Perovskita de LaFeO3 sintetizadas pelo método de Pechini foram avaliadas como catalisadores para a reação de oxidação parcial do metano. Foi impregnado níquel por via úmida como fase ativa em concentrações de 15 e 30 %, sobre as perovskitas, 15NLF e 30NLF, respectivamente, e o seu efeito foi avaliado para a mesma reação. Foi realizado análises termogravimétricas (TGA/DTGA) nos precursores da perovskitas, constatando a sua formação a 650 °C. A análise de microscopia de varredura (MEV) foi realizada nas amostras da perovskita pura, sendo que em uma delas foi realizada um banho de ultrassom para diminuir o tamanho de suas partículas e avaliar este efeito na reação de POM. Análises de difração de raio X (DRX) mostraram que todas as amostras apresentam as mesmas propriedades cristalográficas, sendo que, nas amostras contendo níquel, o metal apresentou-se na forma de NiO. O tamanho dos cristais, cálculado através da equação de Scherer, foi na ordem de 20 nm. Este resultado apontou que o níquel impregnado não participa da estrutura perovskita, mas sim está sobreposto a esta. Através da microscopia eletrônica de transmissão (TEM) foi possível visualizar a dispersão da fase ativa na superfície óxida e tamanhos de partículas na ordem de 20 nm. A redução a temperatura programada (TPR) apresentou as temperaturas de redução de espécies níquel e de ferro, presente na perovskita, e permitiu compreender a atuação das espécies Ni+2 e Fe0 na formação de H2 e CO. Os testes catalíticos foram realizados a 700ºC e 750°C, a pressão atmosférica, para uma vazão de alimentação de 200 cm3.min-1. Os testes cataliticos mostraram que a conversão de H2 dobrou para perovskita Ni/LaFeO3 em relação a LaFeO3. O catalisador 15NLF apresentou melhor estabilidade que o catalisador 30NLF para a reação. / LaFeO3 perovskite synthesized by the Pechini method were evaluated for the partial oxidation reaction of methane. Nickel was impregnated as the active phase in concentrations of 15 and 30%, on perovskites, 15NLF and 30NLF, respectively, and its effect was evaluated for the same reaction. Thermogravimetric analyzes (TGA / DTGA) were carried out on the perovskite precursors, confirming their formation at 650 °C. Scanning microscopy (SEM) was performed on pure perovskite samples, in one of them an ultrasonic bath was performed to reduce the size of its particles and to evaluate this effect in the POM reaction. X-ray diffraction (XRD) analyzes showed that all samples had the same crystallographic properties, and in the samples containing nickel, the metal was present as NiO. The size of the crystals, calculated through the Scherer equation, was in the order of 20 nm. This result pointed out that the impregnated nickel does not participate in the perovskite structure. Through transmission electron microscopy (TEM) it was possible to visualize the dispersion of the active phase on the oxide surface and particle sizes in the order of 20 nm. The programmed temperature reduction (TPR) showed the iron and nickel species reduction temperatures present in the perovskite, and allowed to understand the Ni+ 2 and Fe0 species in the H2 and CO formation. The catalytic tests were performed at 700 °C and 750 °C at atmospheric pressure for a flow rate of 200 cm3.min-1. The catalytic tests showed that the conversion of H2 doubled to perovskite Ni/LaFeO3 in relation to LaFeO3. 15NLF catalyst presented better stability than the 30NLF catalyst for the reaction.

