Traditionally, lead-based bearing overlays dominate the commercial automotive market and it has been proven that an excellent combination of properties can be attained through their use. However, lead is a toxic metal and a cumulative poison in humans. According to the European Union End-of-Life Vehicle (ELV) Directive proposed in 1997, vehicles that registered in'all the member states after 1st July 2003 should contain no lead, mercury, cadmium and hexavalent chromium. In this study, a new sulphate-gluconate electrolyte was used to produce multilayer SnCo coatings, aimed at a lead-free overlay for future market use. Tin-cobalt compositionally modulated alloy (CMA) coatings produced from sulphategluconate electrolytes have been previously examined as a potential replacement for lead-free bearing overlays [1]. However, some obstacles may exist which limit their potential use on an industrial scale. For example, long electroplating times are required to produce a thick coating which is very undesirable from an industrial viewpoint, and also the possible elemental interdiffusion occurring in the coating system under engine operating temperatures could rapidly deteriorate the coating properties. In addition, there is an increasing demand from automotive industry to further improve bearing overlay properties, for example for high performance and high compression ratio engines.

Reservoir heterogeneities exhibit a wide range of length scales, and their interaction with various transport mechanisms control the overall performance of subsurface flow and transport processes. Modeling these processes at large-scales requires proper scale-up of both heterogeneity and the underlying transport mechanisms. This research demonstrates a new reservoir modeling procedure to systematically quantify the scaling characteristics of transport processes by accounting for sub-scale heterogeneities and their interaction with various transport mechanisms based on the volume averaging approach. Although treatments of transport problems with the volume averaging technique have been published in the past, application to real geological systems exhibiting complex heterogeneity is lacking. A novel procedure, where results from a fine-scale numerical flow simulation reflecting the full physics of the transport process albeit over a small sub-volume of the reservoir, can be integrated with the volume averaging technique to provide effective description of transport at the coarse scale. In a volume averaging procedure, scaled up equations describing solute transport in single-phase flow are developed. Scaling characteristics of effective transport coefficient corresponding to different reservoir heterogeneity correlation lengths as well as different transport mechanisms including convection, dispersion, and diffusion are studied. The method is subsequently extended to describe transport in multiphase systems to study scaling characteristics of processes involving adsorption and inter-phase transport. Key conclusions drawn from this dissertation show that 1) variance of reservoir properties and flow responses generally decrease with scale; 2) scaling of recovery processes can be described by the scaling of effective mass transfer coefficient (Keff); in particular, mean and variance of Keff decrease with length scale, similar in the fashion of recovery statistics (e.g., variances in tracer breakthrough time and recovery); 3) the scaling of Keff depends on the underlying heterogeneity and is influenced by the dominant transport mechanisms. To show the versatility of the approach for studying scale-up of other transport mechanisms, it is also applied to derive scaled up formulations of non-Newtonian polymer flow to investigate the scaling characteristics of the apparent viscosity and effective shear rate in porous media. / text

Cereals contain naturally occurring biopolymers (for example proteins and starches) that can be used as renewable raw materials in a variety of speciality chemical applications. The separation of protein and starch biopolymers from wheat is well established and relies on a group of proteins called glutens that have a unique network-forming functionality. Oat and other cereals do not naturally contain these gluten proteins and typically rely on chemical-based separation techniques which alter the chemical and physical structures and damage the inherent natural functionality of the biopolymers. This research study investigated the separation of the protein and starch fractions from cereals using the Al-Hakkak Process, a new aqueous process. This process involves adding water and wheat gluten protein to cereals that do not contain gluten. The wheat gluten interacts with the cereal proteins, facilitating the separation of the starch and protein fractions whilst retaining their inherent natural functionality. The aim of this research project was to investigate and optimise the pilot scale separation performance of the Al-Hakkak Process using oat flour. As very little prior research had been carried out, the focus was to characterise the oat starch and protein separation performance and gain an understanding of the mechanisms involved. A variety of techniques were employed. Large scale deformation rheology was used to gain an understanding of the oat-gluten dough rheology and establish the relationship between the rheology and the separation performance. Confocal scanning laser microscopy was used to investigate the structure of the oat-gluten