Neutron slowing down with inelastic scattering

The emphasis in reactor physics research has shifted toward investigations of fast reactors. The effects of high energy neutron processes have thus become fundamental to our understanding, and one of the most important of these processes is nuclear inelastic scattering. In this research we include inelastic scattering as a primary energy transfer mechanism, and study the resultant neutron energy spectrum in an infinite medium. We assume that the moderator material has a high mass number, so that in a laboratory coordinate system the energy loss of an inelastically scattered neutron may be taken as discrete. It is then consistent to treat elastic scattering with an age theory expansion. Mathematically these assumptions lead to balance equations of the differential-difference type.

The steady state problem is explored first by way of Laplace transformation of the energy variable. We then develop another steady state technique, valid for multiple inelastic level excitations, which depends on the level structure satisfying a physically reasonable constraint. In all cases the solutions we generate are compared with results obtained by modeling inelastic scattering with a separable, evaporative kernel.

The time dependent problem presents some new difficulties. By modeling the elastic scattering cross section in a particular way, we generate solutions to this more interesting problem. We conjecture the method of characteristics may be useful in analyzing time dependent problems with general cross sections. These ideas are briefly explored.

Recursos de combustible en central nuclear de fusión en el País Vasco

[ES]Este trabajo surge de la inquietud del alumno sobre la energía nuclear y mas concretamente sobre la energía de fusión. Esta inquietud se plasma en una recopilación de información sobre los combustibles necesarios , su abundancia y su forma de obtención actual. Analizaremos la posibilidad de implantar alguna de estas plantas de combustible en el País Vasco, junto con un estudio de una posible central nuclear de fusión con la suma de la potencia de cada uno de los reactores de fisión que se encuentran actualmente en funcionamiento en el estado Español. Compararemos las cantidades de combustible necesarias en un año de uranio y el combustible de fusión, así como el coste de construcción de cada una.

Bioestímulo e bioaumento na remediação de solo contaminado com óleo lubrificante usado escala piloto

O óleo lubrificante mineral é amplamente utilizado no cenário mundial no funcionamento de máquinas e motores. No entanto, o ciclo de vida deste petro-derivado resulta na geração de um resíduo (óleo lubrificante usado), o qual é nocivo ao meio ambiente quando não descartado adequadamente ou reciclado. No Brasil, apesar das normas que tratam especificamente do armazenamento, recolhimento e destino de óleo lubrificante usado, grande parte do mesmo ainda é despejado diretamente no meio ambiente, sem qualquer tratamento, sendo de grande importância estudos que visem o entendimento dos processos e o desenvolvimento de tecnologias de remediação de áreas contaminadas por esse resíduo. O objetivo geral do presente trabalho foi conduzir estudos de tratabilidade de solo arenoso contaminado experimentalmente com 5% (m m-1 seco) de óleo lubrificante usado, através de duas diferentes estratégias de biorremediação: bioestímulo e bioaumento. Foram conduzidos dois experimentos. No primeiro, foi avaliada a atividade microbiana aeróbia na biodegradação do OLU através do método respirométrico de Bartha. No segundo, foram montados três biorreatores de fase sólida simulando biopilhas estáticas com aeração forçada, cada um contendo 125 kg de solo e 5% (m m-1 seco) de óleo lubrificante automotivo usado, os quais receberam como tratamento: bioestímulo por ajuste de pH e umidade (BIOSca); bioestímulo por ajuste de pH e umidade associado ao bioaumento com a adição de composto maduro (BIOA1ca) ; e bioestímulo por ajuste de pH e umidade associado ao bioaumento com a adição de composto jovem (BIOA2ca). Foram também montados três biorreatores de bancada simulando biopilhas estáticas sem aeração forçada, cada um contendo 3 kg de solo e 5% (m m-1) do mesmo contaminante, sendo que o primeiro continha solo sem contaminação - CONTsa, o segundo, solo contaminado com ajuste de pH BIOSsa e o terceiro, solo contaminado com adição de 0,3% de azida sódica - ABIOsa. Os tratamentos foram avaliados pela remoção de hidrocarbonetos totais de petróleo (HTPs) e após 120 dias de experimento obteve-se remoções de HTPs de 84,75%, 99,99% e 99,99%, com BIOS, BIOA1 e BIOA2, respectivamente, demonstrando que a estratégia de bioestímulo associada ao bioaumento foram promissoras na remediação do solo contaminado pelo óleo lubrificante usado. Os tratamentos que receberam composto (BIOA1 e BIOA2) não apresentaram diferenças quanto à remoção de HTPs, evidenciando que a fase de maturação dos compostos não apresentou influência na eficiência do processo. No entanto, verificou-se uma eficiência nos tratamentos que receberam composto quando comparado ao tratamento sem adição de composto