Perovskita de LaFeO3 sintetizadas pelo método de Pechini foram avaliadas como catalisadores para a reação de oxidação parcial do metano. Foi impregnado níquel por via úmida como fase ativa em concentrações de 15 e 30 %, sobre as perovskitas, 15NLF e 30NLF, respectivamente, e o seu efeito foi avaliado para a mesma reação. Foi realizado análises termogravimétricas (TGA/DTGA) nos precursores da perovskitas, constatando a sua formação a 650 °C. A análise de microscopia de varredura (MEV) foi realizada nas amostras da perovskita pura, sendo que em uma delas foi realizada um banho de ultrassom para diminuir o tamanho de suas partículas e avaliar este efeito na reação de POM. Análises de difração de raio X (DRX) mostraram que todas as amostras apresentam as mesmas propriedades cristalográficas, sendo que, nas amostras contendo níquel, o metal apresentou-se na forma de NiO. O tamanho dos cristais, cálculado através da equação de Scherer, foi na ordem de 20 nm. Este resultado apontou que o níquel impregnado não participa da estrutura perovskita, mas sim está sobreposto a esta. Através da microscopia eletrônica de transmissão (TEM) foi possível visualizar a dispersão da fase ativa na superfície óxida e tamanhos de partículas na ordem de 20 nm. A redução a temperatura programada (TPR) apresentou as temperaturas de redução de espécies níquel e de ferro, presente na perovskita, e permitiu compreender a atuação das espécies Ni+2 e Fe0 na formação de H2 e CO. Os testes catalíticos foram realizados a 700ºC e 750°C, a pressão atmosférica, para uma vazão de alimentação de 200 cm3.min-1. Os testes cataliticos mostraram que a conversão de H2 dobrou para perovskita Ni/LaFeO3 em relação a LaFeO3. O catalisador 15NLF apresentou melhor estabilidade que o catalisador 30NLF para a reação. / LaFeO3 perovskite synthesized by the Pechini method were evaluated for the partial oxidation reaction of methane. Nickel was impregnated as the active phase in concentrations of 15 and 30%, on perovskites, 15NLF and 30NLF, respectively, and its effect was evaluated for the same reaction. Thermogravimetric analyzes (TGA / DTGA) were carried out on the perovskite precursors, confirming their formation at 650 °C. Scanning microscopy (SEM) was performed on pure perovskite samples, in one of them an ultrasonic bath was performed to reduce the size of its particles and to evaluate this effect in the POM reaction. X-ray diffraction (XRD) analyzes showed that all samples had the same crystallographic properties, and in the samples containing nickel, the metal was present as NiO. The size of the crystals, calculated through the Scherer equation, was in the order of 20 nm. This result pointed out that the impregnated nickel does not participate in the perovskite structure. Through transmission electron microscopy (TEM) it was possible to visualize the dispersion of the active phase on the oxide surface and particle sizes in the order of 20 nm. The programmed temperature reduction (TPR) showed the iron and nickel species reduction temperatures present in the perovskite, and allowed to understand the Ni+ 2 and Fe0 species in the H2 and CO formation. The catalytic tests were performed at 700 °C and 750 °C at atmospheric pressure for a flow rate of 200 cm3.min-1. The catalytic tests showed that the conversion of H2 doubled to perovskite Ni/LaFeO3 in relation to LaFeO3. 15NLF catalyst presented better stability than the 30NLF catalyst for the reaction.

This study introduces an evaluation of the downstream utilization of oxygen produced by the hybrid sulfur process (HYS). Both technical and economic aspects were considered in the production of primarily synthesis gas and hydrogen. Both products could increase the economic potential of the hybrid sulfur process. Based on an assumed 500MWt pebble bed modular nuclear reactor, the volume of hydrogen and oxygen produced by the scaled down HYS was found to be 121 and 959 ton per day respectively. The partial oxidation plant (POX) could produce approximately 1840 ton synthesis gas per day based on the oxygen obtained from the HYS. The capital cost of the POX plant is in the order of $104 million (US dollars, Base year 2008). Compared to the capital cost of the HYS, this seems to be a relatively small additional investment. The production cost varied from a best case scenario $9.21 to a worst case scenario of $19.36 per GJ synthesis gas. The profitability analysis conducted showed favourable results, indicating that under the assumed conditions, and with 20 years of operation, a NPV of $87 mil. and an IRR of 19.5% could be obtained, for the assumed base case. The economic sensitivity analysis conducted, provided insight into the upper and lower limitations of favourable operation. The second product that could be produced was hydrogen. With the addition of a water gas shift and a pressure swing adsorption process to the POX, it was found that an additional 221 ton of hydrogen per day could be produced. The hydrogen could be produced in the best case at $2.34/kg and in the worst case at $3.76/kg. The investment required would be in the order of $50 million. The profitability analysis for the base case analysis predicts an NPV of $206 million and a high IRR of 23.0% under the assumed conditions. On financial grounds it therefore seemed that the hydrogen production process was favourable. The thermal efficiency of the synthesis gas production section was calculated and was in good agreement with that obtained from literature. The hydrogen production section’s thermal efficiency was compared to that of steam methane reforming of natural gas (SMR) and it was found that the efficiencies were comparable but the SMR process was superior. The hydrogen production capacity of the HYS process was increased by a factor of 1.83. This implied that for every 1 kg of hydrogen produced by the HYS an additional 1.83 kg was produced by the proposed process addition. This lowers the cost of hydrogen produced by the HYS from $6.83 to the range of approximately $3.93 - $4.85/kg. In the event of a global hydrogen economy, traditional production methods could very well be supplemented with new and innovative methods. The integration of the wellknown methods incorporated with the new nuclear based methods of hydrogen production and chemical synthesis could facilitate the smooth transition from fossil fuel based to environmentally friendly methods. This study presents one possible integration method of nuclear based hydrogen production and conventional processing methods. This process is technically possible, efficient and economically feasible. / Thesis (M.Ing. (Nuclear Engineering))--North-West University, Potchefstroom Campus, 2009.

