Submitted by Neusa Fagundes (neusa.fagundes@unioeste.br) on 2017-09-04T18:13:04Z No. of bitstreams: 1 Tamiris_Tonello2017.pdf: 1063307 bytes, checksum: d80fc677c2b209daeed59666a3b6e67a (MD5) / Made available in DSpace on 2017-09-04T18:13:04Z (GMT). No. of bitstreams: 1 Tamiris_Tonello2017.pdf: 1063307 bytes, checksum: d80fc677c2b209daeed59666a3b6e67a (MD5) Previous issue date: 2017-03-06 / Coordenação de Aperfeiçoamento de Pessoal de Nível Superior - CAPES / Energy demand has been met, for the most part, by non-renewable sources of energy, mainly from fossil fuels. These fuels tend to become extinct, so that, in order to guarantee economic, social, and ecological progress,it is necessary to look for renewable alternatives for the generation of energy. Bio-hydrogen production resulting from the biological method stands out due to the possibility of its obtaining from residue. Therefore, this work has the objective of evaluating the efficiency of anaerobic sequential batch reactor with immobilized biomass (AnSBBR) for the production of bio-hydrogen from cassava starch wastewater (CSW). The AnSBBR used in the tests presents mechanical agitation system and total and useful volumes of 6.0 and 4.3 L, respectively. The reactor was kept in a controlled temperature chamber (30 °C). Four experimental conditions (I, II, III, and IV) were carried out in a fed batch with organic volumetric loads (9.0, 13.5, 18.0, and 18.0 g-total sugars L-1d-1) for cycle durations of 4; 4; 3; and 2 h, respectively.Conditions I, II, and IV were inoculated with sludge from an anaerobic reactor from CSW, and condition III was with auto-fermented inoculum. It was found that the inoculum from the anaerobic reactor of the cassava starch effluent influenced the production of biogas in AnSBBR reactors. Condition II showed total sugar conversion of 84%, hydrogen molar productivity of 35.8 mLH2 m-3d-1 and hydrogen yield related to total sugar applied and removed of 2.42 and 4.6 molH2 Kg total sugars-1, respectively. In condition III (18 g-total sugars L-1d-1 and TDH of 3 h) with auto-fermented inoculum, there was no hydrogen production; however, it presented 98.47% of total sugar conversion throughout the operation. As for the intermediate products, there was an increase of acetic, butyric, and propionic acids in the reactor. However, the lactic acid did not increase, probably due to consumption by microorganisms, except in condition IV. / A demanda energética vem sendo atendida, em sua maior parte, por fontes de energia não renováveis advindas, principalmente, de combustíveis fósseis. Esses combustíveis tendem a se extinguir, de forma que se faz necessário, para garantir os avanços econômico, social e ecológico, buscar alternativas renováveis para a geração de energia.A produção de bio-hidrogênio, resultante do método biológico, se mostra de interesse pela possibilidade da sua obtenção a partir de resíduos.Diante disso, esse trabalho teve por objetivo avaliar a influência da carga orgânica na produção de bio-hidrogênio, a partir de água residuária de fecularia de mandioca (ARF) em reator anaeróbio operado em bateladas sequenciais com biomassa imobilizada (AnSBBR). O AnSBBR utilizado nos ensaios apresenta sistema de agitação mecânica e volume total e útil de 6,0 e 4,3L, respectivamente. O reator foi mantido em câmara com temperatura controlada (30 °C). Foram realizadas quatro condições experimentais (I, II, III e IV) em batelada alimentada com cargas orgânicas volumétricas de 9,0; 13,5; 18,0 e 18,0 g-carboidratos totais.L-1d-1), nos tempos de ciclo de 4; 4; 3 e 2 h, respectivamente. As condições I, II e IV foram inoculadas com lodo de um reator anaeróbio tratado termicamente, e a condição III com inóculo obtido por autofermentação da ARF. Concluiu-se que o inóculo proveniente do reator anaeróbio influenciou na produção de biogás em reatores AnSBBR. A condição II apresentou a conversão de açúcar total de 84%, a produtividade molar de hidrogênio de 35,8 molH2 m-3d-1 e o rendimento de hidrogênio em relação ao açúcar total aplicado e removido de 2,42 e 4,6 molH2 Kg-carboidratos totais-1, respectivamente. Na condição III (18 g-carboidratos totais L-1d-1e TDH de 3 h) com inóculo autofermentado não houve produção de hidrogênio; no entanto, houve conversão de açúcar total de 98,47% ao longo da operação. Quanto aos produtos intermediários, ocorreu aumento dos ácidos acético, butírico e propiônico no reator. Todavia, o ácido lático não aumentou, provavelmente devido ao consumo pelos micro-organismos, exceto na condição IV.