Avaliação de diferentes estratégias de biorremediação de solo argiloso contaminado por óleo em biorreator de fase semi-sólida

A prática da troca de óleo lubrificante usado, particularmente óleos automotivos, representa um grave problema ambiental em função de sua natureza perigosa, do manuseio incorreto e do descarte indiscriminado no meio ambiente. A investigação quanto à remediação de áreas contaminadas por esse resíduo torna-se necessária, particularmente para solo de natureza argilosa. O presente estudo teve por objetivo avaliar a biorremediação de um solo argiloso contaminado por óleo lubrificante utilizando biorreatores de fase semi-sólida. Frascos tipo Erlenmeyer, contendo 20 g de solo contaminado com 3% (m/m) de óleo lubrificante, em triplicata, foram mantidos em temperatura e agitação constantes, segundo as seguintes estratégias de tratamento: (i) Bioestímulo com ajuste de nutrientes (BIOE); (ii) Bioaumento com adição de inóculo microbiano aclimatado (BIOA); (iii) Bioestímulo e adição de surfactante sintético Tween-80 (BIOES); (iv) Bioaumento, bioestímulo e surfactante sintético Tween-80 (BIOAS) e (iv) controle, com água destilada purificada (CONT). A eficiência de remoção do contaminante foi avaliada após 68 dias de tratamento por análises de evolução de CO2, redução de COT, decaimento de HTP, de n-alcanos e frações de hidrocarbonetos saturados, aromáticos e compostos polares. O tratamento BIOAS resultou na maior produção de CO2 acumulada (1247,0 mg.20g-1 de solo) seguida pelo tratamento BIOES (1077,6 mg.20g-1 de solo). Ao final do experimento, todos os tratamentos reduziram significativamente os teores de HTPs quando comparados ao controle (11,14,2%). Os tratamentos BIOAS e BIOES não apresentaram diferenças significativas quanto à redução de HTPs (42,03,7% e 37,46,3%, respectivamente). Tanto o bioestímulo quanto o bioaumento mostraram-se estratégias com potencial para aumentar a eficácia da biorremediação de solos argilosos, sendo que a adição de surfactante foi o fator mais importante, tendo aumentado significativamente a capacidade de remoção em ambas as estratégias. O uso de biorreatores em fase semi-sólida na biorremediação de solo argiloso contaminado com óleo lubrificante mostrou-se bastante promissor e tal estratégia pode ser aplicada em escala imediatamente superior

Dielectric recovery of short A-C arcs between low-boiling-point electrodes

The re-ignition characteristics (variation of re-ignition voltage with time after current zero) of short alternating current arcs between plane brass electrodes in air were studied by observing the average re-ignition voltages on the screen of a cathode-ray oscilloscope and controlling the rates of rise of voltage by varying the shunting capacitance and hence the natural period of oscillation of the reactors used to limit the current. The shape of these characteristics and the effects on them of varying the electrode separation, air pressure, and current strength were determined.

The results show that short arc spaces recover dielectric strength in two distinct stages. The first stage agrees in shape and magnitude with a previously developed theory that all voltage is concentrated across a partially deionized space charge layer which increases its breakdown voltage with diminishing density of ionization in the field-tree space. The second stage appears to follow complete deionization by the electric field due to displacement of the field-free region by the space charge layer, its magnitude and shape appearing to be due simply to increase in gas density due to cooling. Temperatures calculated from this second stage and ion densities determined from the first stage by means of the space charge equation and an extrapolation of the temperature curve are consistent with recent measurements of arc value by other methods. Analysis or the decrease with time of the apparent ion density shows that diffusion alone is adequate to explain the results and that volume recombination is not. The effects on the characteristics of variations in the parameters investigated are found to be in accord with previous results and with the theory if deionization mainly by diffusion be assumed.

