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Molybdenum disulfide (MoS2) catalysts are used for hydrodesulfurization processes, needed for the removal of sulfur from oil feedstocks. The commonly accepted active site of MoS2 is believed to have a S4 pyramidal geometry with molybdenum (IV) at the apex. This work is interested in small molecules as models. Recent work has shown that one ligand can be removed from a molybdenum trisdithiolene by reacting the metal complex with an olefin creates a labile chelate cap. The resulting structure resembles the active site of interest. The present contribution will show approaches to molybdenum bisdithiolenes with one or two labile solvent molecules. The use of acetonitrile, adiponitrile, isobutyronitrile, and oxalate has been investigated. A complex containing two different labile moieties (tetrahydrothiophene, acetonitrile) was crystallographically characterized. Other nitrile molybdenum complexes were monitored using NMR spectroscopy. Two complexes have been characterized with an oxalato ligand; a single unit, and a dimer.

Molybdenum disulfide (MoS2) catalysts are used for hydrodesulfurization processes, needed for the removal of sulfur from oil feedstocks. The commonly accepted active site of MoS2 is believed to have a S4 pyramidal geometry with molybdenum (IV) at the apex. This work is interested in small molecules as models. Recent work has shown that one ligand can be removed from a molybdenum trisdithiolene by reacting the metal complex with an olefin creates a labile chelate cap. The resulting structure resembles the active site of interest. The present contribution will show approaches to molybdenum bisdithiolenes with one or two labile solvent molecules. The use of acetonitrile, adiponitrile, isobutyronitrile, and oxalate has been investigated. A complex containing two different labile moieties (tetrahydrothiophene, acetonitrile) was crystallographically characterized. Other nitrile molybdenum complexes were monitored using NMR spectroscopy. Two complexes have been characterized with an oxalato ligand; a single unit, and a dimer.

In this research, two-stage hydrotreating of bitumen-derived light gas oil (LGO) from Athabasca oil sands was studied. The objective was to catalytically upgrade the LGO by reducing the aromatics content and enhancing the cetane content via inter-stage removal of hydrogen sulfide. The impact of hydrogen sulfide inhibition on aromatics hydrogenation (HDA), hydrodenitrogenation (HDN) and hydrodesulfirization (HDS) activities was investigated. Experiments for this study were carried out in a trickle-bed reactor loaded with commercial NiMo/Al2O3 and lab-prepared NiW/Al2O3 in the stage I and stage II reactors, respectively. Temperature was varied from 350 to 390 oC at the optimum LHSV and pressure conditions of 0.6 h-1 and 11.0 MPa, respectively. The results from two-stage process showed significant improvement in HDA, cetane rating and HDS activities compared to the single-stage process after the inter-stage removal of hydrogen sulfide. Hence, the presence of hydrogen sulfide in the reaction retarded both the HDA and HDS processes in the single-stage operation. Negligible hydrogen sulfide inhibition was however, observed in the HDN process. <p>Prior to the two-stage hydrotreating study, single-stage hydrotreating reactions were carried out over commercial NiMo/Al2O3 catalyst to determine the optimum operating conditions for maximizing hydrogenation of aromatics. A statistical approach via the Analysis of Variance (ANOVA) technique was used to develop regression models for predicting the conversion of aromatics, sulfur and nitrogen in the LGO feed. Experiments were performed at the following operating conditions: temperature (340-390 oC); pressure (6.9-12.4 MPa) and liquid hourly space velocity, LHSV (0.5-2.0 h-1). Hydrogen-to-oil ratio was maintained constant at 550 ml/ml. The results showed that the two-level interaction between temperature and pressure was the only significant interaction parameter affecting HDA while interaction between temperature and LHSV was the most important parameter affecting both HDS and HDN activities. A maximum 63 % HDA was obtained at 379 oC, 11.0 MPa and 0.6 h-1. Experiments with NiW/Al2O3 were also performed in a single-stage reactor with LGO blend feedstock by varying temperature from 340-390 oC at the optimum pressure and space velocity of 11.0 MPa and 0.6 h-1, respectively. The following order of ease of hydrogenation was observed: poly- > di- >> monoaromatics. The order of ease of hydrogenation in other LGO feedstocks (atmospheric light gas oil, ALGO; hydrocrack light gas oil, HLGO; and vacuum light gas oil, VLGO) was studied and found to follow the order: VLGO > ALHO > HLGO. Studies on mild hydrocracking (MHC) in the gas oil feedstocks showed a net increase in gasoline with a corresponding decrease in diesel with increasing temperature. <p>Both the single and two-stage HDA and HDS kinetics were modeled using Langmuir-Hinshelwood rate equations. These models predicted the experimental data with reasonable accuracy. The degree of conversion of the gas oil fractions in ALGO, HLGO and VLGO via mild hydrocracking was best described by a pseudo-first order kinetic model based on a parallel conversion scheme.