Thesis (MScEng)--Stellenbosch University, 2012 / ENGLISH ABSTRACT: Through many years of research, a number of production schemes have been developed for converting lignocellulosic biomass into transport fuels. These technologies have been assessed through a number of techno-economic studies for application in a particular context in terms of the technical and economic feasibility. However, previous studies using these methods have tended to lack vigour in various aspects. Either the energy efficiency of the processes were not maximised through adequate heat integration, or a competing technology which existed was not considered. From an economic perspective, the financial models would often lack the vigour to account for the risk and uncertainty that is inherent in the market prices of the commodities. This phenomenon is especially relevant for the biofuel industry that faces the full fledge of uncertainties experienced by the agricultural sector and the energy sector. Furthermore, from an environmental perspective, the techno-economic studies had often ignored the environmental impacts that are associated with biofuel production. Thus, a comparative study could have favoured an option due to its economic feasibility, while it could have had serious environmental consequences. The aim of this study was to address these issues in a South African context, where biofuels could be produced from sugarcane bagasse. The first step would be to modify an existing simulation model for a bioethanol scenario that operates with a Separate Hydrolysis and Fermentation (SHF process) configuration into a second processing scenario that operates with a Simultaneous Saccharification and Fermentation (SSF process) configuration using reliable experimental data. The second step was to ensure that the maximum energy efficiency of each scenario was realised by carrying out pinch point analysis as a heat integration step. In contrast to these biological models is the thermochemical model that converts bagasse to gasoline and diesel via gasification, Fischer-Tropsch synthesis and refining (GFT process). While there were no significant advances in technology concerning this type of process, the energy efficiency was to be maximised with pinch point analysis. The GFT process obtained the highest energy efficiency of 50.6%. Without the affects of pinch point technology, the efficiency dropped to 46%, which thus emphasises the importance of heat integration. The SSF had an efficiency of 42.8%, which was superior to that of the SHF at 39.3%. This resulted from a higher conversion of biomass to ethanol in the SSF scenario. Comparing the SHF model to an identical model found in literature that did not have pinch point retrofits, this study showed lower efficiency. This arose because the previous study did not account for the energy demands of the cold utility systems such as the cooling tower operation, which has been shown in this study to account for 40% of the electrical energy needs. The economic viability of all three processes was assessed with Monte Carlo Simulations to account for the risks that the fluctuations in commodity prices and financial indices pose. This was accomplished by projecting the fluctuations of these parameters from samples of a historical database that has been transformed into a probability distribution function. The consequences were measured in terms of the Net Present Value (NPV) and Internal Rate of Return (IRR) for a large number of simulations. The results of these variables were aggregated and were then assessed by testing the probability that the NPV<0, and that the IRR recedes below the interest rate of 12.64%. The investment was thus deemed unfeasible if these probabilities were greater than 20%. Both biological models were deemed profitable in terms of this standard. The probabilities were 13% for the SSF and 14% for the SHF. The GFT process however was deemed completely unfeasible because the probability that the NPV<0 was 78%. Given that the GFT process had the highest energy efficiency, this result arises mainly because the capital investment of 140,000USD/MWHHV of biomass energy input is to enormous for any payback to be expected. The environmental footprint of each process was measured using Life Cycle Assessments (LCAs). LCAs are a