Tratamento de efluentes líquidos na Estação Antártica Comandante Ferraz (EACF): avaliação da aplicabilidade do processo eletrolítico.

Esta pesquisa enfoca o uso do processo eletrolítico, como alternativa para tratamento de efluentes líquidos na Estação Antártica Comandante Ferraz (EACF), considerando as limitações ambientais locais e aspectos de consumo de energia. Este processo, classificado como não convencional, vem sendo estudado pela comunidade científica nacional e internacional para tratamento de diversos efluentes, inclusive esgotos domésticos, apresentando várias vantagens que estimularam a verificação de sua aplicabilidade para as condições peculiares da EACF. Foram realizados ensaios, em escala de laboratório, com esgotos domésticos coletados em um condomínio no Rio de Janeiro, usando reatores eletrolíticos com capacidade de 4 L, com eletrodos de desgaste de alumínio (Al) e de ferro (Fe), distância entre as placas de 0,9 cm e 1,8 cm, temperaturas na faixa de 7C a 22C, e ensaios para verificação da sua eficiência, por meio de parâmetros como DQO, DBO5, SST, turbidez e volume de lodo gerado. Sob temperatura de 15C e condições de condutividade da ordem de 900 S/cm, estimada para os esgotos da EACF, aplicando densidade de corrente de 22,9 A/m2, 4,5 V, tempo de retenção de 25 min, os resultados apresentaram valores de DQO no efluente tratado de 65 mg/L(redução de 89%), DBO de 56 mg/L (redução de 64 %), SST de 8 mg/L, com turbidez de 11,3 uT e, após filtração, turbidez de 3,2 uT, consumo de energia de 0,8 Wh/L. O aspecto é límpido e a qualidade final obtida é compatível para ser submetida a tratamento de desinfecção. A partir dos dados obtidos, foram avaliadas por meio de pré-projeto: a viabilidade de sua implantação em container, a estimativa de consumo de energia e de lodo gerado, requisitos de manutenção, operação, além da sugestão de monitoramentos e de medidas de mitigação de impactos ambientais associados à respectiva instalação.

Modelagem, simulação e otimização operacional de unidades de síntese de metanol

A indústria de processos químicos tem sofrido consideráveis transformações devido ao acirramento da competitividade. Importantes progressos tecnológicos têm sido atingidos através de técnicas de modelagem, simulação e otimização visando o aumento da lucratividade e melhoria contínua nos processos industriais. Neste contexto, as plantas de metanol, um dos mais importantes produtos petroquímicos, podem ser destacadas. Atualmente, a principal matéria-prima para obtenção de metanol é o gás natural. A produção do metanol é caracterizada por três etapas: geração de gás de síntese, conversão do gás de síntese em metanol (unidade de síntese ou loop de síntese) e purificação do produto na especificação requerida. Os custos fixos e variáveis da unidade de síntese são fortemente dependentes das variáveis operacionais, como temperatura, pressão, razão de reciclo e composição da carga. Desta forma, foi desenvolvido um conjunto de modelos e algoritmos computacionais para representar matematicamente unidades de síntese de metanol. O modelo apresenta operações unitárias associadas aos seguintes equipamentos: divisores de correntes, misturadores de correntes, compressores, trocadores de calor, vasos de flash e reatores. Inicialmente, foi proposto um simulador estacionário, que serviu como base para um pseudo-estacionário, o qual contempla a desativação do catalisador por sinterização térmica. Os simuladores foram criados segundo uma arquitetura seqüencial modular e empregou-se o método de substituição sucessiva para a convergência dos reciclos. O estudo envolveu dois fluxogramas típicos, um constituído por reatores adiabáticos em série, enquanto o outro constituído por um reator tipo quench. Uma análise do efeito das principais variáveis operacionais foi realizada para o reator e para o loop de síntese. Estudou-se também o efeito da desativação do catalisador ao longo do tempo. Uma ferramenta de otimização operacional foi empregada para alcançar a máxima produção manipulando as injeções de carga fria na entrada dos leitos catalíticos. Formulou-se também um problema de maximização do lucro em função da otimização de paradas da unidade para troca do catalisador. Os resultados obtidos apontam que a ferramenta desenvolvida é promissora para a compreensão e otimização da unidade objeto deste estudo