In this research, two-stage hydrotreating of bitumen-derived light gas oil (LGO) from Athabasca oil sands was studied. The objective was to catalytically upgrade the LGO by reducing the aromatics content and enhancing the cetane content via inter-stage removal of hydrogen sulfide. The impact of hydrogen sulfide inhibition on aromatics hydrogenation (HDA), hydrodenitrogenation (HDN) and hydrodesulfirization (HDS) activities was investigated. Experiments for this study were carried out in a trickle-bed reactor loaded with commercial NiMo/Al2O3 and lab-prepared NiW/Al2O3 in the stage I and stage II reactors, respectively. Temperature was varied from 350 to 390 oC at the optimum LHSV and pressure conditions of 0.6 h-1 and 11.0 MPa, respectively. The results from two-stage process showed significant improvement in HDA, cetane rating and HDS activities compared to the single-stage process after the inter-stage removal of hydrogen sulfide. Hence, the presence of hydrogen sulfide in the reaction retarded both the HDA and HDS processes in the single-stage operation. Negligible hydrogen sulfide inhibition was however, observed in the HDN process. <p>Prior to the two-stage hydrotreating study, single-stage hydrotreating reactions were carried out over commercial NiMo/Al2O3 catalyst to determine the optimum operating conditions for maximizing hydrogenation of aromatics. A statistical approach via the Analysis of Variance (ANOVA) technique was used to develop regression models for predicting the conversion of aromatics, sulfur and nitrogen in the LGO feed. Experiments were performed at the following operating conditions: temperature (340-390 oC); pressure (6.9-12.4 MPa) and liquid hourly space velocity, LHSV (0.5-2.0 h-1). Hydrogen-to-oil ratio was maintained constant at 550 ml/ml. The results showed that the two-level interaction between temperature and pressure was the only significant interaction parameter affecting HDA while interaction between temperature and LHSV was the most important parameter affecting both HDS and HDN activities. A maximum 63 % HDA was obtained at 379 oC, 11.0 MPa and 0.6 h-1. Experiments with NiW/Al2O3 were also performed in a single-stage reactor with LGO blend feedstock by varying temperature from 340-390 oC at the optimum pressure and space velocity of 11.0 MPa and 0.6 h-1, respectively. The following order of ease of hydrogenation was observed: poly- > di- >> monoaromatics. The order of ease of hydrogenation in other LGO feedstocks (atmospheric light gas oil, ALGO; hydrocrack light gas oil, HLGO; and vacuum light gas oil, VLGO) was studied and found to follow the order: VLGO > ALHO > HLGO. Studies on mild hydrocracking (MHC) in the gas oil feedstocks showed a net increase in gasoline with a corresponding decrease in diesel with increasing temperature. <p>Both the single and two-stage HDA and HDS kinetics were modeled using Langmuir-Hinshelwood rate equations. These models predicted the experimental data with reasonable accuracy. The degree of conversion of the gas oil fractions in ALGO, HLGO and VLGO via mild hydrocracking was best described by a pseudo-first order kinetic model based on a parallel conversion scheme.