scientifically intricate way of quantifying and qualifying the effects of a product or process within a specified boundary. The impacts are assessed on a range of environmental issues, such as Global Warming, Acidification, Eutrophication and Human toxicity. Furthermore, if the project under concern has multiple output products, then the impacts are distributed between the output products in proportion to the revenue that each generates. The impacts were either relative to the flow of feedstock, which was 600MW of bagasse, or to the functional unit, which was the amount of fuel required to power a standard vehicle for a distance of 1 kilometre. In either case, the GFT scenario was the least burdening on the environmental. This was expected because the GFT process had the highest energy efficiency and the process itself lacked the use of processing chemicals. Relative to the feedstock flow, the SSF was the most environmentally burdening scenario due to the intensive use of processing chemicals. Relative to the functional unit, the SHF was the most severe due to its low energy efficiency. Thus, the following conclusions were drawn from the study:  The GFT is the most energy and environmentally efficient process, but it showed no sign of economic feasibility. iv  There is no significant difference in the economic and environmental evaluation of the SSF and SHF process, even though the SSF is considered to be a newer and more efficient process. The major cause of this is because the setup of the SSF model was not optimised. / AFRIKAANSE OPSOMMING: Deur baie jare van navorsing is ‘n aantal produksie-skemas vir die omskakeling van lignosellulose biomassa na vloeibarebrandstof ontwikkel. Hierdie tegnologië is geassesseer ten opsigte van die tegniese en ekonomiese haalbaarheid deur middel van tegno-ekonomiese studies in bepaalde tekste. Tog het hierdie vorige studies besliste beperkings gehad. Of die energie-doeltreffendheid van die proses is nie gemaksimeer deur voldoende hitte-integrasie nie, of 'n mededingende tegnologie wat bestaan is nie oorweeg nie. Vanuit 'n ekonomiese perspektief, was die finansiële modelle dikwels nie die omvattend genoeg om rekening te hou met die risiko en onsekerheid wat inherent is in die markpryse van die kommoditeite nie. Hierdie verskynsel is veral relevant vir die biobrandstof bedryf wat die volle omvang van onsekerhede ervaar waaraan die landbousektor en die energiesektoronderhewig is. Verder het die tegno-ekonomiese studies dikwels die omgewingsimpakte wat verband hou met biobrandstofproduksie geïgnoreer. Dus kon ‘n opsie deur die ekonomiese haalbaarheid bevoordeel word, ten spyte van die ernstige omgewingsimpakte wat dit kon inhou. Die doel van hierdie studie was om hierdie kwessies aan te spreek in 'n Suid-Afrikaanse konteks, waar biobrandstof uit suikerriet bagasse geproduseer kan word. Die eerste stap was om 'n bestaande simulasiemodel vir 'n bio-scenario wat met Afsonderlike Hidroliese en Fermentasie (SHF proses) stappe werk, te modifiseer vir 'n tweede verwerking scenario wat met 'n gelyktydige Versuikering en Fermentasie (SSF proses) konfigurasie werk. Die verandering is gedoen deur die gebruik van betroubare eksperimentele data. Die tweede stap was om te verseker dat elke scenario die maksimum energie-doeltreffendheid het, deur 'n hitte-integrasie stap, wat gebruik maak van “pinch-point” analise. In teenstelling met hierdie biologiese modelle, is daar die thermochemiese roete waar petrol en diesel van bagasse vervaardig word via vergassing, Fischer-Tropsch-sintese en rafinering (GFT proses). Daar was geen betekenisvolle vooruitgang in tegnologie vir hierdie proses nie, maar die energie-doeltreffendheid is gemaksimeer word deur energie-integrasie. Die GFT proses toon die hoogste energie-doeltreffendheid van 50,6%. Sonder die invloed van energie-integrasie het die doeltreffendheid gedaal tot 46%, wat dus die belangrikheid van hitte-integrasie beklemtoon. Die SSF het 'n effektiwiteit van 42,8% gehad, wat beter was as dié 39,3% van die SHF opsie. Hierdie hoër effektiwiteit wasas gevolg van die hoër omskakeling van biomassa na etanol in die SSF scenario. Die energie doeltreffendheid vir die SHF-model was laer as met 'n identiese model (sonder energie-integrasie) wat in die literatuur gevind wat is. Dit het ontstaan omdat die