The scope for biomanipulation in improving water quality

Biomanipulation is a form of biological engineering in which organisms are selectively removed or encouraged to alleviate the symptoms of eutrophication. Most examples involve fish and grazer zooplankton though mussels have also been used. The technique involves continuous management in many deeper lakes and is not a substitute for nutrient control. In some lakes, alterations to the lake environment have given longer-term positive effects. And in some shallow lakes, biomanipulation may be essential, alongside nutrient control, in re- establishing former aquatic-plant-dominated ecosystems which have been lost through severe eutrophication. The emergence of biomanipulation techniques emphasises that lake systems are not simply chemical reactors which respond simply to engineered chemical changes, but very complex and still very imperfectly understood ecosystems which require a yet profounder understanding before they can be restored with certainty.

Management of Biesboch reservoirs for quality control with special reference to eutrophication

The three Biesbosch Reservoirs are pumped storage reservoirs, fed with rather polluted and highly eutrophic water from the River Meuse. Air injection at the bottom of the reservoirs prevents thermal stratification, which would otherwise result in serious water quality deterioration. Reservoir mixing also serves as an economic algal control measure; mixing over sufficient depth causes light to play the role of limiting factor and this, combined with zooplankton grazing, keeps the biomass of phytoplankton at acceptable levels. Special problems are caused by benthic, geosmin-producing Oscillatoria species growing on the inner embankment. Rooting up the bottom with a harrow is used as the method of control, based on underwater observations by biological staff trained as SCUBA-divers. With regard to pollutant behaviour the three reservoirs act as a series of fully mixed reactors. This enables the application of kinetic models to describe their behaviour and allows the use of a selective intake policy, e.g. for suspended solids with associated contaminants, ammonia and polynuclear aromatic hydrocarbons. A combination of selective intake and self- purification processes - enhanced by the compartmentalisation of the storage volume in three reservoirs - leads to a striking improvement for many water-quality parameters.

Estimation of catalyst activity profiles and deactivation parameters from reactor operating data with applications to naphtha reforming

Techniques are developed for estimating activity profiles in fixed bed reactors and catalyst deactivation parameters from operating reactor data. These techniques are applicable, in general, to most industrial catalytic processes. The catalytic reforming of naphthas is taken as a broad example to illustrate the estimation schemes and to signify the physical meaning of the kinetic parameters of the estimation equations. The work is described in two parts. Part I deals with the modeling of kinetic rate expressions and the derivation of the working equations for estimation. Part II concentrates on developing various estimation techniques.

Part I: The reactions used to describe naphtha reforming are dehydrogenation and dehydroisomerization of cycloparaffins; isomerization, dehydrocyclization and hydrocracking of paraffins; and the catalyst deactivation reactions, namely coking on alumina sites and sintering of platinum crystallites. The rate expressions for the above reactions are formulated, and the effects of transport limitations on the overall reaction rates are discussed in the appendices. Moreover, various types of interaction between the metallic and acidic active centers of reforming catalysts are discussed as characterizing the different types of reforming reactions.

Part II: In catalytic reactor operation, the activity distribution along the reactor determines the kinetics of the main reaction and is needed for predicting the effect of changes in the feed state and the operating conditions on the reactor output. In the case of a monofunctional catalyst and of bifunctional catalysts in limiting conditions, the cumulative activity is sufficient for predicting steady reactor output. The estimation of this cumulative activity can be carried out easily from measurements at the reactor exit. For a general bifunctional catalytic system, the detailed activity distribution is needed for describing the reactor operation, and some approximation must be made to obtain practicable estimation schemes. This is accomplished by parametrization techniques using measurements at a few points along the reactor. Such parametrization techniques are illustrated numerically with a simplified model of naphtha reforming.