The impact of H2 partial pressure (H2 pp) during the hydrotreating of heavy gas oil, derived from Athabasca bitumen, over commercial NiMo/¥ã-Al2O3 catalyst was studied in a micro-trickle bed reactor. The experimental conditions were varied as follows: temperature: 360 to 400¨¬C, pressure: 7 to 11 MPa, gas/oil ratio: 400 to 1270 mL/mL, H2 purity range of 0 to 100 vol. % (with the rest either CH4 or He), and LHSV range of 0.65 to 2 h-1. The two main objectives of the project were to study the nature of the dependence of H2 pp on temperature, pressure, gas/oil ratio, LHSV (Liquid Hourly Space Velocity), and H2 purity. The project was divided into three phases: in phase one the effect of H2 purity on hydrotreating of heavy gas oil (HGO) was studied, in phase two the nature of H2 pp dependency and the effect of H2 pp on hydrotreating of HGO was investigated, and in phase three kinetic studies were carried out using different kinetic models.<p> The objective of phase one was to study the effect of hydrogen purity on hydrotreating of HGO was studied in a trickle bed reactor over a commercial Ni−Mo/¥ã-alumina catalyst. Methane was used as a diluent for the hydrogen stream, and its effect on the catalyst performance was compared to that of helium, which is inert toward the catalyst. Furthermore, a deactivation study was conducted over a period of 66 days, during which the catalyst was subjected to H2 purities ranging from 75 to 95% (with the rest methane); no significant deterioration in the hydroprocessing activities of the catalyst was observed. Therefore, it was concluded that methane was inert toward a commercial Ni−Mo/¥ã-alumina catalyst. However, its presence resulted in hydrogen partial pressure reduction, which in turn led to a decrease in hydrodesulphurization (HDS), hydrodenitrogenation (HDN), hydrodearomatization (HDA) conversions. This reduction can be offset by increasing the total pressure of the system. HDS, HDN, HDA, and mild hydrocracking (MHC) conversions were studied. Also determined were cetane index, density, aniline point, diesel index, and fractional distribution of the products.<p> The main objective of phase two was to study the effects of H2 pp on hydrotreating conversions, feed vaporization, H2 dissolution, and H2 consumption were studied. The results show that HDN and HDA are significantly more affected by H2 partial pressure than HDS; with the HDN being the most affected. For instance as the inlet H2 partial pressure was increased from 4.6 to 8.9 MPa HDS, HDN, and HDA conversions increased for 94.9%, 55.1%, and 46.0% to 96.7%, 83.9%, and 58.0% , respectively. Moreover, it was observed that H2 dissolution and H2 consumption increased with increasing H2 pp. No clear trend was observed for the effect of H2 pp on feed vaporization.<p> In phase three the kinetics of HDS, HDN, and HDA were studied. The power law, multi-parameter, and Langmuir - Hinshelwood type models were used to fit the data. The prediction capacities of the resulting models were tested. It was determined that, while multi-parameter model yielded better prediction, L-H had an advantage in that it took a lesser number of experimental data to determine its parameters. Kinetic fitting of the data to a pseudo-first-order power law model suggested that conclusions on the effect of H2 pp on hydrotreating activities could be equally drawn from either inlet or outlet hydrogen partial pressure. However, from the catalyst deactivation standpoint, it is recommended that such conclusions are drawn from the outlet H2 partial pressure, since it is the reactor point with the lowest hydrogen partial pressure.