vorige studie nie 'n volledig voorsiening gemaak het met die energie-eise van die verkillingstelselsnie, wat tot 40% van die elektriese energie behoeftes kan uitmaak. Die ekonomiese lewensvatbaarheid van al drie prosesse is bepaal met Monte Carlo simulasies om die risiko's wat die fluktuasies in kommoditeitspryse en finansiële indekse inhou, in berekening te bring. Hierdie is bereik deur die projeksie van die fluktuasies van hierdie parameters aan die hand van 'n historiese databasis wat omskep is in 'n waarskynlikheid verspreiding funksie. Die gevolge is gemeet in terme van die netto huidige waarde (NHW) en Interne Opbrengskoers (IOK) vir 'n groot aantal simulasies. Die resultate van hierdie veranderlikes is saamgevoeg en daarna, deur die toets van die waarskynlikheid dat die NPV <0, en dat die IRR laer as die rentekoers van 12,64% daal, beoordeel. Die belegging is dus nie realiseerbaar geag as die waarskynlikhede meer as 20% was nie. Beide biologieseprosesse kan as winsgewend beskou word in terme van bostaande norme. Die waarskynlikhede was 13% vir die SSF en 14% vir die SHF. Aangesien die NHW van die GFT-proses onder 0 met ‘n waarskynlikheid van 78% is, is die opsie as nie-winsgewend beskou. Gegewe dat die GFT-proses die hoogste energie-doeltreffendheid het, is die resultaat hoofsaaklik omdat die kapitale belegging van 140,000 USD / MWHHV-biomassa energie-inset te groot is, om enige terugbetaling te verwag. Die omgewingsvoetspoor van elke proses is bepaal deur die gebruik van Lewens Siklus Analises (“Life Cycle Assessments”) (LCAS). LCAS is 'n wetenskaplike metodeom die effek van ‘n produk of proses binne bepaalde grense beide kwalitatief en kwantitatief te bepaal. Die impakte word beoordeel vir 'n verskeidenheid van omgewingskwessies, soos aardverwarming, versuring, eutrofikasie en menslike toksisiteit. Voorts, indien die projek onder die saak verskeie afvoer produkte het, word die impakte tussen die afvoer produkte verdeel, in verhouding tot die inkomste wat elkeen genereer. Die impak was met of relatief tot die vloei van roumateriaal (600MW van bagasse), of tot die funksionele eenheid, wat die hoeveelheid van brandstof is om 'n standaard voertuig aan te dryf oor 'n afstand van 1 kilometer. In al die gevalle het die GFT scenario die laagste belading op die omgewing geplaas. Hierdie is te verwagte omdat die GFT proses die hoogste energie-doeltreffendheid het en die proses self nie enige addisionele chemikalieë vereis nie. Relatief tot die roumateriaal vloei, het die SSF die grootse belading op die omgewing geplaas as gevolg van die intensiewe gebruik van verwerkte chemikalieë. Relatief tot die funksionele eenheid, was die SHF die swakste as gevolg van sy lae energie-doeltreffendheid.

Made available in DSpace on 2017-05-12T14:46:46Z (GMT). No. of bitstreams: 1 Cristiane.pdf: 1676874 bytes, checksum: b32327481322325a528776559d52d690 (MD5) Previous issue date: 2012-12-12 / Attempting to associate waste treatment to the production of clean and renewable energy, the present research aimed to evaluate the biological production of hydrogen using wastewater from the manioc starch treatment industry, a liquid wastewater of high organic content, generated during the processes of extraction and purification of manioc starch. The experiment was carried out in two upflow fixed-bed anaerobic reactors. As support, bamboo stems and low density polyethylene scraps. Made with pexiglass, each reactor was built with 75 cm of height, with 2.96 L of useful volume for the reactor with bamboo support and 3.13 L for the one with Polyethylene support. The inoculum, collected in a pilot anaerobic reactor, received thermal pretreatment and was recirculated in the reactors for 48 h. Then, alimentation was initiated in a continuum manner. The system was operated with hydraulic detention time (TDH) of 4 and 3 h, at 36 °C and initial pH of 6.0. In the TDH of 4 h, 3 organic loading rates were applied (COV), of 28; 15 and 26 g.L-1.d-1; in the TDH of 3 h 4 COV were applied, of 35; 22; 22 and 27 g.L-1.d-1. The application of the COV did not follow any particular pattern due to the variability of the wastewater constitution. Hence, the effects of TDH, COV and the support mean on the production of hydrogen were evaluated, as well as the influence of bamboo and of low density polyethylene