This study introduces an evaluation of the downstream utilization of oxygen produced by the hybrid sulfur process (HYS). Both technical and economic aspects were considered in the production of primarily synthesis gas and hydrogen. Both products could increase the economic potential of the hybrid sulfur process. Based on an assumed 500MWt pebble bed modular nuclear reactor, the volume of hydrogen and oxygen produced by the scaled down HYS was found to be 121 and 959 ton per day respectively. The partial oxidation plant (POX) could produce approximately 1840 ton synthesis gas per day based on the oxygen obtained from the HYS. The capital cost of the POX plant is in the order of $104 million (US dollars, Base year 2008). Compared to the capital cost of the HYS, this seems to be a relatively small additional investment. The production cost varied from a best case scenario $9.21 to a worst case scenario of $19.36 per GJ synthesis gas. The profitability analysis conducted showed favourable results, indicating that under the assumed conditions, and with 20 years of operation, a NPV of $87 mil. and an IRR of 19.5% could be obtained, for the assumed base case. The economic sensitivity analysis conducted, provided insight into the upper and lower limitations of favourable operation. The second product that could be produced was hydrogen. With the addition of a water gas shift and a pressure swing adsorption process to the POX, it was found that an additional 221 ton of hydrogen per day could be produced. The hydrogen could be produced in the best case at $2.34/kg and in the worst case at $3.76/kg. The investment required would be in the order of $50 million. The profitability analysis for the base case analysis predicts an NPV of $206 million and a high IRR of 23.0% under the assumed conditions. On financial grounds it therefore seemed that the hydrogen production process was favourable. The thermal efficiency of the synthesis gas production section was calculated and was in good agreement with that obtained from literature. The hydrogen production section’s thermal efficiency was compared to that of steam methane reforming of natural gas (SMR) and it was found that the efficiencies were comparable but the SMR process was superior. The hydrogen production capacity of the HYS process was increased by a factor of 1.83. This implied that for every 1 kg of hydrogen produced by the HYS an additional 1.83 kg was produced by the proposed process addition. This lowers the cost of hydrogen produced by the HYS from $6.83 to the range of approximately $3.93 - $4.85/kg. In the event of a global hydrogen economy, traditional production methods could very well be supplemented with new and innovative methods. The integration of the wellknown methods incorporated with the new nuclear based methods of hydrogen production and chemical synthesis could facilitate the smooth transition from fossil fuel based to environmentally friendly methods. This study presents one possible integration method of nuclear based hydrogen production and conventional processing methods. This process is technically possible, efficient and economically feasible. / Thesis (M.Ing. (Nuclear Engineering))--North-West University, Potchefstroom Campus, 2009.

