts with a comparable surface area. Moreover, at the same Mo and Co loading, the two catalysts present a similar HDS activity (Table 2, Fig. 6 and 7). This result indicates that the Co atoms are able to migrate directly to the edges of MoS2 to form the active CoMoS phase in both cases. The intermediate MoS3 seems to be not a prerequisite for the generation of active CoMoS phases under the actual synthesis conditions.
On the other hand, the Co promoting effect might be hindered strongly by carbon entities formed during the decomposition of a tetraalkylammonium thiomolybdate precursor , e.g. the cobalt synergetic effect could be completely suppressed like for the ex situ activated Co promoted catalyst using TMATM as Mo source . Unfortunately, the suppression of such a synergetic effect cannot be evaluated by the HRTEM imaging technique. But, the precursor type has shown a strong influence on the MoS2 morphology detected in HRTEM micrographs. High density of short slabs appears on the catalysts derived from ATM, whereas for the catalysts using TMATM the CoMo species preferably form big needle-like aggregates of slabs with a low crystalline perfection perpendicular to the c axis (compare Figs. 4, 5). The distinct MoS2 morphologies should be mainly responsible for the observed different HDS performance. In summary, it can be concluded that the efficiency of the decomposition process to generate good catalysts depends on the type of the precursor and the chosen conditions .
Increasing HDS activity with increasing Mo loading is visible when the same precursor is employed (Table 2). It is well-known that the optimal atomic Co/Mo ratio for γ-Al2O3 supported HDS catalysts is 0.4 . Consequently, the cobalt loading of one of the present catalysts Co(2.5)Mo(20)/SBA-15(A) was increased to this ratio to monitor the change of the HDS activity as function of Co content. Increasing the Co concentration by post-impregnation leads apparently to an increase in HDS activity [see Co(4)Mo(20)/SBA-15(C)]. For this Co-rich sample, the absence of reflections of crystalline Co sulfides in the X-ray powder pattern (Fig. 2) indicates that the usage of CoDMTC retards crystallization of such CoS x crystallites. Interestingly, the HRTEM/EDS investigation of this sample shows that the Co content is not larger than for Co(2.5)Mo(20)/SBA-15(B). The excess CoS x species are finely dispersed over the large surface area of SBA-15. The result of the HDS test suggests that the amorphous cobalt sulfide may be responsible for the enhanced HDS activity. But at this stage one can only speculate about the effect of the CoS x particles onto the enhancement of the HDS activity. One possibility I the so-called spill-over effect but one can also imagine that the finely dispersed CoS x itself acts as an active catalytic material.
The HYD/DDS ratio of Co–MoS2/SBA-15 catalysts prepared from different S containing starting materials and different synthesis methods scatters around 0.2 [exception: CoMo(ATM), Table 2], and these ratios are in accordance with the results from our previous study . Multilayered WS2 slabs have been confirmed by Vradman and Landau to facilitate π-complexation of the aromatic ring with respect to single-layered or thin slabs , and consequently result in higher HYD activity. Opposite to that, the present catalysts with multilayered MoS2 slabs shows a strong preference for the DDS pathway which may be correlated mainly to the promoting effect of Co. It has been proposed that the promoting effect of Co is due to an increased mobility of S atoms in the Co–MoS phase where the strength of the Mo–S bond is considered to be weakened. But the pronounced selectivity for the DDS route could be also related to the presence of a large amount of CUS (Lewis acid sites) in our supported catalysts. Furthermore, the results of different studies suggest that hydrogenolysis and HYD reactions occur on separate sites, i.e., on Lewis acid sites (vacancies) and Brønsted acid sites .
In the present study an all sulfur route for the preparation of Co promoted MoS2 catalysts supported on SBA-15 are presented. This method avoids the treatment of the materials in a poisonous H2S atmosphere. The catalysts obtained from ATM exhibit higher catalytic activity compared to a CoMo/γ-Al2O3 catalyst despite of the pronounced MoS2 stacking. An explanation for the observed high HDS activity and selectivity for the DDS pathway is the co-operative or synergistic effect of a Co–MoS phase as well as large amount of vacancies (CUS). The synergetic effect of Co depends on the nature of the thiosalt precursor material. In the case of catalysts derived from TMATM, large needle-like aggregates of Co–MoS2 slabs are formed and a pronounced pore blocking effect is observed. These two properties may be the important factors for the lower HDS activities compared to the catalysts obtained from ATM. In addition, our study highlights that the intermediate MoS3 is not a prerequisite for the generation of catalytic active Co–MoS phases. A more active catalyst was obtained by increasing the Co content through post-impregnation method due to the positive contribution of amorphous cobalt sulfide to the catalytic performance. In further studies the new synthetic approach is tested with different supports to monitor the influence of the support material onto the catalytic activity and selectivity.