in the fixation and selection of microorganisms that produce hydrogen. Maximum hydrogen production in the reactor using bamboo was of 2.9 L.d-1 in TDH 4h and of 2.2 L.d-1 in the reactor using polyethylene in TDH of 3 h. Hydrogen percentage of 25% in biogas was reached in the reactor using bamboo and of 29% in the reactor using polyethylene. The yielding obtained was of 0.6 L H2.g-1sugar in the reactor using bamboo in TDH 4 h and of 0.8 L H2.g-1sugar in the reactor using polyethylene in TDH 3 h. In both reactors, the mean total sugar removal was of approximately 90%. / Buscando aliar o tratamento de resíduos à produção de energia limpa e renovável, o presente trabalho teve como objetivo avaliar a produção biológica de hidrogênio a partir da água residuária da indústria de fécula de mandioca, resíduo líquido de elevada carga orgânica, gerado durante os processos de extração e purificação do amido. O experimento foi realizado em dois reatores anaeróbios de leito fixo e fluxo ascendente. Como meio suporte foram utilizadas hastes de bambu e aparas de polietileno de baixa densidade. Confeccionados em pexiglass, cada reator foi construído com 75 cm de altura, o volume útil calculado foi de 2,96 L para o reator com suporte de bambu e 3,13 L para o reator com suporte de polietileno. O inóculo, coletado em um reator anaeróbio piloto, recebeu pré-tratamento térmico e foi recirculado nos reatores por 48 h. Em seguida, iniciou-se a alimentação em modo contínuo. O sistema foi operado com tempo de detenção hidráulica (TDH) de 4 e 3 h, a 36 °C e pH inicial 6,0. No TDH de 4 h foram aplicadas 3 cargas orgânicas volumétricas (COV) de 28; 15 e 26 g.L-1.d-1; no TDH de 3 h foram aplicadas 4 COV de 35; 22; 22 e 27 g.L-1.d-1. A aplicação das COV não seguiu a um padrão devido à variabilidade na constituição da água residuária. Dessa forma, foram avaliados os efeitos do TDH, da COV e do suporte sobre a produção fermentativa de hidrogênio e também a influência do bambu e do polietileno de baixa densidade na fixação e seleção dos micro-organismos produtores de hidrogênio. A produção máxima de hidrogênio no reator com bambu foi de 2,9 L.d-1 em TDH 4 h e de 2,2 L.d-1 no reator com polietileno em TDH de 3 h. Foram alcançados percentuais de hidrogênio no biogás de 25% no reator com bambu e 29% o reator com polietileno. O rendimento obtido foi de 0,6 L H2.g-1açúcar no reator com bambu em TDH 4 h e 0,8 L H2.g-1açúcar no reator com polietileno em TDH 3 h. Em ambos os reatores a degradação média de açúcares totais foi de aproximadamente 90%.

Made available in DSpace on 2017-07-10T19:23:35Z (GMT). No. of bitstreams: 1 Cristiane.pdf: 1676874 bytes, checksum: b32327481322325a528776559d52d690 (MD5) Previous issue date: 2012-12-12 / Attempting to associate waste treatment to the production of clean and renewable energy, the present research aimed to evaluate the biological production of hydrogen using wastewater from the manioc starch treatment industry, a liquid wastewater of high organic content, generated during the processes of extraction and purification of manioc starch. The experiment was carried out in two upflow fixed-bed anaerobic reactors. As support, bamboo stems and low density polyethylene scraps. Made with pexiglass, each reactor was built with 75 cm of height, with 2.96 L of useful volume for the reactor with bamboo support and 3.13 L for the one with Polyethylene support. The inoculum, collected in a pilot anaerobic reactor, received thermal pretreatment and was recirculated in the reactors for 48 h. Then, alimentation was initiated in a continuum manner. The system was operated with hydraulic detention time (TDH) of 4 and 3 h, at 36 °C and initial pH of 6.0. In the TDH of 4 h, 3 organic loading rates were applied (COV), of 28; 15 and 26 g.L-1.d-1; in the TDH of 3 h 4 COV were applied, of 35; 22; 22 and 27 g.L-1.d-1. The application of the COV did not follow any particular pattern due to the variability of the wastewater constitution. Hence, the effects of TDH, COV and the support mean on the production of hydrogen were evaluated, as well as the influence of bamboo and of low density polyethylene in the fixation and selection of microorganisms that produce hydrogen. Maximum hydrogen production in the reactor using bamboo was of 2.9 L.d-1 in TDH 4h and of 2.2 L.d-1 in the