Die Nutzung fossiler Energieträger hat die wirtschaftliche und gesellschaftliche Entwicklung der Menschheit bedeutend geprägt. Die Relevanz der verschiedenen Brennstoffe ist dabei stark vom technologischen Niveau abhängig gewesen. Mit der fortschreitenden Entwicklung und dem Aufstreben der Automobilindustrie in der ersten Hälfte des 20. Jahrhunderts gewann Erdöl als Quelle für verschiedene Kraftstoffe und Grundchemikalien immer größere Bedeutung. Der Energieverbrauch der Industriestaaten ist seit dem stetig gestiegen und zum Ende des 20. Jahrhunderts treten immer mehr Schwellenländer wie China, Indien oder Brasilien mit großem Energiehunger in Erscheinung. Dadurch wurden die Vorkommen fossiler Brennstoffe mit immer höherem Tempo ausgebeutet, sodass Schätzungen davon ausgehen, dass bereits 2030 nur noch 75% des Bedarfs durch bereits erschlossene Lagerstätten gedeckt werden können.[1] Im Gegensatz dazu sind die Reserven an Erdgas noch deutlich größer. Erdgas besteht vor allem aus Methan, welches auch über alternative Methoden z.B. Biofermentation hergestellt werden kann. Neben der Nutzung als primärer Energieträger ist Methan Ausgangsstoff für die Herstellung einer Vielzahl chemischer Produkte, z.B. Methanol oder kurzkettige Olefine[2, 3]. Eine wichtige Zwischenstufe dieser Prozesse stellt die Herstellung von Synthesegas dar, einem Gemisch aus Wasserstoff und Kohlenmonoxid. Die Herstellung erfolgt industriell über die Reaktion von Methan und Wasserdampf, dem Steamreforming. Alternative Verfahren stellen die partielle Oxidation von Methan und das Dry Reforming dar. In dieser Arbeit wurde die Aktivität verschiedener Katalysatorsysteme in der Totaloxidation, der partiellen Oxidation und dem Dry Reforming von Methan untersucht. Zur Synthese der Katalysatoren wurde die von E.Kockrick[4, 5] entwickelte Mikroemulsionsmethode angewandt. Dabei wurde die Abhängigkeit der katalytischen Aktivität von der Zusammensetzung der Komposite und den Synthesebedingungen untersucht. Das modulare Syntheseprinzip der Mikroemulsionsmethode wurde durch die Substitution der katalytisch aktiven Spezies durch verschiedene Übergangsmetalle und Gemische demonstiert. Weiterhin wurde eine neue Methode zur Herstellung makroporöser SiC-Keramiken (Abbildung 1) entwickelt. Dabei wird ein flüssiges Polycarbosilan in einer Emulsion mit besonders hohem Anteil der inneren Phase (high internal phase emulsion = HIPE) polymerisiert und zum SiC umgesetzt. Diese SiC-PolyHIPEs zeichnen sich durch ihre hohe Porosität und geringe Dichte aus. Ausgehend von der Synthesevorschrift nach Schwab et al.,[6] die die Synthese styrolbasierter PolyHIPEs beschreibt, wurde Styrol schrittweise durch SMP-10 ersetzt. Die erfolgreiche Inkorporation wurde durch thermogravimetrische Untersuchungen nachgewiesen. Zur Vernetzung des HIPE wurden verschiedene Initiatoren verwendet. Über den Anteil des SMP-10 am PolyHIPE konnte direkt Einfluss auf den Porenradius und die Dichte genommen werden, wobei die Porosität konstant bei 75% gehalten werden konnte.[7] Das Potential der SiC-PolyHIPEs für den Einsatz als poröser Katalysatorträger konnte durch die Funktionalisierung mit CeO2 und den Einsatz in der temperaturprogrammierten Oxidation von Methan nachgewiesen werden. Bereits durch eine Beladung des SiC-PolyHIPEs mit 30 Gew.% CeO2 konnte die gleiche Umsetzungstemperatur des Methans erreicht werden wie bei reinem CeO2. Eine weitere Strategie zur Erzeugung katalytisch aktiver SiC-Materialien wurde über die Funktionalisierung des Polycarbosilans mit hydrophoben CeO2-Nanopartikeln und Cerkomplexen entwickelt. Dabei zeigte sich, dass durch das Einbringen von 5 Gew.