The impact of H2 partial pressure (H2 pp) during the hydrotreating of heavy gas oil, derived from Athabasca bitumen, over commercial NiMo/¥ã-Al2O3 catalyst was studied in a micro-trickle bed reactor. The experimental conditions were varied as follows: temperature: 360 to 400¨¬C, pressure: 7 to 11 MPa, gas/oil ratio: 400 to 1270 mL/mL, H2 purity range of 0 to 100 vol. % (with the rest either CH4 or He), and LHSV range of 0.65 to 2 h-1. The two main objectives of the project were to study the nature of the dependence of H2 pp on temperature, pressure, gas/oil ratio, LHSV (Liquid Hourly Space Velocity), and H2 purity. The project was divided into three phases: in phase one the effect of H2 purity on hydrotreating of heavy gas oil (HGO) was studied, in phase two the nature of H2 pp dependency and the effect of H2 pp on hydrotreating of HGO was investigated, and in phase three kinetic studies were carried out using different kinetic models.<p> The objective of phase one was to study the effect of hydrogen purity on hydrotreating of HGO was studied in a trickle bed reactor over a commercial Ni−Mo/¥ã-alumina catalyst. Methane was used as a diluent for the hydrogen stream, and its effect on the catalyst performance was compared to that of helium, which is inert toward the catalyst. Furthermore, a deactivation study was conducted over a period of 66 days, during which the catalyst was subjected to H2 purities ranging from 75 to 95% (with the rest methane); no significant deterioration in the hydroprocessing activities of the catalyst was observed. Therefore, it was concluded that methane was inert toward a commercial Ni−Mo/¥ã-alumina catalyst. However, its presence resulted in hydrogen partial pressure reduction, which in turn led to a decrease in hydrodesulphurization (HDS), hydrodenitrogenation (HDN), hydrodearomatization (HDA) conversions. This reduction can be offset by increasing the total pressure of the system. HDS, HDN, HDA, and mild hydrocracking (MHC) conversions were studied. Also determined were cetane index, density, aniline point, diesel index, and fractional distribution of the products.<p> The main objective of phase two was to study the effects of H2 pp on hydrotreating conversions, feed vaporization, H2 dissolution, and H2 consumption were studied. The results show that HDN and HDA are significantly more affected by H2 partial pressure than HDS; with the HDN being the most affected. For instance as the inlet H2 partial pressure was increased from 4.6 to 8.9 MPa HDS, HDN, and HDA conversions increased for 94.9%, 55.1%, and 46.0% to 96.7%, 83.9%, and 58.0% , respectively. Moreover, it was observed that H2 dissolution and H2 consumption increased with increasing H2 pp. No clear trend was observed for the effect of H2 pp on feed vaporization.<p> In phase three the kinetics of HDS, HDN, and HDA were studied. The power law, multi-parameter, and Langmuir - Hinshelwood type models were used to fit the data. The prediction capacities of the resulting models were tested. It was determined that, while multi-parameter model yielded better prediction, L-H had an advantage in that it took a lesser number of experimental data to determine its parameters. Kinetic fitting of the data to a pseudo-first-order power law model suggested that conclusions on the effect of H2 pp on hydrotreating activities could be equally drawn from either inlet or outlet hydrogen partial pressure. However, from the catalyst deactivation standpoint, it is recommended that such conclusions are drawn from the outlet H2 partial pressure, since it is the reactor point with the lowest hydrogen partial pressure.