reactor using polyethylene in TDH of 3 h. Hydrogen percentage of 25% in biogas was reached in the reactor using bamboo and of 29% in the reactor using polyethylene. The yielding obtained was of 0.6 L H2.g-1sugar in the reactor using bamboo in TDH 4 h and of 0.8 L H2.g-1sugar in the reactor using polyethylene in TDH 3 h. In both reactors, the mean total sugar removal was of approximately 90%. / Buscando aliar o tratamento de resíduos à produção de energia limpa e renovável, o presente trabalho teve como objetivo avaliar a produção biológica de hidrogênio a partir da água residuária da indústria de fécula de mandioca, resíduo líquido de elevada carga orgânica, gerado durante os processos de extração e purificação do amido. O experimento foi realizado em dois reatores anaeróbios de leito fixo e fluxo ascendente. Como meio suporte foram utilizadas hastes de bambu e aparas de polietileno de baixa densidade. Confeccionados em pexiglass, cada reator foi construído com 75 cm de altura, o volume útil calculado foi de 2,96 L para o reator com suporte de bambu e 3,13 L para o reator com suporte de polietileno. O inóculo, coletado em um reator anaeróbio piloto, recebeu pré-tratamento térmico e foi recirculado nos reatores por 48 h. Em seguida, iniciou-se a alimentação em modo contínuo. O sistema foi operado com tempo de detenção hidráulica (TDH) de 4 e 3 h, a 36 °C e pH inicial 6,0. No TDH de 4 h foram aplicadas 3 cargas orgânicas volumétricas (COV) de 28; 15 e 26 g.L-1.d-1; no TDH de 3 h foram aplicadas 4 COV de 35; 22; 22 e 27 g.L-1.d-1. A aplicação das COV não seguiu a um padrão devido à variabilidade na constituição da água residuária. Dessa forma, foram avaliados os efeitos do TDH, da COV e do suporte sobre a produção fermentativa de hidrogênio e também a influência do bambu e do polietileno de baixa densidade na fixação e seleção dos micro-organismos produtores de hidrogênio. A produção máxima de hidrogênio no reator com bambu foi de 2,9 L.d-1 em TDH 4 h e de 2,2 L.d-1 no reator com polietileno em TDH de 3 h. Foram alcançados percentuais de hidrogênio no biogás de 25% no reator com bambu e 29% o reator com polietileno. O rendimento obtido foi de 0,6 L H2.g-1açúcar no reator com bambu em TDH 4 h e 0,8 L H2.g-1açúcar no reator com polietileno em TDH 3 h. Em ambos os reatores a degradação média de açúcares totais foi de aproximadamente 90%.

Orientadores: Aline Carvalho da Costa, José Geraldo da Cruz Pradella / Dissertação (mestrado) - Universidade Estadual de Campinas, Faculdade de Engenharia Química / Made available in DSpace on 2018-08-25T15:37:13Z (GMT). No. of bitstreams: 1 Gelain_Lucas_M.pdf: 1331794 bytes, checksum: 116fec6e0222b23e24403c80d7c5c885 (MD5) Previous issue date: 2014 / Resumo: Modelos matemáticos são necessários para o desenvolvimento de processos, pois permitem o entendimento dos fenômenos envolvidos e podem ser usados para scale-up e otimização das condições de operação. O objetivo deste trabalho foi propor um modelo matemático para descrever a cinética de crescimento celular, consumo de substrato e produção de enzimas utilizando o Trichoderma harzianum em diferentes concentrações de bagaço de cana-de-açúcar (fonte de carbono). Além disso, realizaram-se testes utilizando uma sonda de capacitância para estimação on-line da concentração de células no meio. As concentrações de bagaço de cana-de-açúcar empregadas foram de: 5; 10; 20; 30; e 40 g L-1, onde a concentração 10 g L-1 foi utilizada para validar o modelo e as demais concentrações para a estimação dos parâmetros. As enzimas analisadas foram: celulase (FPase), beta-glicosidase e xilanase. A estimação da concentração de células utilizando a sonda de capacitância mostrou ser uma alternativa interessante, indicando que há boa correlação entre o sinal da sonda e a concentração de células em meio solúvel. No entanto, o meio insolúvel (contendo bagaço de cana-de-açúcar) causou interferências, impedindo seu uso para uma análise quantitativa. Modelos matemáticos foram construídos para descrever as cinco variáveis de estado (concentrações de células e substrato, assim como atividades de celulase (FPase), beta-glicosidase e xilanase). Os modelos parecem representar bem a cinética com um bom ajuste para a maioria dos ensaios. Alterações nos modelos e novos ensaios com concentrações diferentes de