% über Dodecylamin stabilisierter CeO2-Nanopartikel eine ähnliche Aktivität in der Methanoxidation erreicht wurde, wie mit reinem Cerdioxid. Die Funktionalisierung des SMP-10 mit Cerkomplexen ergab für alle Cerkomplexe eine Phasenseparation nach dem Entfernen des Lösungsmittels. Nach der getrennten Pyrolyse der Phasen konnte nur im Pyrolysat der festen Phase Cer nachgewiesen werden, wodurch die Methanoxidation katalysiert wird. Als weitere Methode zur Erzeugung katalytisch aktiver und poröser SiC-Komposite wurde die von E.Kockrick entwickelte inverse Mikroemulsionsmethode[4, 5] verwendet. Die gewonnenen CeO2/Pt-SiCKomposite zeigten spezifische Oberflächen von bis zu 482m²/g bei einer Pyrolysetemperatur von 840 °C. Bei höheren Pyrolysetemperaturen von 1200 bzw. 1500 °C wurden Komposite mit maximal 428 bzw. 87m²/g erhalten. Die katalytischen Untersuchungen der CeO2/Pt-SiC-Komposite erfolgten an einem selbst entwickelten Katalyseteststand mit online-Analytik.[8] Dabei wurden die Totaloxidation, die partielle Oxidation und das Dry Reforming von Methan untersucht. Die Umsetzungstemperatur in der Totaloxidation von Methan konnte um bis zu 443K abgesenkt werden. In der partiellen Oxidation von Methan, wie auch beim Dry Reforming konnte bereits ab einer Reaktortemperatur von 805 °C Umsätze gemäß dem thermodynamischen Gleichgewicht erreicht werden. Die Aktivität in der partiellen Oxidation ist vor allem abhängig vom Platingehalt im Komposit. Die höchste Aktivität war bei den Kompositen mit niedriger Pyrolysetemperatur zu verzeichnen. Nach der Pyrolyse bei 1500 °C hingegen wurden aufgrund der geringeren spezifischen Oberfläche und der damit einhergehenden verminderten Zugänglichkeit der aktiven Zentren geringere Umsätze beobachtet. Einen guten Kompromiss zwischen Oxidationsbeständigkeit und katalytischer Aktivität stellten hier die Komposite dar, die bei 1200 °C pyrolysiert wurden. Mit diesen Kompositen wurden ab 805 °C bis zu 90% Umsatz und 80% Selektivität zu CO in der partiellen Oxidation von Methan und im Dry Reforming erreicht. Beim wiederholten Einsatz der CeO2/Pt-SiC-Komposite in der temperaturprogrammierten Oxidation von Methan konnte nach über 7 Zyklen keine Deaktivierung des Katalysators beobachtet werden. Die Übertragbarkeit der Mikroemulsionsmethode konnte durch den Einsatz verschiedener anderer Katalysatormaterialien gezeigt werden. Die katalytische Aktivität der erhaltenen porösen MI/MII-SiCKomposite wurde in der temperaturprogrammierten Oxidation von Methan mit einer Absenkung der Onsettemperatur um 177K bis 267K bestimmt. Damit stellt die Mikroemulsionsmethode eine flexible und robuste Möglichkeit zur Herstellung poröser SiC-Komposit-Katalysatoren dar. Literatur [1] International Energy Agency; World Energy Outlook, 2010. [2] M. Stöcker, Microporous Mesoporous Mater., 1999, 29(1-2), 3–48. [3] A.P.E. York, T. Xiao, M.L.H. Green, and J.B. Claridge, Catal. Rev. - Sci. Eng., 2007, 49(4), 511 – 560. [4] E. Kockrick, P. Krawiec, U. Petasch, H.-P. Martin, M. Herrmann, and S. Kaskel, Chem. Mater., 2008, 20(1), 77–83. [5] E. Kockrick, R. Frind, M. Rose, U. Petasch, W. Böhlmann, D. Geiger, M. Herrmann, and S. Kaskel, J. Mater. Chem., 2009, 19(11), 1543–1553. [6] M.G. Schwab, I. Senkovska, M. Rose, N. Klein, M. Koch, J. Pahnke, G. Jonschker, B. Schmitz, M. Hirscher, and S. Kaskel, Soft Matter, 2009, 5(5), 1055. [7] R. Frind, M. Oschatz, and S. Kaskel, J. Mater. Chem., 2011, (in Revision). [8] R. Frind, L. Borchardt, E. Kockrick, L. Mammitzsch, U. Petasch, M. Herrmann, and S. Kaskel, Appl. Catal., A, 2011, (in Revision).