protein network. The molecular interactions between the oat and gluten proteins were studied using gel electrophoresis. The network-forming functionality of the new oat-gluten protein was explored. The influence of various processing parameters on the pilot scale separation performance was investigated and the results compared with other data collected through the study to identify key processing parameters. This research programme has resulted in interesting, encouraging and some unexpected outcomes and these are discussed in detail in the thesis. It was concluded that an insoluble protein network formed in the oat-gluten dough and both kneading and extraction processes were found to contribute to the formation of this. A key conclusion was that the changes that took place in the oat-gluten dough were similar to, but not identical to, the changes that occur in wheat dough. It was proposed that the mechanism for the development of a protein network in oat-gluten dough differed from wheat dough for two main reasons: a) the presence of the oat flour disrupted the normal wheat gluten behaviour, and b) components in the oat flour altered the activity of the gluten proteins. The research identified key processing parameters for the Al-Hakkak Process including kneading time, gluten content, and sodium chloride content of the oat-gluten dough as well as sodium chloride concentration, pH, and temperature of the extract liquor. An important discovery was that the oat and gluten proteins interacted at a molecular level through reducible, covalent, bonding (most likely disulphide linkages) to form the insoluble protein network in the oat-gluten dough. It was concluded that these reducible bonds coupled the individual protein subunits to form new hybrid oat-gluten protein molecules (a combination of oat proteins and gluten proteins). Both insoluble and soluble proteins in the oat and gluten flour were involved in the formation of the insoluble protein network in the oat-gluten dough. This outcome has applications beyond the Al-Hakkak Process, as this new knowledge can be applied to the wider dough processing industry. It was concluded that the wheat gluten was the source of the protein network-forming functionality of the hybrid oat-gluten protein and that the oat proteins had a diluting effect. It was proposed that oat-gluten protein flour from the Al-Hakkak Process could be reused to replace the commercial wheat gluten flour in subsequent production batches. During spray drying of the starch stream, the soluble biopolymers in the extract liquor were found to act as an adhesive and glued individual starch granules together to form spherical agglomerates. Acidification of the extract liquor was found to enhance this agglomeration. It was proposed the acidified starch granules were sticker during spray drying due to the partial acid hydrolysis of the starch granule suface which enhanced the agglomeration.

Doctor of Philosophy / Department of Chemical Engineering / Mary E. Rezac / Reversible organic reactions, such as esterification, transesterification, and acetalisation, have enjoyed numerous laboratory uses and industrial applications since they are convenient means to synthesize esters and ketals. Reversible organic reactions are limited by thermodynamic equilibrium and often do not proceed to completion. High yields for these equilibrium driven reactions can be obtained either by adding a large excess of one of the reactants, which results a reactant(s)/product(s) mixture requiring a separation, or by the selective removal of by-products. Conventional removal techniques including distillation, adsorption, and absorption have drawbacks in terms of efficiency as well as reactor design. Pervaporation membrane reactors are promising systems for these reactions since they have simpler designs, and are more energy efficient compared to conventional downstream separation techniques. This project created a general protocol that can guide one to carry out experiments and collect necessary data for transferring membrane reactor design concepts to the construction of industrial-scale membrane reactors for organic synthesis. Demonstration of this protocol was achieved by (1) experimental evaluation of membrane reactor performance, (2) modeling, and (3) scale-up. The capability of membranes for water/organic separations and organic/organic separations during reversible reactions was investigated. Our results indicated that enhanced membrane reactors selectively removed the by-product water and methanol from reaction mixtures and achieved high conversions for all investigated reactions. Second, modeling and simulation of pervaporation membrane reactor performance for reversible reactions were carried out. The simulated performance agrees well with experimental data. Using the developed model, the effects of permeate pressure and membrane selectivity on membrane reactor yield were examined. Finally, a scale-up on transesterification membrane reactors was carried out. The membrane modules investigated included a bench-scale flat sheet membrane, a bench-scale hollow fiber membrane module, and a pilot-scale hollow fiber membrane module. A 100% conversion was obtained by the selective methanol removal. It is found that with high methanol selectivity membranes, the reaction time to achieve a given conversion continuously decreases with increasing the methanol removal capacity of the reactor system. However, this is a highly nonlinear relationship.