substrato ainda precisam ser realizados com a finalidade de melhorar o ajuste e aumentar confiabilidade dos modelos / Abstract: Mathematical models are necessary to processes development, because they enable the understanding of the involved phenomena and can be used to scale-up and optimization of operation conditions. The aim of this work was to propose a mathematical model to describe the kinetics of the cellular growth, substrate consumption and enzyme production using Trichoderma harzianum in different sugar cane bagasse concentrations (carbon source). Besides, tests using a capacitance probe to on-line cellular estimation were performed. The sugar cane bagasse concentrations employed were: 5; 10; 20; 30; e 40 g L-1. The 10 g L-1 concentration was used to validate the model and the others to parameters estimation. The enzymes analyzed were cellulase; beta-glucosidase; and xylanase. The estimation of cellular concentration using the capacitance probe is an interesting alternative indicating good correlation between the sign of the probe and the cells in soluble medium. However, the insoluble medium (with sugar cane bagasse) caused interferences that prevented quantitative analysis. Mathematical models were built to describe the five dependents variables (concentrations of cells and substrate, as well as activities of cellulase (FPase), beta-glucosidase and xylanase). The models seem to represent well the kinetics with a good fit for the majority of the assays. Alterations in the models and new assays with different substrate concentration are needed to provide better fit and increase the model trustworthiness / Mestrado / Engenharia Química / Mestre em Engenharia Química

Thesis (MScEng (Process Engineering))--Stellenbosch University, 2010. / ENGLISH ABSTRACT: Recently, improved technologies have been developed for the biobutanol fermentation process: higher butanol concentrations and productivities are achieved during fermentation, and separation and purification techniques are less energy intensive. This may result in an economically viable process when compared to the petrochemical pathway for butanol production. The objective of this study is to develop process models to compare different possible process designs for biobutanol production from sugarcane molasses. Some of the best improved strains, which include Clostridium acetobutylicum PCSIR-10 and Clostridium beijerinckii BA101, produce total solvent concentrations of up to 24 g/L. Among the novel technologies for fermentation and downstream processing, fedbatch fermentation with in situ product recovery by gas-stripping, followed by either liquid-liquid extraction or adsorption, appears to be the most promising techniques for current industrial application. Incorporating these technologies into a biorefinery concept will contribute toward the development of an economically viable process. In this study three process routes are developed. The first two process routes incorporate well established industrial technologies: Process Route 1 consist of batch fermentation and steam stripping distillation, while in Process Route 2, some of the distillation columns is replaced with a liquid-liquid extraction column. The third process route incorporates fed-batch fermentation and gas-stripping, an unproven technology on industrial scale. Process modelling in ASPEN PLUS® and economic analyses in ASPEN Icarus® are performed to determine the economic feasibility of these biobutanol production process designs. Process Route 3 proved to be the only profitable design in current economic conditions. For the latter process, the first order estimate of the total project capital cost is $187 345 000.00 (IRR: 35.96%). Improved fermentation strains currently available are not sufficient to attain a profitable process design without implementation of advanced processing techniques. Gas stripping is shown to be the single most effective process step (of those evaluated in this study) which can be employed on an industrial scale to improve process economics of biobutanol production. / AFRIKAANSE OPSOMMING: Onlangse verbeteringe in die tegnologie vir die vervaardiging van butanol via die fermentasie roete het tot gevolg dat: hoër butanol konsentrasies en produktiwiteit verkry kan word tydens die fermentasie proses, en