An investigation was undertaken to determine the feasibility of increasing the hydrogen production rate by coupling the water gas shift (WGS) process to the hybrid sulphur process (HyS). This investigation also involved the technical and economical analysis of the water gas shift and the H2 separation by means of Pressure swing adsorption (PSA) process. A technical analysis of the water gas shift reaction was determined under the operating conditions selected on the basis of some information available in the literature. The high temperature system (HTS) and low temperature system (LTS) reactors were assumed to be operated at temperatures of 350ºC and 200ºC, respectively. The operating pressure for both reactors was assumed to be 30 atmospheres. The H2 production rate of the partial oxidation (POX) and the WGS processes was 242T/D, which is approximately two times the amount produced by the HyS process alone. The PSA was used for the purification process leading to a hydrogen product with a purity of 99.99%. From the total H2 produced by the POX and the WGS processes only 90 percent of H2 is recovered in the PSA. The unrecovered H2 leaves the PSA as a purge gas together with CO2 and traces of CH4, CO, and saturated H2O. The estimated capital cost of the WGS plant with PSA is about US$50 million. The production cost is highly dependent on the cost of all of the required raw materials and utilities involved. The production cost obtained was US $1.41/kg H2 based on the input cost of synthesis gas as produced by the POX process. In this case the production cost of synthesis gas based on US $6/GJ for natural gas and US $0/Ton for oxygen was estimated to be US $0.154/kg. By increasing the oxygen and natural gas cost, the corresponding increase in synthesis gas has resulted in an increase in H2 production cost of US $1.84/kg. / Thesis (M.Sc. (Chemical Engineering))--North-West University, Potchefstroom Campus, 2006.

Made available in DSpace on 2014-12-17T15:42:13Z (GMT). No. of bitstreams: 1 ValdeliceRS_TESE.pdf: 2586359 bytes, checksum: e3d9d5d8e2c97ad0990f43fd755545a2 (MD5) Previous issue date: 2010-11-26 / One of the main applications of methane is in the production of syngas, a mixture of hydrogen and carbon monoxide. Procedures used in this process are steam reforming, CO2 reforming, partial oxidation and autothermal reforming. The present study evaluated and compared the behavior of nickel catalysts supported on mixed oxides of cerium and manganese in the partial oxidation of methane with that of nickel catalysts supported on mixed oxides of cerium and zirconium. Mixed oxides of cerium and zirconium or cerium and manganese were synthesized using two different preparation methods, the polymeric precursor based on Pechini method and combustion reaction using a microwave. This was followed by impregnation with nickel content of 15 %. Samples were calcined at 300, 800 and 900 ?C and characterized by specific surface area (SSA), X-ray fluorescence (XRF), X-ray diffraction (XRD), scanning electron microscopy (SEM), temperature programmed reduction (TPR) and the reaction of partial oxidation of methane. The specific areas of samples decrease with the rise in calcination temperature and after nickel impregnation. Metal-cerium solid solution was formed and the presence of other manganese species outside the solid solution structure was confirmed in the compound with the highest amounts of manganese oxides showed. With regard to scanning electron microscopy, supports based on cerium and zirconium prepared by Pechini method exhibited agglomerated particles without uniform geometry or visible pores on the surface. However, compounds containing manganese presented empty spaces in its structure. Through synthesis by combustion reaction, morphology acquired independently of the proposed composition demonstrated greater porosity in relation to Pechini synthesis. Although catalysts were prepared using different synthesis methods, the insertion of nickel showed very similar reduction profiles (TPR). In relation to nickel catalysts supported on mixed oxide of cerium and zirconium, there is an initial reduction of NiO species that present certain interaction with the support. This is followed by the reduction of Ce4+ in Ce3+ surface, with