Ocean Thermal Energy Conversion (OTEC) is a renewable energy technology that has to overcome several key challenges before achieving its ultimate goal of producing baseload power on a commercial scale. The economic challenge of deploying an OTEC plant remains the biggest barrier to implementation. Although small OTEC demonstration plants and recent advances in subsystem technologies have proven OTEC’s technical merits, the process still lacks the crucial operational data required to justify investments in large commercial OTEC plants on the order of 50-100 megawatts of net electrical power (MWe-net). A pre-commercial pilot plant on the order of 5-10 MWe-net is required for an OTEC market to evolve. In addition to the economic challenge,OTEC plants have potential for adverse environmental impacts from redistribution of nutrients and residual chemicals in the discharge plume. Although long-term operational records are not available for commercial sizeOTEC plants, synergistic operational data can be leveraged from the desalination industry to improve the potential for OTEC commercialization. Large capacity desalination plants primarily use membranes or thermal evaporator tubes to transform enormous amounts of seawater into freshwater. Thermal desalination plants in particular possess many of the same technical, economic, and environmental traits as a commercial scale OTEC plant. Substantial long-term economic data and environmental impact results are now widely available since commercial desalination began in the 1950s. Analysis of this data indicates that the evolution of the desalination industry could be akin to the potential future advancement of OTEC. Furthermore, certain scenarios exist where a combined OTEC-desalination plant provides a new opportunity for commercial plants. This paper seeks to utilize operational data from the desalination industry as a progressive approach towards OTEC commercialization.

No presente trabalho, dados de ampliacao de escala, de um processo de pre-tratamento alcalino em escala laboratorial (2L) para escala piloto (350L) foram avaliados. Os experimentos realizados previamente em escala laboratorial apontaram duas condições potenciais para a ampliacao de escala, a saber: Ensaio 5 (130°C, 30 min, 1,5% m/v NaOH, 0,15% m/m antraquinona) apresentando a maior conversao enzimatica da polpa obtida (64,5%) e Ensaio 7 (170°C, 1,5 % m/v NaOH, 30 min, 0,15% m/m antraquinona) com a maior solubilizacao de lignina (81,0 %). Os experimentos em escala piloto foram realizados nas condicoes apontadas, com e sem a adicao de antraquinona. A reprodutibilidade dos dados em escala piloto foi satisfatoria, considerando o sistema de aquecimento e agitacao mais eficientes do reator piloto em relacao ao reator usado no laboratorio. O uso da antraquinona diminuiu a solubilizacao de carboidratos durante o pretratamento (evitando 67% de solubilizacao quando comparado a reacao sem antraquinona, a 130°C), mas interferiu negativamente na etapa subsequente de hidrolise, principalmente na reacao a 170°C. Dentre as condicoes testadas, o ensaio 5Pil/AQ (130°C, 30 min, 1,5% NaOH e 0,15% m/m antraquinona) foi eleito como a melhor condicao de pre-tratamento, com maior rendimento em carboidratos apos a hidrolise enzimatica, sendo possivel obter (extrapolando os resultados) 290 kg de glicose e 98 kg de xilose a partir de uma tonelada de bagaco (base seca). Para a obtencao de etanol a partir desse hidrolisado, foram realizadas fermentacoes com tres diferentes leveduras - S. cerevisiae CAT-1, S. stipitis NRRL Y-7124 e S. passalidarum NRRL Y-27907. O melhor resultado foi apresentado para fermentacao em batelada alimentada aplicando reciclo de celulas utilizando a levedura S. passalidarum, produzindo 23,3 g/L de etanol (97 % do teorico) com produtividade de 0,90 g/L.h em 24 h de fermentacao no terceiro reciclo. O processo de pre-tratamento alcalino gera, alem da polpa rica em carboidratos, um hidrolisado rico em lignina. A lignina foi precipitada desse hidrolisado apos cada pre-tratamento realizado e caracterizada, apresentando poder calorifico entre 22,8 e 25,3 MJ/kg. / In this study, data scale up for an alkaline pretreatment process from lab to pilot scale was evaluated. Lab scale experiments indicated two potential conditions for the scale-up, namely: 130°C, 30 min, 1.5% w/v NaOH, 0.15% w/w anthraquinone , presenting the highest enzymatic conversion (64.5%); and 170°C, 30 min, 1.5% w/v NaOH, 0.15% w/w anthraquinone with the highest lignin solubilization (81.0 %). The experiments were performed on pilot scale under the aforementioned conditions, with and without anthraquinone. Data reproducibility on pilot scale was satisfactory considering the more efficient heating and stirring reactor system when compared to the reactor in lab scale. Anthraquinone decreases the solubilization of carbohydrates during pretreatment (avoiding 67% solubilization compared to the reaction without anthraquinone, at 130°C), but interferes negatively in the subsequent hydrolysis step, mostely at 170°C. Among the conditions tested, the test performed at 130°C, 30 min, 1.5% w/v NaOH and with 0.15% w/w anthraquinone was chosen as the best pretreatment condition, with the highest carbohydrate conversion after enzymatic hydrolysis, allowing 290 kg of glucose and 98 kg of xylose per a dry base ton of bagasse. In order to produce ethanol from this hydrolyzate, fermentations with three different yeasts were performed - S. cerevisiae CAT-1, S. stipites NRRL Y-7124, S. passalidarum NRRL Y-27907. Fed-batch fermentation with S. passalidarum cell recycling provided the best result, yielding 23.3 g/L ethanol, 97 % (theoretical yield) with 0.90 g/L.h productivity within 24 h of fermentation. The alkaline pretreatment process generates, besides the pulp rich in carbohydrates, a lignin-rich hydrolyzate. Lignin was precipitated from the hydrolyzate obtained after each pretreatment carried out and characterized, presenting heating values between 22.8 and 25.3 MJ/kg.