Hagenbach G, Courty P, Delmon B (1973) J Catal 31:264
Candia R, Clausen BS, TopsØe H (1982) J Catal 77:564
Zdrazil M (1988) Catal Today 3:269
Zhao D, Feng J, Huo Q, Melosh N, Fredrickson GH, Chmelka BF, Stucky GD (1998) Science 279:548
Vradman L, Landau MV, Herskowitz M, Ezersky V, Talianker M, Nikitenko S, Koltypin Y, Gedanken A (2003) J Catal 213:163
Dhar GM, Kumaran GM, Kumar M, Rawat KS, Sharma LD, Raju BD, Rao KSR (2005) Catal Today 99:309
Klimova T, Lizama L, Amezcua JC, Roquero P, Terrés E, Navarrete J, Domínguez JM (2004) Catal Today 98:141
Kumaran GM, Garg S, Soni K, Kumar M, Sharma LD, Dhar GM, Rao KSR (2006) Appl Catal A Gen 305:123
Gutiérrez OY, Fuentes GA, Salcedo C, Klimova T (2006) Catal Today 116:485
Gutiérrez OY, Valencia D, Fuentes GA, Klimova T (2007) J Catal 249:138
Breysse M, Afanasiev P, Geantet C, Vrinat M (2003) Catal Today 86:5
Huang Z-D, Bensch W, Kienle L, Fuentes S, Alonso G, Ornelas C (2008) Catal Lett 122:57
Sundaramurthy V, Dalai AK, Adjaye J (2005) Catal Lett 102:299
Coulier L, Kishan G, van Veen JAR, Niemantsverdriet JW (2002) J Phys Chem B 106:5897
Rana MS, Ramírez J, Gutiérrez-Alejandre A, Ancheyta J, Cedeňo L, Maity SK (2007) J Catal 246:100
Poisot M, Bensch W, Fuentes S, Alonso G (2006) Thermochim Acta 444:35
Cambi L, Cagnasso A, Tanara A (1931) Atti Linc 13:404
Whitehurst DD, Isoda T, Mochida I (1998) Adv Catal 42:345
Huang Z-D, Bensch W, Sigle W, van Aken PA, Kienle L, Vitova T, Modrow H, Ressler T (2008) J Mater Sci 43:244
Poisot M, Bensch W, Fuentes S, Ornelas C, Alonso G (2007) Catal Lett 117:2007
Landau MV, Vradman L, Herskowitz M, Koltypin Y, Gedanken A (2001) J Catal 201:22
Nava R, Ortega RA, Alonso G, Ornelas C, Pawelec B, Fierro JLG (2007) Catal Today 127:70
Alonso G, Berhault G, Aguilar A, Collins V, Ornelas C, Fuentes S, Chianelli RR (2002) J Catal 208:359
Nava H, Ornelas C, Aguilar A, Berhault G, Fuentes S, Alonso G (2003) Catal Lett 86:257
Topsoe H, Clausen BS (1984) Catal Rev Sci Eng 26:395
Lauritsen JV, Kibsgaard J, Olesen GH, Moses PG, Hinnemann B, Helveg S, NØrskov JK, Clausen BS, TopsØe H, Lægsgaard E, Besenbacher F (2007) J Catal 249:218
Wilkinson K, Merchan MD, Vasudevan PT (1997) J Catal 171:325
Karroua M, Matralis H, Grange P, Delmon B (1993) J Catal 139:371
Eijsbouts S, van den Oetelaar LCA, van Puijenbroek RR (2005) J Catal 229:352
Furimsky E, Massoth FE (1993) Catal Today 17:535
Absihalabi M, Stanislaus A, Trimm DL (1991) Appl Catal 72:193
Brito JL, Severino F, Delgado NN, Laine (1998) Appl Catal A Gen 173:193
Alvarez L, Espino J, Ornelas C, Rico JL, Cortez MT, Berhault G, Alonso G (2004) J Mol Catal Chem 210:105
Lauritsen JV, Bollinger MV, Lægsgaard E, Jacobsen KW, Nørskov JK, Clausen BS, Topsøe H, Besenbacher F (2004) J Catal 221:510
Al-Zeghayer YS, Sunderland P, Al-Masry W, Al-Mubaddel F, Ibrahim AA, Bhartiya BK, Jibril BY (2005) Appl Catal A Gen 282:163
Vradman L, Landau MV (2001) Catal Lett 77:47
The financial support of the Deutsche Forschungsgemeinschaft (DFG) and of the State of Schleswig-Holstein is greatly acknowledged.
About this article
Cite this article
Huang, ZD., Bensch, W., Kienle, L. et al. Preparation and Characterization of SBA-15 Supported Cobalt–Molybdenum Sulfide Catalysts for HDS Reaction: An All Sulfide Route to Hydrodesulfurization Catalysts. Catal Lett 124, 24 (2008). https://doi.org/10.1007/s10562-008-9516-3
- Methylammonium thiomolybdate
- Cobalt dimethyldithiocarbamate
- Co–MoS2/SBA-15 catalysts
- SBA-15 support
- MoS2 morphology