subsequent bulk reduction. For catalysts containing manganese, a reduction of nickel oxide species occurs, followed by two stages of reduction for species Mn2O3 in Mn3O4 and Mn3O4 in MnO, with subsequent reduction of bulk. With respect to partial oxidation reactions, the nickel catalyst supported on mixed oxide of cerium and zirconium, prepared using the Pechini method, exhibited CH4 conversion of approximately 80 %, with conversion of 81 % when prepared by combustion. This behavior continued for 10 hours of reaction. Manganese content was also found to directly influence catalytic activity of materials; the greater the manganese oxide content, the faster deactivation and destabilization occurred in the catalyst. In both synthesis methods, the nickel catalyst supported on mixed oxide of cerium and zirconium maintained an H2/CO ratio very close to 2 during the 10 hours of partial oxidation reaction. Samples containing manganese displayed smaller H2/CO ratios and lower performance in partial oxidation. / Uma das principais aplica??es do metano ? a produ??o de g?s de s?ntese, mistura de hidrog?nio e mon?xido de carbono. Os processos utilizados na produ??o de g?s de s?ntese a partir do metano s?o: reforma a vapor, reforma com CO2, oxida??o parcial e reforma autot?rmica. Neste trabalho, o comportamento de catalisadores de n?quel suportados em ?xidos mistos de c?rio e mangan?s na rea??o de oxida??o parcial do metano foi avaliado e comparado com o catalisador de n?quel suportados no ?xido misto de c?rio e zirc?nio. Os ?xidos mistos de c?rio e zirc?nio ou c?rio e mangan?s foram sintetizadas usando dois diferentes m?todos de prepara??o; o de precursores polim?ricos baseado no processo Pechini e por rea??o de combust?o usando um micro-ondas, seguido da impregna??o de n?quel com teor de 15 %. As amostras foram calcinadas a 300, 800 e 900 ?C e caracterizados por ?rea espec?fica (ASE), fluoresc?ncia de raios X (FRX), difra??o de raios X (DRX), microscopia eletr?nica de varredura (MEV), redu??o ? temperatura programada (RTP) e a rea??o de oxida??o parcial do metano. As ?reas espec?ficas das amostras diminuem com o aumento da temperatura de calcina??o e ap?s a impregna??o com n?quel. A solu??o s?lida c?rio-metal foi formada e nos composto com as maiores quantidades de ?xidos de mangan?s verificou-se a presen?a de outras esp?cies de mangan?s fora da estrutura da solu??o s?lida. Quanto ? microscopia eletr?nica de varredura os suportes a base de c?rio e zirc?nio preparados via Pechini exibem part?culas aglomeradas, sem geometria uniforme e sem a visualiza??o de poros na superf?cie, enquanto os compostos contendo mangan?s apresentaram alguns vazios na sua estrutura. Atrav?s da s?ntese por rea??o de combust?o a morfologia adquirida independente da composi??o proposta apresentou uma maior porosidade em rela??o ? s?ntese Pechini. Mesmo sendo os catalisadores preparados por diferentes m?todos de s?ntese, a inser??o de n?quel deixou seus perfis de redu??o (RTP) muito semelhantes. Para os catalisadores de n?quel suportados no ?xido misto de c?rio e zirc?nio, h? em primeiro lugar redu??o de esp?cies NiO que apresentam certa intera??o com o suporte, seguido da redu??o de Ce4+ em Ce3+ superficiais, com posterior redu??o do bulk. Para os catalisadores contendo mangan?s h? a redu??o das esp?cies de ?xido de n?quel, seguido de duas etapas de redu??o para as esp?cies Mn2O3 em Mn3O4 e Mn3O4 em MnO, com posterior redu??o do bulk. Quanto ?s rea??es de oxida??o parcial, o catalisador de n?quel suportados no ?xido misto de c?rio e zirc?nio preparado via m?todo Pechini, apresentou uma convers?o de CH4 de cerca de 80 %, sendo 81 % a convers?o quando preparado via combust?o. Esse comportamento manteve-se durante 10 horas de rea??o. Observou-se tamb?m que o teor de mangan?s influencia diretamente na atividade catal?tica dos materiais, quanto maior o teor de ?xido de mangan?s mais r?pido o catalisador apresentava desativa??o e desestabiliza??o. Para ambos os m?todos de s?ntese o catalisador de n?quel suportados no ?xido misto de c?rio e zirc?nio manteve a raz?o H2/CO bem pr?xima de 2 durante as 10 horas em que ocorre a rea??o de oxida??o parcial. As amostras contendo mangan?s apresentaram menores raz?es de H2/CO e menor desempenho na oxida??o parcial.