It is estimated that over a third of the diet in the Western world is made up of oils and fats, of which a prominent percentage is in the form of emulsion food products, including milks, creams, yoghurts, margarines, salad dressings, desserts, soups and cheese. Current processing techniques involve the extraction and refining of edible oils using high temperatures and organic solvents, followed by re-encapsulation of the oil, for incorporation into the required emulsion products. The research presented in this PhD thesis was performed within the auspices of the UK Department of Environment, Food and Rural Affairs (DEFRA) funded, Sustainable Emulsion Ingredients through Bio-Innovation (SEIBI) project, which involved collaboration with researchers from the University of Nottingham together with a consortium of industrial partners. SEIBI was initiated to investigate a novel processing route for the production of food-grade rape and sunflowerseed oil emulsions from aqueously extracted oil-bodies. Being less energy and chemical intensive, the novel process offered potential reductions in both greenhouse gas emissions and wider environmental impacts when compared with conventional processing. Using Life Cycle Assessment (LCA) techniques, the environmental burdens of the aqueous oil-body extraction process were determined and compared with those of the existing technology route. To facilitate this, the research focussed on six key objectives, designed to both identify the environmental loads of the systems involved and scrutinise the impact of a number of methodological choices for LCA. These included choice of allocation method, normalisation, scaling issues distinct for novel processes and the extent to which the single-issue LCA variant, carbon footprinting could be used as an environmental indicator for the system. LCAs for four separate categories of product systems were developed encompassing seed oils, mayonnaises, aqueously extracted oil-body materials and mayonnaise-like oil-body emulsions. In addition to generating the environmental profiles required to fulfil the research objectives, the analysis of these models enabled the generation of original knowledge through the quantification of impacts for a range of processes that had either not previously been assessed or for which no published data could be found. The novel process was concluded as having clear potential for improved environmental performance over current technology even in its' pre-optimised, although the methodological choices examined were found to have profound effects on these and other results. Oil-body yield from seed was identified as key for optimisation to further maximise the environmental gains, with modest improvements, well within those theoretically possible being required for the novel process to better the environmental credentials of current technology in all key impact areas. The original outputs from this thesis will be of considerable use to developers involved in the continued advancement of the oil-body extraction technology, together with researchers within the edible oils and emulsions sector. In addition, the methodological outputs will help to inform LCA practitioners and developers in the continuing quest to understand the capabilities and limitations of this powerful analytical tool.