Η ηλεκτροχημική ενίσχυση της κατάλυσης (EPOC ή αλλιώς μη-φαρανταïκή τροποποίηση της καταλυτικής ενεργότητας, φαινόμενο NEMCA) είναι ένα φαινόμενο όπου εφαρμογή μικρών ρευμάτων ή δυναμικών (±2V) σε ένα καταλύτη που είναι υποστηριγμένος σε ένα ηλεκτρολύτη, ιοντικό ή μικτό ιοντικό-ηλεκτρονιακό αγωγό, μπορεί να επιφέρει σημαντική τροποποίηση της καταλυτικής ενεργότητας αλλά και εκλεκτικότητας της αντίδρασης που γίνεται στην αέρια φάση, με τρόπο ελεγχόμενο, αντιστρεπτό και έως ένα βαθμό προβλέψιμο. Η ηλεκτροχημική ενίσχυση έχει βρεθεί με χρήση διαφόρων τεχνικών ότι πηγάζει από την ηλεκτροχημικά ελεγχόμενη διάχυση ενισχυτικών ιοντικών ειδών ανάμεσα στο φορέα-ηλεκτρολύτη και στα καταλυτικά σωματίδια. Το φαινόμενο έχει εφαρμοστεί σε πληθώρα καταλυτικών συστημάτων (πάνω από 70) τα τελευταία 30 χρόνια ενώ έχει πραγματοποιηθεί και επιτυχής εφαρμογή του σε πιλοτική κλίμακα χάρη στον μονολιθικό ηλεκτροχημικά ενισχυόμενο αντιδραστήρα. Στο πρώτο κεφάλαιο της παρούσας διατριβής γίνεται εκτεταμένη αναφορά στους στερεούς ηλεκτρολύτες, στις ιδιότητες τους καθώς και τους τομείς στους οποίους χρησιμοποιούνται με ιδιαίτερη σημασία στη σταθεροποιημένη με οξείδιο του υττρίου ζιρκονία (YSZ), που αποτελεί ένα πολύ συχνά χρησιμοποιούμενο αγωγό ιόντων οξυγόνου. Επιπρόσθετα, εισάγονται οι έννοιες της μετανάστευσης (spillover) και της αντίστροφης μετανάστευσης (backspillover), οι οποίες χρησιμοποιούνται στην ερμηνεία και την κατανόηση του φαινομένου της ηλεκτροχημικής ενίσχυσης και των αλληλεπιδράσεων μετάλλου-φορέα (MSI). Στο δεύτερο κεφάλαιο γίνεται μια εισαγωγή στις αρχές του φαινομένου της Ηλεκτροχημικής Ενίσχυσης της Κατάλυσης όπου συζητούνται αρκετά παραδείγματα εφαρμογής του και γίνεται ανασκόπηση όλων των εργασιών που υπάρχουν στην βιβλιογραφία και αφορούν στο συγκεκριμένο φαινόμενο. Παρουσιάζονται επίσης, πλήθος πειραματικών τεχνικών, όπως ηλεκτροκινητικών πειραμάτων δυναμικής απόκρισης, μετρήσεων έργου εξόδου, κυκλικής βολταμμετρίας, XPS, TPD και STM, καθώς και θεωρητικών μελετών ,με στόχο την κατανόηση της αρχής του φαινομένου σε ατομικό επίπεδο. Στο τρίτο κεφάλαιο παρουσιάζονται τα πειραματικά αποτελέσματα από την εφαρμογή του φαινομένου της ηλεκτροχημικής ενίσχυσης της κατάλυσης στην αντίδραση βιομηχανικής σημασίας της υδρογονοαποθείωσης (HDS). Στην παρούσα μελέτη χρησιμοποιήθηκε η πρότυπη ένωση του θειοφαινίου, χρησιμοποιώντας στερεούς ηλεκτρολύτες αγωγούς ιόντων (BCN18, CZI ή YSZ) σε συνδυασμό καταλύτες, όπως RuS2, MoS2, FeSx και MoS2-CoS2 καθώς και μη-στηριγμένους όπως ο Nebula (NiMoW). Η μελέτη επικεντρώθηκε στην επίτευξη ηλεκτροχημικής ενίσχυσης στην HDS του θειοφαινίου υπό συνθήκες ατμοσφαιρικής πίεσης στο θερμοκρασιακό εύρος 250οC-550οC. Ηλεκτροχημική Ενίσχυση επιτεύχθηκε σε συνολικά 10 καταλυτικά ηλεκτρόδια. Στην περίπτωση χρήσης πρωτονιακών αγωγών, τιμές προσαύξησης ρυθμού έως 20% και φαρανταϊκής απόδοσης έως ~600 καταγράφησαν, αναδεικνύοντας την ισχυρά μη-φαρανταϊκή συμπεριφορά και το υψηλό ενεργειακό όφελος σε Τ<300oC. Στην περίπτωση των αγωγών ιόντων οξυγόνου (YSZ) προσαύξηση ρυθμού έως και 300% καταγράφηκε με τιμές