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.

FundaÃÃo Cearense de Apoio ao Desenvolvimento Cientifico e TecnolÃgico / A biomassa lÃquida residual de processos agrÃcolas e agroindustriais em geral representa um recurso renovÃvel em quantidade expressiva sem uma destinaÃÃo econÃmica e ambientalmente sustentÃvel Como exemplo a soluÃÃo quanto aos estoques de glicerina resultante da transesterificaÃÃo de Ãleos vegetais para obtenÃÃo do biodiesel tem sido postergada pela carÃncia de alternativas de engenharia apropriadas ao aproveitamento adequado dessa biomassa Por essa razÃo foi iniciado o desenvolvimento de um reator de gaseificaÃÃo destinado à biomassa lÃquida pela via da oxidaÃÃo parcial onde à empregada uma tecnologia de combustÃo nÃo convencional a CombustÃo de FiltraÃÃo como base de projeto para a concepÃÃo do reator em que a biomassa de referÃncia utilizada foi o glicerol (C3H8O3) Este trabalho eminentemente experimental foi realizado com a construÃÃo de um protÃtipo de reator de gaseificaÃÃo em escala de laboratÃrio em que seu queimador à preenchido completamente por esferas cerÃmicas de alumina (Al2O3) formando assim uma matriz porosa inerte que fica parcialmente imersa no glicerol na sua extremidade inferior e que envolve um trocador de calor instalado na parte superior do reator O processo à investigado no sentido de identificar algumas caracterÃsticas fundamentais de projeto tais como: limite de operaÃÃo do reator em termos de misturas arcombustÃvel; presenÃa de fenÃmenos de instabilidade; velocidade de propagaÃÃo da onda de combustÃo; e influÃncia dos principais parÃmetros de operaÃÃo, razÃo de equivalÃncia taxa de consumo de combustÃvel e vazÃes de ar e Ãgua na reaÃÃo Embora toda a experimentaÃÃo tenha se restringido a ensaiar o gaseificador para produÃÃo de gÃs de sÃntese pelo mÃtodo da oxidaÃÃo parcial a investigaÃÃo teÃrica foi mais abrangente englobando a reforma autotÃrmica Os experimentos respaldados por instrumentos de monitoramento e anÃlise cromatogrÃfica foram apoiados por um estudo teÃrico a partir de um modelo analÃtico simplificado com base na reaÃÃo global de oxidaÃÃo parcial associada à reaÃÃo de deslocamento ÃguaâgÃs Resultados experimentais demonstraram a viabilidade do processo constatando estabilidade operacional em ampla faixa de razÃo de equivalÃncia e eficiÃncia de conversÃo (>20%) do glicerol em gÃs de sÃntese mantendo extraÃÃo de energia da reaÃÃo / The residual liquid biomass from agricultural and agroindustrial processes in general way represents a renewable resource in significant amount without an economically and environmentally sustainable destination For instance the solution concerning glycerin stocks remaining from the vegetable oil transesterification for obtaining biodiesel has been postponed due to the lack of engineering alternatives appropriate to the proper utilization of this biomass Therefore the development of a liquid biomass gasification reactor based on partial oxidation has been initiated where a non conventional combustion technology has been employed Filtration Combustion as a design basis for the reactor conception in which the reference biomass used was glycerol This work eminently experimental was carried out to build a gasification reactor prototype in laboratory scale in which its burner is completely filled by ceramic spheres of alumina (Al2O3) thus forming a inert porous matrix which is partially immersed in glycerol at its bottom end and which involves a heat exchanger installed at the top of the reactor The process is investigated to identify some key design features such as: reactor operation limit in terms of fuel-air mixtures; occurrence of instability phenomena; combustion wave propagation velocity; and influence of the main operation parameters equivalence ratio fuel consumption rate and air and water flow rates into the reaction Although all experimentation has been restricted to test the gasifier for the production of synthesis gas by partial oxidation method theoretical investigation was broader comprising the autothermal reforming The experiments supported by monitoring instruments and chromatographic analysis were supported by a theoretical study based on a simplified analytical model considering the global reaction of partial oxidation associated with water-gas shift reaction Experimental results have demonstrated the feasibility of the process providing operational stability over a wide range of equivalence ratio and conversion efficiency (>20%) of glycerol to syngas while maintaining energy extraction from reaction