Este trabalho estudou a aplicação de oito métodos clássicos de escalonamento de tanques condicionadores, testando sua validade para dois tanques de geometria semelhante, mas com diferentes volumes (V1=10 e V2=49 decímetros cúbicos). No interior dos tanques, operavam impulsores (diâmetro D1=0,078m x D2=0,132m) que exibiam três distintos desenhos (2 pás versus 4 pás inclinadas em 45 graus versus turbina de Rushton). Sua rotação (N1 no tanque menor x N2 no tanque maior) visava à suspensão de partículas grossas de apatita (diâmetro médio = 254 micrometros) em polpas com 40% de sólidos em massa. Para balizar o escalonamento, adotou-se como variável de controle a mínima rotação do impulsor (Njs) que é capaz de fazer com que nenhuma partícula repouse no fundo do tanque por mais do que 1 ou 2 segundos (Critério 1-s), além de perfis axiais de distribuição de sólidos e a extensão da Zona Turbulenta versus Zona Quiescente no interior dos tanques. A diferença entre o valor previsto de Njs para o tanque de 49 decímetros cúbicos (N2) pelos métodos de escalonamento versus o valor de Njs (N2) determinado experimentalmente foi expressa como erro percentual (E). Consideraram-se como adequados para a aplicação que constitui o objetivo desta dissertação todos os métodos que exibiram E menor que 10%. Para o impelidor de 2 pás inclinadas, a adequação do método baseado na constância da razão potência/volume (E=2%) e também do método empírico de Rautzen (E=6%), indica a expressão N2=N1.(D1/D2) com seu expoente da relação entre os diâmetros variando entre 0,67 e 0,75 para a aplicação desejada. Considerando o impulsor de 4 pás inclinadas, a adequação do método da constância da razão potência/volume (E=4%); assim como dos métodos empíricos de Rautzen (E=0%) e Zwietering (5%), sugere o uso da expressão N2=N1.(D1/D2) com seu expoente da relação entre os diâmetros variando entre 0,67 e 0,85. Para a turbina de Rushton, o único método que exibiu E menor que 10% foi o da constância da relação potência/volume (E=8%), cuja expressão é N2=N1.(D1/D2) com seu expoente da relação entre os diâmetros igual a 0,67. Uma vez que a determinação do valor real de N2 foi baseada numa técnica experimental influenciada pelas limitações do observador, pode-se inferir que uma expressão geral de escalonamento do tipo N2=N1.(D1/D2) com seu expoente da relação entre os diâmetros igual a 0,75 atende aos propósitos desta aplicação. Por outro lado, o uso da relação P/V provê um critério mais objetivo para se balizar o escalonamento, haja vista que ele se adequou a todos os três tipos de impelidores contemplados por este estudo. / This work has studied the application of eight classical methods appointed by literature to accomplish the scale-up of stirred tanks which aimed to suspend slurries of 40% of solids, containing coarse (mean diameter=254 micrometers) apatite particles. The validity of the methods was accomplished by using two tanks of similar geometry but different capacity (V1=10 e V2=49 cubic decimeter), together with impellers of different diameter (D1=0,078m versus D2=0,132m) and design (turbine of 2 or 4 blades inclined at 45 degrees and Rushton turbine). To assist the process of validation, the impeller speed (Njs) under which no particle rests on the bottom of the tank for more than 1-2 seconds (1-s Criterium) was used together with the axial profile of solids percent distribution plus the extension of the turbulent versus quiescent zones within the two tanks. For any of the eight scale-up methods, the difference between the predicted value of Njs (N2) for the 49 cubic decimeter tank and the actual value (experimental) of the same variable was determined and its magnitude was expressed in terms of the percent error (E). The methods that yielded E less than 10% were considered as suitable for the aimed application. Considering the 2-inclined blade impeller, low value of E yielded by the method based on the constancy of the ratio power/volume (E=2%) and also by the empiric method of Rautzen (E=6%) indicate that the expression N2=N1.(D1/D2) with its exponent of the relation between diameters ranging between 0,67 and 0,75 is suitable for the desired application. Regarding the 4-inclined blade impeller, because the method based on the constancy of the ratio power/volume (E=4%) and also the empiric methods of Rautzen (E=0%) and Zwietering (E=5%) yielded the lowest values of E, the expression N2=N1.(D1/D2) with its exponent of the relation between diameters ranging between 0,67 and 0,85 is suitable for the aimed application. Moreover, for the Rusthon turbine, only the method based on the constancy of the ratio power/volume (E=8%) was adequate for the aimed application and, thus, the expression N2=N1.(D1/D2) with its exponent of the relation between the diameters equal to 0,67 is suitable for the purpose of this dissertation. Once the actual value of N2 is determined by visual observation, it is not possible to get very accurate results. This way, a generic scale-up expression is proposed: N2=N1.(D1/D2) with its exponent of the relation between the diameters equal to 0,75. On the other hand, the ratio P/V may provide a more objective criterium for scale-up, because the three sort of impellers used in this study yielded E less than 10% when the power/volume method was applied for the purpose of scale-up.