φαρανταϊκής απόδοσης έως και 0.2 στους 500oC. Στο τέταρτο κεφάλαιο παρουσιάζεται η ηλεκτροχημική ενίσχυση της αντίδρασης υδρογόνωσης του CO2 χρησιμοποιώντας καταλυτικά υμένια Ru εναποτεθειμένα σε στερεούς ηλεκτρολύτες YSZ με στόχο την παραγωγή μεθανίου. Βρέθηκε ότι η αντίδραση μπορεί να ενισχυθεί σε μεγάλο βαθμό και επιπλέον να τροποποιηθεί και η εκλεκτικότητά της σε CΗ4 που είναι και το επιθυμητό προϊόν. / Electrochemical Promotion of Catalysis (EPOC or Non-Faradaic Electrochemical Modification of Catalytic Activity, NEMCA effect) is a phenomenon where the application of small currents or potentials (±1V) between a catalyst electrode, which is in contact with a solid electrolyte support, and a counter or reference electrode, causes a significant change in catalytic activity in a predictable, reversible and to some extend controllable manner. As have been shown by numerous surface science and electrochemical techniques, electrochemical promotion is due to electrochemically controlled migration (backspillover) of promoting or poisoning ionic species between the ionic or mixed ionic-electronic conductor support and the gas exposed catalytic surface. Τhe phenomenon has been studied extensively in a variety of catalytic systems (>70) during the last 30 years, while it has been successfully applied in a pilot scale reactor, the monolithic electrochemically promoted reactor (MEPR) in environmental important reactions. In the first chapter, an extended analysis is given of the properties of solid electrolytes, and focused on the yttria-stabilized zirconia (YSZ). Moreover, the concepts of spillover and backspillover, which are used to describe the phenomenon of electrochemical promotion and the metal-support interactions, are discussed in detail. In the second chapter, the fundamentals of Electrochemical Promotion of Catalysis are discussed in the basis of classical promotion, reaction kinetics and the rules of Electrochemical Promotion of Catalysis. In the third chapter, the effect of the electrochemical promotion of catalysis on the hydrodesulfurization (HDS) reaction of sulfur containing model compounds (thiophene) has been investigated, using ion conducting solid electrolytes (BCN18, CZI or YSZ) and state-of-the-art catalysts, e.g. RuS2, MoS2, MoS2-CoS2 and the unsupported state-of-the-art catalyst Nebula (NiMoW). In this study thiophene, was used under atmospheric pressure in the temperature range of 250 οC -550οC. Significant Electrochemical Promotion was achieved with 10 different CoMo based catalyst-electrodes. Values of rate enhancement up to 20% and faradaic efficiency values up to ~600 were achieved, denoting the strongly non-faradaic behavior and high energy efficiency at T<300oC. In the case of oxygen ion conductors (YSZ) an increase of 300% on the catalytic rate and a faradaic efficiency value of 0.2 was recorded at 500oC. The results show the strong potential of Electrochemical Promotion of Catalysis on improving the efficiency of industrial and/or environmental processes. In the last chapter, the electrochemical promotion of the CO2 hydrogenation reaction was also examined, towards methane production using Ru/YSZ/Au type electrochemical catalytic elements. It was found that the reaction rates and similarly as well as the selectivity to CH4 can be enhanced under anodic polarizations.