Vehicles powered by fuel cells are from an environmentalaspect superior to the traditional automobile using internalcombustion of gasoline. Power systems which are based upon fuelcell technology require hydrogen for operation. The ideal fuelcell vehicle would operate on pure hydrogen stored on-board.However, storing hydrogen on-board the vehicle is currently notfeasible for technical reasons. The hydrogen can be generatedon-board using a liquid hydrogen carrier such as methanol andgasoline. The objective of the work presented in this thesiswas to develop a catalytic hydrogen generator for automotiveapplications using methanol as the hydrogen carrier. The first part of this work gives an introduction to thefield of methanol reforming and the properties of a fuel cellbased power system. Paper I reviews the catalytic materials andprocesses available for producing hydrogen from methanol. The second part of this thesis consists of an experimentalinvestigation of the influence of the catalyst composition,materials and process parameters on the activity andselectivity for the production of hydrogen from methanol. InPapers II-IV the influence of the support, carrier andoperational parameters is studied. In Paper V an investigationof the catalytic properties is performed in an attempt tocorrelate material properties with performance of differentcatalysts. In the third part of the thesis an investigation isperformed to elucidate whether it is possible to utilizeoxidation of liquid methanol as a heat source for an automotivereformer. In the study which is presented in Paper VI a largeseries of catalytic materials are tested and we were able tominimize the noble metal content making the system more costefficient. In the final part of this thesis the reformer prototypedeveloped in the project is evaluated. The reformer which wasconstructed for serving a 5 kWe fuel cell had a highperformance with near 100 % methanol conversion and COconcentrations below 1 vol% in the product stream. The resultsof this part are presented in Paper VII. <b>Keywords:</b>methanol, fuel cell, vehicle, catalyst,copper, hydrogen, on-board, steam reforming, partial oxidation,combined reforming, oxidative steam reforming, auto-thermalreforming, zinc, zirconium, chromium, aluminium oxide,manganese, characterization, temperature programmed reduction,X-ray diffraction, chemisorption, carbon monoxide, poisoning,reformer.

Propylene epoxidation reaction was investigated on catalytic surfaces of chlorinated copper(I) oxide and ruthenium(IV) oxide using periodic density functional theory (DFT). Cu2O(001) and (110) surface of RuO2 was selected to generate chlorinated surfaces to be used in the study. Besides epoxidation, other reactions that compete with epoxidation were also studied such as formations of allyl-radical, acrolein, acetone on chlorinated Cu2O(001) and formations of propionaldehyde, allyl-radical and acetone on chlorinated RuO2(110) surface. Path of each reaction was determined by CI-NEB method and transition state analyses. Generally accepted stable surface intermediate mechanism was utilized in reactions to final products. The surface intermediate favorable on the surfaces in this study was determined to be the intermediate that is not preferable on metallic surfaces under low oxygen. On chlorinated Cu2O(001) surface, formation of propylene oxide, acetone and acrolein have higher probability than gas phase allyl-radical since the desorption energy of allyl-radical was calculated to be 70kcal/mol which is a relatively high value. In fact it is desirable since gas phase allyl-radical is known to be the precursor of combustion products. On chlorinated RuO2(110) surface, desorption Propylene epoxidation reaction was investigated on catalytic surfaces of chlorinated copper(I) oxide and ruthenium(IV) oxide using periodic density functional theory (DFT). Cu2O(001) and (110) surface of RuO2 was selected to generate chlorinated surfaces to be used in the study. Besides epoxidation, other reactions that compete with epoxidation were also studied such as formations of allyl-radical, acrolein, acetone on chlorinated Cu2O(001) and formations of propionaldehyde, allyl-radical and acetone on chlorinated RuO2(110) surface. Path of each reaction was determined by CI-NEB method and transition state analyses. Generally accepted stable surface intermediate mechanism was utilized in reactions to final products. The surface intermediate favorable on the surfaces in this study was determined to be the intermediate that is not preferable on metallic surfaces under low oxygen. On chlorinated Cu2O(001) surface, formation of propylene oxide, acetone and acrolein have higher probability than gas phase allyl-radical since the desorption energy of allyl-radical was calculated to be 70kcal/mol which is a relatively high value. In fact it is desirable since gas phase allyl-radical is known to be the precursor of combustion products. On chlorinated RuO2(110) surface, desorption observed to be possible on chlorinated RuO2(110) surface but not possible on chlorinated Cu2O(001). When activation barriers and desorption energies of all possible reactions are compared on chlorinated RuO2(110) surface / gas phase propylene oxide generated directly seems as the preferable product with allylradical although it was computed to have high desorption energy. Comparison of activation barriers obtained in this study on chlorinated Cu2O(001) with the barriers of nonchlorinated surface revealed chlorine slightly increases the activation barrier of unwanted allylic hydrogen stripping and hence slightly decreases the probability of occurance. When chlorine is placed closer to reaction site, activation barrier of allylic hydrogen stripping reaction increases further. The effect of chlorine might be electronic since the charge of oxygen at reaction site slightly becomes less negative when the place of chlorine gets closer to the reaction site on the surface. Similar comparison between chlorinated and nonchlorinated RuO2(110) surfaces revealed that chlorine addition does not improve the surface toward propylene oxide formation, rather it is detrimental as chlorine addition caused a decrease in unwanted allylic hydrogen stripping reaction.