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No. of bitstreams: 1 perez_cl_me_sjrp.pdf: 6948213 bytes, checksum: 88316394d4ffc78684a65d0a022b2c93 (MD5) Previous issue date: 2017-03-03 / Conselho Nacional de Desenvolvimento Científico e Tecnológico (CNPq) / Esta dissertação apresenta um estudo sobre a ampliação de escala de biorreatores de leito empacotado para produção de celulases e hemicelulases por fermentação em estado sólido (FES) empregando o fungo termofílico Myceliophthora thermophila I-1D3b e substrato composto por bagaço de cana de açúcar e farelo de trigo. As etapas de desenvolvimento do projeto consistiram em ensaios em biorreator de diâmetro interno e altura iguais a 7,62 e 10 centímetros, de modo que foram realizados ensaios variando tamanho das partículas de bagaço de cana, densidade bulk do leito, taxas de aeração e modo de distribuição da vazão de ar. Com base nos resultados obtidos, observou-se que partículas de bagaço de tamanho reduzido fornecem bons rendimentos de atividades enzimáticas quando submetidas a altas taxas de aeração em leitos de elevada densidade. Partículas maiores forneceram melhores resultados para leitos de �bulk= 0,395 g/cm3 , bem como a utilização de vazão de ar determinada com base no número de Damköhler modificado igual a 1. Resultados obtidos em ensaios em biorreatores de 0,8 metros, com e sem distribuição de ar, mostraram que inserir ar ao longo do leito é uma estratégia que permite aeração eficiente ao longo do sistema fermentativo, sem que ocorra secagem excessiva do substrato. Atividades relativas de CMCase e xilanase atingiram cerca de 1,2 e 0,7, respectivamente. As etapas finais consistiram em fermentações realizadas em biorreator de diâmetro interno e altura iguais a 20 centímetros. Nessas condições, foram testadas duas formas de distribuição de ar ao longo do leito de quatro módulos fermentativos: utilizando um tubo interno perfurado no módulo central inserindo metade da vazão total, e a outra metade inserida pelo inferior do leito e utilizando um tubo interno central, com quatro orifícios por módulo para espalhamento da vazão. Em termos de produção de celulase, o tubo no módulo central se mostrou a melhor alternativa para o aumento de escala, chegando a apresentar 0,8 de atividades enzimáticas relativas de CMCase, e em termos de atividades relativas de xilanase, a melhor opção foi o tubo interno longitudinal, apresentando valores de 0,55. Diante do exposto, o número de Damköhler modificado é interessante do ponto de vista de aumento de escala, no entanto é preciso ainda entender o mecanismo de atividade respiratória dos microrganismos para que os conceitos possam ser aplicados em sinergia, podendo-se assim esperar bom desempenho do processo em escala industrial. / This work presents a study of scale–up packed bed bioreactors for the production of cellulases and hemicellulases by solid-state fermentation (SSF) using the thermophilic fungus Myceliophthora thermophila I-1D3b and substrate composed by sugar cane bagasse and wheat bran. The development phases of the project consist in tests using bioreactors composed by internal diameter and height equal to 7.62 and 10 centimeters, respectively, so that the assays vary the size of the sugar cane bagasse particles, the bulk density, the airflow rate and how’s distributed along the bed. Based on the results obtained, it was defined that the particles of small size provide good results of enzymatic activity yields when submitted to high aeration rates in high bulk density beds. When testing normal size sugarcane bagasse particles, the best results were obtained for the beds with �bulk= 0,395 g/cm3 as well as airflow rate based on the modified Damköhler number equal to 1. Results obtained in tests in 0,8 meter height bioreactors, with and without airflow distribution, show that inserting air in different bed heights is a strategy to ensure efficient aeration throughout the fermentation system without excessive drying of the substrate. Activities related to CMCase and xylanase reached about 1.2 and 0.7, respectively. The final stages consisted in perform fermentation assays in a bioreactor of internal diameter and height equal to 20 centimeters. Under these conditions, two forms of long-term distribution were tested: using an internal ring to insert half of the total flow, together with the other half inserted in the lower part of the bed and using a central internal pipe with 4 holes per module for airflow distribution. In terms of cellulase production, the internal ring showed a better alternative for scaling-up, reaching a valeu of 0.8 CMCase relative enzymatic activities, and with respect to xylanase relative enzymatic activities, the best option was the central pipe, presenting values of 0,55. On the above, the modified Damköhler number is interesting when it refers to scale-up, although it’s necessary to understand the mechanism of respiratory activity of the microorganisms so that the concepts can be applied in synergy, and it can be expected good process performance in industrial scale. / CNPq: 132957/2016-7