To determine long term catalyst utilization and regeneration policies, it is necessary to estimate catalyst deactivation parameters from the the current operating data. For a first order deactivation model with a monofunctional catalyst or with a bifunctional catalyst in special limiting circumstances, analytical techniques are presented to transform the partial differential equations to ordinary differential equations which admit more feasible estimation schemes. Numerical examples include the catalytic oxidation of butene to butadiene and a simplified model of naphtha reforming. For a general bifunctional system or in the case of a monofunctional catalyst subject to general power law deactivation, the estimation can only be accomplished approximately. The basic feature of an appropriate estimation scheme involves approximating the activity profile by certain polynomials and then estimating the deactivation parameters from the integrated form of the deactivation equation by regression techniques. Different bifunctional systems must be treated by different estimation algorithms, which are illustrated by several cases of naphtha reforming with different feed or catalyst composition.

Desempenho de um reator para compostagem descentralizada de lixo orgânico domiciliar e grau de maturação do composto

Nas últimas décadas, a disposição final de lixo tornou-se um sério problema a ser enfrentado por todos os países, em função da escassez crescente de terrenos disponíveis para aterros sanitários e distância cada vez maior dos centros geradores e a disposição final, assim como do aumento substancial da geração per capita. A acumulação de lixo nos grandes centros populacionais estimula a proliferação de macro e microvetores (ratos, baratas, moscas, vírus, bactérias, parasitos) e conseqüentemente, a disseminação de doenças. Em particular, com relação ao lixo gerado em ilhas e comunidades isoladas, é de alta relevância estratégias baseadas na descentralização do tratamento da fração orgânica de lixo domiciliar, com fim do transporte através de barcas para o continente, gerando mau cheiro e riscos de poluição ambiental. O presente projeto teve por objetivo: Testar o mesmo reator de compostagem descentralizada sob condições do verão sueco, alimentando-o com resíduos de restaurantes da cidade costeira Kalmar e sob condições brasileiras, alimentando-o com resíduos de cozinha da escola municipal de Abraão-Ilha Grande, RJ; propor modificações mecânicas e/ou operacionais para otimização dos processos; avaliar a qualidade e o grau de maturação do composto de diferentes fases através do método respirométrico Specific Oxygen Uptake Rate (SOUR)o método respirométrico NBR 14283 da ABNT. Em resumo, concluiu-se que a composição do lixo e pH inicial do material estruturante adicionado são fatores determinantes do tempo requerido para degradação dos ácidos orgânicos gerados e subseqüente elevação do pH; dependendo das características dos resíduos orgânicos, é necessária a inclusão de inoculante (ex: composto) para melhor desenvolvimento de bactérias e fungos e, conseqüentemente, otimização do processo; as análises físico-químicas e microbiológicas confirmaram que o processo de degradação aeróbia ocorre no interior do corpo principal do reator e que a qualidade do composto gerado é satisfatória; entretanto, melhorias consideráveis no sistema de trituração e alimentação são requeridas para que o reator testado possa se usado em sua capacidade plena. Os testes respirométrico atráves do Specific Oxygen Uptake Rate(SOUR) e da norma NBR 14283 da ABNT mostraram-se ambos eficazes na identificação do grau de maturação do composto e do avanço do processo de compostagem. Uma vez removidos os problemas mecânicos de trituração e alimentação, o reator testado poderá ser utilizado como uma tecnologia inovadora do tratamento de lixo orgânico in situ para pequenos e médios geradores de lixo orgânico domiciliar.

Optimization of the pyrolysis process for the production of a biomass derived reducing agent and hydrogen-rich gases

221 p.