In this study, catalytic activity of the Co and/or Pb-SBA-15 mesoporous catalysts in methane partial oxidation reaction was investigated. By using sol-gel, incipient wetness impregnation and post grafting method, SBA-15 samples are incorporated with Co and/or Pb at different weight loadings to provide a controlled geometry in nanometer scale. The characterization of the synthesized samples was done by XRD, N2 adsorption isotherms, FTIR, TEM images, Raman and XPS analysis. In the present study also, gas phase methane partial oxidation modeling and the synthesizing of mesoporous SBA-15 silica with different pore sizes were investigated. For the samples prepared by sol-gel method, XRD analysis showedthat cobalt exists in the form of Co3O4and Pb exist in the form of PbO. BET surface areas of the Co loaded catalysts are in the range of 479.5-640.1 m2/g. However, in Pb loaded samples, higher metal loading decrease the surface area up to 4.63 m2/g. Considering the both Co and Pb containing bi-metallic samples, TEM and BET results revealed that the ordered hexagonal mesostructure was fully destroyed. The samples prepared by incipient wetness impregnation and post grafting method characterized by using BET, TEM, Raman and XPS analysis. According to the BET results all the samples show ordered mesostructure in agreement with TEM results for all Co and/or SBA-15 mesoporous samples. TEM results also revealed that, the Co(5%) Pb(5%)-SBA-15 catalyst prepared by incipient wetness impregnation method possess big cobalt and lead oxide crystallines on the mesoporous structure. Raman analysis results indicated that cobalt exist in Co3O4 form. According to XPS results all samples containing cobalt include Co3O4. The partial oxidation of methane was carried out in a fixed bed flow-type reactor in a temperature range of 50&ndash / 850&deg / C under atmospheric pressure.According to the reaction test results, the 0.5%Rh-Co-SBA15 catalyst shows the highest methane conversion (82%) and H2 selectivity. The non-precious metal show lower reactivities, addition of Pb to the Co-SBA-15 catalyst increases the catalytic activity and decrease the H2 production temperature.

<p>Vehicles powered by fuel cells are from an environmentalaspect superior to the traditional automobile using internalcombustion of gasoline. Power systems which are based upon fuelcell technology require hydrogen for operation. The ideal fuelcell vehicle would operate on pure hydrogen stored on-board.However, storing hydrogen on-board the vehicle is currently notfeasible for technical reasons. The hydrogen can be generatedon-board using a liquid hydrogen carrier such as methanol andgasoline. The objective of the work presented in this thesiswas to develop a catalytic hydrogen generator for automotiveapplications using methanol as the hydrogen carrier.</p><p>The first part of this work gives an introduction to thefield of methanol reforming and the properties of a fuel cellbased power system. Paper I reviews the catalytic materials andprocesses available for producing hydrogen from methanol.</p><p>The second part of this thesis consists of an experimentalinvestigation of the influence of the catalyst composition,materials and process parameters on the activity andselectivity for the production of hydrogen from methanol. InPapers II-IV the influence of the support, carrier andoperational parameters is studied. In Paper V an investigationof the catalytic properties is performed in an attempt tocorrelate material properties with performance of differentcatalysts.</p><p>In the third part of the thesis an investigation isperformed to elucidate whether it is possible to utilizeoxidation of liquid methanol as a heat source for an automotivereformer. In the study which is presented in Paper VI a largeseries of catalytic materials are tested and we were able tominimize the noble metal content making the system more costefficient.</p><p>In the final part of this thesis the reformer prototypedeveloped in the project is evaluated. The reformer which wasconstructed for serving a 5 kWe fuel cell had a highperformance with near 100 % methanol conversion and COconcentrations below 1 vol% in the product stream. The resultsof this part are presented in Paper VII.</p><p><b>Keywords:</b>methanol, fuel cell, vehicle, catalyst,copper, hydrogen, on-board, steam reforming, partial oxidation,combined reforming, oxidative steam reforming, auto-thermalreforming, zinc, zirconium, chromium, aluminium oxide,manganese, characterization, temperature programmed reduction,X-ray diffraction, chemisorption, carbon monoxide, poisoning,reformer.</p>

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).

The presence of excess free radicals in the body can result in severe health consequences because of oxidative damage to cells. Spin traps may be used as a probe to examine radical reactions in cells, but there is a need for less toxic and more lipid soluble examples. Melatonin is one of the numerous antioxidants used to scavenge free radicals in the body and reportedly one of the most efficient radical scavengers known. It is relatively nontoxic and easily crosses the lipid bilayer in cell membranes. Melatonin is thought to undergo a multistep oxidation process and this work investigates the potential for it to be used as a spin trap. The presence of electron withdrawing or donating groups added to melatonin may stabilize an intermediate and allow it to function as a spin trap. The essence of this study is to conduct a computational inquiry into the relative stability of melatonin, selected derivatives, and the partial oxidation products formed from the scavenging of hydroxyl radical. To determine this, geometries were optimized for each molecule at the DFT/B3LYP/6-31G(d) and HF/6-31G(d) levels of theory.