No presente trabalho, dados de ampliacao de escala, de um processo de pre-tratamento alcalino em escala laboratorial (2L) para escala piloto (350L) foram avaliados. Os experimentos realizados previamente em escala laboratorial apontaram duas condições potenciais para a ampliacao de escala, a saber: Ensaio 5 (130°C, 30 min, 1,5% m/v NaOH, 0,15% m/m antraquinona) apresentando a maior conversao enzimatica da polpa obtida (64,5%) e Ensaio 7 (170°C, 1,5 % m/v NaOH, 30 min, 0,15% m/m antraquinona) com a maior solubilizacao de lignina (81,0 %). Os experimentos em escala piloto foram realizados nas condicoes apontadas, com e sem a adicao de antraquinona. A reprodutibilidade dos dados em escala piloto foi satisfatoria, considerando o sistema de aquecimento e agitacao mais eficientes do reator piloto em relacao ao reator usado no laboratorio. O uso da antraquinona diminuiu a solubilizacao de carboidratos durante o pretratamento (evitando 67% de solubilizacao quando comparado a reacao sem antraquinona, a 130°C), mas interferiu negativamente na etapa subsequente de hidrolise, principalmente na reacao a 170°C. Dentre as condicoes testadas, o ensaio 5Pil/AQ (130°C, 30 min, 1,5% NaOH e 0,15% m/m antraquinona) foi eleito como a melhor condicao de pre-tratamento, com maior rendimento em carboidratos apos a hidrolise enzimatica, sendo possivel obter (extrapolando os resultados) 290 kg de glicose e 98 kg de xilose a partir de uma tonelada de bagaco (base seca). Para a obtencao de etanol a partir desse hidrolisado, foram realizadas fermentacoes com tres diferentes leveduras - S. cerevisiae CAT-1, S. stipitis NRRL Y-7124 e S. passalidarum NRRL Y-27907. O melhor resultado foi apresentado para fermentacao em batelada alimentada aplicando reciclo de celulas utilizando a levedura S. passalidarum, produzindo 23,3 g/L de etanol (97 % do teorico) com produtividade de 0,90 g/L.h em 24 h de fermentacao no terceiro reciclo. O processo de pre-tratamento alcalino gera, alem da polpa rica em carboidratos, um hidrolisado rico em lignina. A lignina foi precipitada desse hidrolisado apos cada pre-tratamento realizado e caracterizada, apresentando poder calorifico entre 22,8 e 25,3 MJ/kg. / In this study, data scale up for an alkaline pretreatment process from lab to pilot scale was evaluated. Lab scale experiments indicated two potential conditions for the scale-up, namely: 130°C, 30 min, 1.5% w/v NaOH, 0.15% w/w anthraquinone , presenting the highest enzymatic conversion (64.5%); and 170°C, 30 min, 1.5% w/v NaOH, 0.15% w/w anthraquinone with the highest lignin solubilization (81.0 %). The experiments were performed on pilot scale under the aforementioned conditions, with and without anthraquinone. Data reproducibility on pilot scale was satisfactory considering the more efficient heating and stirring reactor system when compared to the reactor in lab scale. Anthraquinone decreases the solubilization of carbohydrates during pretreatment (avoiding 67% solubilization compared to the reaction without anthraquinone, at 130°C), but interferes negatively in the subsequent hydrolysis step, mostely at 170°C. Among the conditions tested, the test performed at 130°C, 30 min, 1.5% w/v NaOH and with 0.15% w/w anthraquinone was chosen as the best pretreatment condition, with the highest carbohydrate conversion after enzymatic hydrolysis, allowing 290 kg of glucose and 98 kg of xylose per a dry base ton of bagasse. In order to produce ethanol from this hydrolyzate, fermentations with three different yeasts were performed - S. cerevisiae CAT-1, S. stipites NRRL Y-7124, S. passalidarum NRRL Y-27907. Fed-batch fermentation with S. passalidarum cell recycling provided the best result, yielding 23.3 g/L ethanol, 97 % (theoretical yield) with 0.90 g/L.h productivity within 24 h of fermentation. The alkaline pretreatment process generates, besides the pulp rich in carbohydrates, a lignin-rich hydrolyzate. Lignin was precipitated from the hydrolyzate obtained after each pretreatment carried out and characterized, presenting heating values between 22.8 and 25.3 MJ/kg.