Advanced Reaction Systems for Hydrogen Production

[EN] This PhD work started in March 2010 with the support of the University of the Basque Country (UPV/EHU) under the program named “Formación de Personal Investigador” at the Chemical and Environmental Engineering Department in the Faculty of Engineering of Bilbao. The major part of the Thesis work was carried out in the mentioned department, as a member of the Sustainable Process Engineering (SuPrEn) research group. In addition, this PhD Thesis includes the research work developed during a period of 6 months at the Institut für Mikrotechnik Mainz GmbH, IMM, in Germany. During the four years of the Thesis, conventional and microreactor systems were tested for several feedstocks renewable and non-renewable, gases and liquids through several reforming processes in order to produce hydrogen. For this purpose, new catalytic formulations which showed high activity, selectivity and stability were design. As a consequence, the PhD work performed allowed the publication of seven scientific articles in peer-reviewed journals. This PhD Thesis is divided into the following six chapters described below. The opportunity of this work is established on the basis of the transition period needed for moving from a petroleum based energy system to a renewable based new one. Consequently, the present global energy scenario was detailed in Chapter 1, and the role of hydrogen as a real alternative in the future energy system was justified based on several outlooks. Therefore, renewable and non-renewable hydrogen production routes were presented, explaining the corresponding benefits and drawbacks. Then, the raw materials used in this Thesis work were described and the most important issues regarding the processes and the characteristics of the catalytic formulations were explained. The introduction chapter finishes by introducing the concepts of decentralized production and process intensification with the use of microreactors. In addition, a small description of these innovative reaction systems and the benefits that entailed their use were also mentioned. In Chapter 2 the main objectives of this Thesis work are summarized. The development of advanced reaction systems for hydrogen rich mixtures production is the main objective. In addition, the use and comparison between two different reaction systems, (fixed bed reactor (FBR) and microreactor), the processing of renewable raw materials, the development of new, active, selective and stable catalytic formulations, and the optimization of the operating conditions were also established as additional partial objectives. Methane and natural gas (NG) steam reforming experimental results obtained when operated with microreactor and FBR systems are presented in Chapter 3. For these experiments nickel-based (Ni/Al2O3 and Ni/MgO) and noble metal-based (Pd/Al2O3 and Pt/Al2O3) catalysts were prepared by wet impregnation and their catalytic activity was measured at several temperatures, from 973 to 1073 K, different S/C ratios, from 1.0 to 2.0, and atmospheric pressure. The Weight Hourly Space Velocity (WHSV) was maintained constant in order to compare the catalytic activity in both reaction systems. The results obtained showed a better performance of the catalysts operating in microreactors. The Ni/MgO catalyst reached the highest hydrogen production yield at 1073 K and steam-to-carbon ratio (S/C) of 1.5 under Steam methane Reforming (SMR) conditions. In addition, this catalyst also showed good activity and stability under NG reforming at S/C=1.0 and 2.0. The Ni/Al2O3 catalyst also showed high activity and good stability and it was the catalyst reaching the highest methane conversion (72.9 %) and H2out/CH4in ratio (2.4) under SMR conditions at 1073 K and S/C=1.0. However, this catalyst suffered from deactivation when it was tested under NG reforming conditions. Regarding the activity measurements carried out with the noble metal-based catalysts in the microreactor systems, they suffered a very quick deactivation, probably because of the effects attributed to carbon deposition, which was detected by Scanning Electron Microscope (SEM). When the FBR was used no catalytic activity was measured with the catalysts under investigation, probably because they were operated at the same WHSV than the microreactors and these WHSVs were too high for FBR system. In Chapter 4 biogas reforming processes were studied. This chapter starts with an introduction explaining the properties of the biogas and the main production routes. Then, the experimental procedure carried out is detailed giving concrete information about the experimental set-up, defining the parameters measured, specifying the characteristics of the reactors used and describing the characterization techniques utilized. Each following section describes the results obtained from activity testing with the different catalysts prepared, which is subsequently summarized: Section 4.3: Biogas reforming processes using γ-Al2O3 based catalysts The activity results obtained by several Ni-based catalysts and a bimetallic Rh-Ni catalyst supported on magnesia or alumina modified with oxides like CeO2 and ZrO2 are presented in this section. In addition, an alumina-based commercial catalyst was tested in order to compare the activity results measured. Four different biogas reforming processes were studied using a FBR: dry reforming (DR), biogas steam reforming (BSR), biogas oxidative reforming (BOR) and tri-reforming (TR). For the BSR process different steam to carbon ratios (S/C) from 1.0 to 3.0, were tested. In the case of BOR process the oxygen-to-methane (O2/CH4) ratio was varied from 0.125 to 0.50. Finally, for TR processes different S/C ratios from 1.0 to 3.0, and O2/CH4 ratios of 0.25 and 0.50 were studied. Then, the catalysts which achieved high activity and stability were impregnated in a microreactor to explore the viability of process intensification. The operation with microreactors was carried out under the best experimental conditions measured in the FBR. In addition, the physicochemical characterization of the fresh and spent catalysts was carried out by Inductively Coupled Plasma Atomic Emission Spectroscopy (ICP-AES), N2 physisorption, H2 chemisorption, Temperature Programmed Reduction (TPR), SEM, X-ray Photoelectron Spectroscopy (XPS) and X-ray powder Diffraction (XRD). Operating with the FBR, conversions close to the ones predicted by thermodynamic calculations were obtained by most of the