Made available in DSpace on 2015-05-14T13:21:50Z (GMT). No. of bitstreams: 1 parte1.pdf: 1916067 bytes, checksum: e4045cc0ffe2f947f30aea1666f195a2 (MD5) Previous issue date: 2009-09-25 / Coordenação de Aperfeiçoamento de Pessoal de Nível Superior - CAPES / Air pollution is of great concern to all of us, and among the main causes are the gases emitted from fossil fuels burning. Therefore, the search for clean technologies is of prime importance nowadays. Thus, in the present work the reaction mechanism for the hydrodesulfurization is investigated. Such reaction is widely used in oil refinery, where new materials, with lowest cost and greater range of application, are searched for. This reaction causes the reduction of hydrocarbons containing sulfur-based functional groups, such as thiols, sulfides and thiophenes, releases hydrogen sulfide, and is catalyzed by molybdenum sulfides or oxides. Since the absorption of SOx compounds is harmful to health and environment, the levels of these types of compounds should be considerably reduced, according to the Kyoto Protocol and the current legislation. In the present study, the hydrodesulfurization reaction involving thiophene is investigated through the use of Quantum Chemical Methods. A mechanism is proposed, using the MoO3, NiMoO4 and CrMoO4 compounds as catalysts. Besides, the effects of Mo6+, Ni2+ and Cr2+ ions are analyzed and also, a mechanism is proposed, considering Thermodynamic and Kinetic Chemistry aspects, once they are not completely established in literature. Geometry optimization and harmonic frequency calculations are performed using the PM6 method, implemented in MOPAC2007. The catalysts structures are built from experimental data provided by the Inorganic Crystal Structure Database. Reaction enthalpies, entropies, Gibbs free energies, as well as activation and reaction energies are computed. Some results of this work comprehend values referring to absortion energies for the catalysts MoO3, MoO3:Ni e MoO3:Cr, corresponding to -117.23, -115.26 and -407.14 kJ mol-1, respectively, originating the following stability order: Cr > Mo > Ni. / A atmosfera sofre graves efeitos oriundos da poluição gerada, principalmente, pelos gases procedentes dos combustíveis fósseis. Por conseguinte, a busca por tecnologias limpas é de suma importância na contemporaneidade. Pertinente a esse fato, o trabalho em questão investiga o mecanismo para a reação de hidrodessulfurização, que é empregada nas refinarias de petróleo, onde são averiguados novos materiais, com custos menos onerosos e de maior aplicabilidade. A partir dessa reação, reduzem-se hidrocarbonetos que contêm grupos funcionais contendo enxofre, como tióis, tiofenos e sulfetos, liberando gás sulfídrico, sendo promovida por sulfetos ou óxidos de molibdênio. A absorção dos compostos SOX causa efeitos prejudiciais à saúde e ao meio ambiente, de modo que os níveis desses compostos devem ser reduzidos consideravelmente, conforme o Protocolo de Kyoto e a legislação vigente. Neste estudo teórico, a reação de hidrodessulfurização envolve o tiofeno, empregando os catalisadores MoO3, MoO3:Ni e MoO3:Cr, a fim de avaliar o efeito dos íons Mo6+, Ni2+ e Cr2+, além de propor o mecanismo para a mesma, considerando os aspectos da Termodinâmica e da Cinética Química, visto que o mesmo não é estabelecido completamente pela literatura. Para otimização de geometria e cálculos das frequências harmônicas, utilizou-se o método PM6, incorporado ao MOPAC2007. Os catalisadores foram construídos a partir de dados experimentais oriundos do Inorganic Crystal Structure Database, tornando a estrutura de cada catalisador inédita para este tipo de investigação. Resultados como entalpia, entropia, energia livre de Gibbs, energia de ativação e de reação foram averiguados. Alguns resultados deste trabalho, englobam os valores referentes às energias de adsorção para os catalisadores MoO3, MoO3:Ni e MoO3:Cr, que corresponderam a -117,23, -115,26 e -407,14 kJ mol-1, respectivamente, originando a seguinte ordem de estabilidade: Cr > Mo > Ni.

No / In this paper, hydrodesulfurization (HDS) of crude oil in the three-phase slurry reactor over cobalt – molybdenum catalyst (CoMo / ɣ- AL2O3) is studied. Effects of space velocity and length of reactor on the conversion rate and catalyst effectiveness for HDS process have been investigated. Kinetics of the reaction rate for this process is primarily and Arrhenius equation for the rate constant is used. The results show that the effectiveness factor for catalyst along the length of reactor is decreased about 83%. By increasing liquid velocity from 4 to 10 1/s, the conversion of sulfur components is decreased about 22% at the temperature of 523 K. At the same temperature, by increasing liquid velocity from 36 to 84 1/s conversion is reduced to 25%. The results of the variation of the dimensionless reaction rate against conversion show that with increasing conversion, the reaction rate decreases and the reaction is stopped when the conversion is 100%.