An investigation was undertaken to determine the feasibility of increasing the hydrogen production rate by coupling the water gas shift (WGS) process to the hybrid sulphur process (HyS). This investigation also involved the technical and economical analysis of the water gas shift and the H2 separation by means of Pressure swing adsorption (PSA) process. A technical analysis of the water gas shift reaction was determined under the operating conditions selected on the basis of some information available in the literature. The high temperature system (HTS) and low temperature system (LTS) reactors were assumed to be operated at temperatures of 350ºC and 200ºC, respectively. The operating pressure for both reactors was assumed to be 30 atmospheres. The H2 production rate of the partial oxidation (POX) and the WGS processes was 242T/D, which is approximately two times the amount produced by the HyS process alone. The PSA was used for the purification process leading to a hydrogen product with a purity of 99.99%. From the total H2 produced by the POX and the WGS processes only 90 percent of H2 is recovered in the PSA. The unrecovered H2 leaves the PSA as a purge gas together with CO2 and traces of CH4, CO, and saturated H2O. The estimated capital cost of the WGS plant with PSA is about US$50 million. The production cost is highly dependent on the cost of all of the required raw materials and utilities involved. The production cost obtained was US $1.41/kg H2 based on the input cost of synthesis gas as produced by the POX process. In this case the production cost of synthesis gas based on US $6/GJ for natural gas and US $0/Ton for oxygen was estimated to be US $0.154/kg. By increasing the oxygen and natural gas cost, the corresponding increase in synthesis gas has resulted in an increase in H2 production cost of US $1.84/kg. / Thesis (M.Sc. (Chemical Engineering))--North-West University, Potchefstroom Campus, 2006.

An investigation was undertaken to determine the feasibility of increasing the hydrogen production rate by coupling the water gas shift (WGS) process to the hybrid sulphur process (HyS). This investigation also involved the technical and economical analysis of the water gas shift and the H2 separation by means of Pressure swing adsorption (PSA) process. A technical analysis of the water gas shift reaction was determined under the operating conditions selected on the basis of some information available in the literature. The high temperature system (HTS) and low temperature system (LTS) reactors were assumed to be operated at temperatures of 350°C and 200°C, respectively. The operating pressure for both reactors was assumed to be 30 atmospheres. The H2 production rate of the partial oxidation (POX) and the WGS processes was 242T/D, which is approximately two times the amount produced by the HyS process alone. The PSA was used for the purification process leading to a hydrogen product with a purity of 99.99%. From the total H2 produced by the POX and the WGS processes only 90 percent of H2 is recovered in the PSA. The unrecovered H2 leaves the PSA as a purge gas together with C02 and traces of CH4, CO, and saturated H20. The estimated capital cost of the WGS plant with PSA is about US$50 million. The production cost is highly dependent on the cost of all of the required raw materials and utilities involved. The production cost obtained was US $1.41/kg H2 based on the input cost of synthesis gas as produced by the POX process. In this case the production cost of synthesis gas based on US $6/GJ for natural gas and US $0/Ton for oxygen was estimated to be US $0.154/kg. By increasing the oxygen and natural gas cost, the corresponding increase in synthesis gas has resulted in an increase in H2 production cost of US $1.84/kg. / Thesis (M.Sc. (Nuclear Engineering))--North-West University, Potchefstroom Campus, 2009.

An investigation was undertaken to determine the feasibility of increasing the hydrogen production rate by coupling the water gas shift (WGS) process to the hybrid sulphur process (HyS). This investigation also involved the technical and economical analysis of the water gas shift and the H2 separation by means of Pressure swing adsorption (PSA) process. A technical analysis of the water gas shift reaction was determined under the operating conditions selected on the basis of some information available in the literature. The high temperature system (HTS) and low temperature system (LTS) reactors were assumed to be operated at temperatures of 350°C and 200°C, respectively. The operating pressure for both reactors was assumed to be 30 atmospheres. The H2 production rate of the partial oxidation (POX) and the WGS processes was 242T/D, which is approximately two times the amount produced by the HyS process alone. The PSA was used for the purification process leading to a hydrogen product with a purity of 99.99%. From the total H2 produced by the POX and the WGS processes only 90 percent of H2 is recovered in the PSA. The unrecovered H2 leaves the PSA as a purge gas together with C02 and traces of CH4, CO, and saturated H20. The estimated capital cost of the WGS plant with PSA is about US$50 million. The production cost is highly dependent on the cost of all of the required raw materials and utilities involved. The production cost obtained was US $1.41/kg H2 based on the input cost of synthesis gas as produced by the POX process. In this case the production cost of synthesis gas based on US $6/GJ for natural gas and US $0/Ton for oxygen was estimated to be US $0.154/kg. By increasing the oxygen and natural gas cost, the corresponding increase in synthesis gas has resulted in an increase in H2 production cost of US $1.84/kg. / Thesis (M.Sc. (Nuclear Engineering))--North-West University, Potchefstroom Campus, 2009.