catalysts tested. The Rh-Ni/Ce-Al2O3 catalyst obtained the highest hydrogen production yield in DR. In BSR process, the Ni/Ce-Al2O3 catalyst achieved the best activity results operating at S/C=1.0. In the case of BOR process, the Ni/Ce-Zr-Al2O3 catalyst showed the highest reactants conversion values operating at O2/CH4=0.25. Finally, in the TR process the Rh-Ni/Ce-Al2O3 catalyst obtained the best results operating at S/C=1.0 and O2/CH4=0.25. Therefore, these three catalysts were selected to be coated onto microchannels in order to test its performance under BOR and TR processes conditions. Although the operation using microreactors was carried out under considerably higher WHSV, similar conversions and yields as the ones measured in FBR were measured. Furthermore, attending to other measurements like Turnover Frequency (TOF) and Hydrogen Productivity (PROD), the values calculated for the catalysts tested in microreactors were one order of magnitude higher. Thus, due to the low dispersion degree measured by H2-chemisorption, the Ni/Ce-Al2O3 catalyst reached the highest TOF and PROD values. Section 4.4: Biogas reforming processes using Zeolites L based catalysts In this section three type of L zeolites, with different morphology and size, were synthesized and used as catalyst support. Then, for each type of L zeolite three nickel monometallic and their homologous Rh-Ni bimetallic catalysts were prepared by the wetness impregnation method. These catalysts were tested using the FBR under DR process and different conditions of BSR (S/C ratio of 1.0 and 2.0), BOR (O2/CH4 ratio of 0.25 and 0.50) and TR processes (at S/C=1.0 and O2/CH4=0.25). The characterization of these catalysts was also carried out by using the same techniques mentioned in the previous section. Very high methane and carbon dioxide conversion values were measured for almost all the catalysts under investigation. The experimental results evidenced the better catalytic behavior of the bimetallic catalysts as compared to the monometallic ones. Comparing the catalysts behavior with regards to their morphology, for the BSR process the Disc catalysts were the most active ones at the lowest S/C ratio tested. On the contrary, the Cylindrical (30–60 nm) catalysts were more active under BOR conditions at O2/CH4=0.25 and TR processes. By the contrary, the Cylindrical (1–3 µm) catalysts showed the worst activity results for both processes. Section 4.5: Biogas reforming processes using Na+ and Cs+ doped Zeolites LTL based catalysts A method for the synthesis of Linde Type L (LTL) zeolite under microwave-assisted hydrothermal conditions and its behavior as a support for heterogeneously catalyzed hydrogen production is described in this section. Then, rhodium and nickel-based bimetallic catalysts were prepared in order to be tested by DR process and BOR process at O2/CH4=0.25. Moreover, the characterization of the catalysts under investigation was also carried out. Higher activities were achieved by the catalysts prepared from the non-doped zeolites, Rh-Ni/D and Rh-Ni/N, as compared to the ones supported on Na+ and Cs+ exchanged supports. However, the differences between them were not very significant. In addition, the Na+ and Cs+ incorporation affected mainly to the Disc catalysts. Comparing the results obtained by these catalysts with the ones studied in the section 4.4, in general worst results were achieved under DR conditions and almost the same results when operated under BOR conditions. In Chapter 5 the ethylene glycol (EG) as feed for syngas production by steam reforming (SR) and oxidative steam reforming (OSR) was studied by using microchannel reactors. The product composition was determined at a S/C of 4.0, reaction temperatures between 625°C and 725°C, atmospheric pressure and Volume Hourly Space Velocities (VHSV) between 100 and 300 NL/(gcath). This work was divided in two sections. The first one corresponds to the introduction of the main and most promising EG production routes. Then, the new experimental procedure is detailed and the information about the experimental set-up and the measured parameters is described. The characterization was carried out using the same techniques as for the previous chapter. Then, the next sections correspond to the catalytic activity and catalysts characterization results. Section 5.3: xRh-cm and xRh-np catalysts for ethylene glycol reforming Initially, catalysts with different rhodium loading, from 1.0 to 5.0 wt. %, and supported on α-Al2O3 were prepared by two different preparation methods (conventional impregnation and separate nanoparticle synthesis). Then, the catalysts were compared regarding their measured activity and selectivity, as well as the characterization results obtained before and after the activity tests carried out. The samples prepared by a conventional impregnation method showed generally higher activity compared to catalysts prepared from Rh nanoparticles. By-product formation of species such as acetaldehyde, ethane and ethylene was detected, regardless if oxygen was added to the feed or not. Among the catalysts tested, the 2.5Rh-cm catalyst was considered the best one. Section 5.4: 2.5Rh-cm catalyst support modification with CeO2 and La2O3 In this part of the Chapter 5, the catalyst showing the best performance in the previous section, the 2.5Rh-Al2O3 catalyst, was selected in order to be improved. Therefore, new Rh based catalysts were designed using α-Al2O3 and being modified this support with different contents of CeO2 or La2O3 oxides. All the catalysts containing additives showed complete conversion and selectivities close to the equilibrium in both SR and OSR processes. In addition, for these catalysts the concentrations measured for the C2H4, CH4, CH3CHO and C2H6 by-products were very low. Finally, the 2.5Rh-20Ce catalyst was selected according to its catalytic activity and characterization results in order to run a stability test, which lasted more than 115 hours under stable operation. The last chapter, Chapter 6, summarizes the main conclusions achieved throughout this Thesis work. Although very high reactant conversions and rich hydrogen mixtures were obtained using a fixed bed reaction system, the use of microreactors improves the key issues, heat and mass transfer limitations, through which the reforming reactions are intensified. Therefore, they seem to be a very interesting and promising alternative for process intensification and decentralized production for remote application.

Condições de contorno albedo para cálculos globais de reatores nucleares térmicos com o modelo de ordenadas discretas a dois grupos de energia

Como eventos de fissão induzida por nêutrons não ocorrem nas regiões nãomultiplicativas de reatores nucleares, e.g., moderador, refletor, e meios estruturais, essas regiões não geram potência e a eficiência computacional dos cálculos globais de reatores nucleares pode portanto ser aumentada eliminando os cálculos numéricos explícitos no interior das regiões não-multiplicativas em torno do núcleo ativo. É discutida nesta dissertação a eficiência computacional de condições de contorno aproximadas tipo albedo na formulação de ordenadas discretas (SN) para problemas de autovalor a dois grupos de energia em geometria bidimensional cartesiana. Albedo, palavra de origem latina para alvura, foi originalmente definido como a fração da luz incidente que é refletida difusamente por uma superfície. Esta palavra latina permaneceu como o termo científico usual em astronomia e nesta dissertação este conceito é estendido para reflexão de nêutrons. Este albedo SN nãoconvencional substitui aproximadamente a região refletora em torno do núcleo ativo do reator, pois os termos de fuga transversal são desprezados no interior do refletor. Se o problema, em particular, não possui termos de fuga transversal, i.e., trata-se de um problema unidimensional, então as condições de contorno albedo, como propostas nesta dissertação, são exatas. Por eficiência computacional entende-se analisar a precisão dos resultados numéricos em comparação com o tempo de execução computacional de cada simulação de um dado problema-modelo. Resultados numéricos para dois problemas-modelo com de simetria são considerados para ilustrar esta análise de eficiência.