energie verbruik tydens skeiding-en suiweringsprosesse laer is. Hierdie verbeteringe kan daartoe lei dat biobutanol op ʼn ekonomiese vlak kan kompeteer met die petrochemiese vervaardigings proses vir butanol. Die doelwit van die studie is om proses modelle te ontwikkel waarmee verskillende proses ontwerpe vir die vervaardiging van biobutanol vanaf suikerriet melasse vergelyk kan word. Verbeterde fermentasie organismes, wat insluit Clostridium acetobutylicum PCSIR-10 en Clostridium beijerinckii BA101, het die vermoë om ABE konsentrasies so hoog as 24 g/L te produseer. Wat nuwe tegnologie vir fermentasie en skeidingprosesse behels, wil dit voorkom of wisselvoer fermentasie met gelyktydige verwydering van produkte deur gasstroping, gevolg deur of vloeistof-vloeistof ekstraksie of adsorpsie, van die mees belowende tegnieke is om tans in die nywerheid te implementeer. Deur hierdie tegnologie in ʼn bioraffinadery konsep te inkorporeer sal bydra tot die ontwikkeling van ʼn ekonomies lewensvatbare proses. Drie prosesserings roetes word in die studie ontwikkel. Die eerste twee maak gebruik van goed gevestigde industriële tegnologie: Proses Roete 1 implementeer enkellading fermentasie en stoom stroping distillasie, terwyl in Proses Roete 2 van die distilasiekolomme vervang word met ʼn vloeistof-vloeistof ekstraksiekolom. Die derde proses roete maak gebruik van wisselvoer fermentasie met gelyktydige verwydering van produkte deur gas stroping. Die tegnologie is nog nie in die nywerheid bewys of gevestig nie. Om die ekonomiese uitvoerbaarheid van die proses ontwerpe te bepaal word proses modellering uitgevoer in ASPEN PLUS® en ekonomiese analises in ASPEN Icarus® gedoen. Proses Roete 3 is die enigste ontwerp wat winsgewend is in huidige ekonomiese toestande. Die eerste orde koste beraming van die laasgenoemde projek se totale kapitale koste is $187 345 000.00 (opbrengskoers: 35.96%). Die verbeterde fermentasie organismes wat tans beskikbaar is, is nie voldoende om ʼn proses winsgewend te maak nie; gevorderde proses tegnologie moet geïmplementeer word. Gasstroping is bewys as die mees effektiewe proses stap (getoets in die studie) wat op industriële skaal geïmplementeer kan word om die winsgewendheid van die biobutanol proses te verbeter. / Centre for Renewable and Sustainable Energy Studies

Estudou-se a cinética do processo de produção de bebidas lácteas por fermentação mantida a 42°C em sistema descontínuo. As bebidas foram preparadas a partir de uma base láctea de leite desnatado e soro de queijo doce e com substituição parcial realizada com extrato solúvel de soja em pó, utilizando 2 culturas lácticas comerciais, representadas pela cultura tradicional, Streptococcus salivarius subsp. thermophilus e Lactobacillus delbrueckii subsp. bulgaricus e pela cultura contendo organismos probióticos, S. thermophilus, L. bulgaricus, Bifidobacterium e Lactobacillus acidophilus. O processo foi monitorado pelas análises de pH - uso de pHmetro digital (GEHAKA, PG1000) - , acidez (g ácido láctico/L) - titulação com solução de NaOH 0,1N, usando como indicador a solução de fenolftaleína 1,0% - e pelas contagens microbiológicas, sendo realizadas do início da fermentação (t=0) até o pH próximo a 4,6. Para a contagem de bactérias lácticas totais, lactobacilos, estreptococos e organismos probióticos foram empregados os meios Agar MRS, Agar MRS acidificado com 0,05% de HCl-L-cisteína, Agar M17 e Agar MRS adicionado de 0,3% de extrato de bile, respectivamente. As alíquotas, retiradas do processo fermentativo foram diluídas em água peptonada 0,1%. Inoculou-se 1mL da diluição em meio fundido e em seguida as placas foram homogeneizadas e submetidas à incubação em jarras herméticas, na temperatura de 42ºC, por 48 horas, utilizando-se um produtor de microaerofilia (Anaerobac - Probac do Brasil). As velocidades instantâneas de produção de ácido láctico (g/L/h) e de crescimento celular (UFC/L/h) foram obtidas a partir do Modelo de Sinclair e Cantero (1990). A bebida, produzida com substrato contendo somente base láctea e cultura tradicional (Trat.1), foi a que necessitou de maior tempo (3h30) para que o pH se aproximasse de 4,6, sendo que quando empregou-se cultura contendo organismos probióticos, (Trat. 3), o tempo necessário para atingir esse pH foi de 3h. Na substituição parcial de sólidos pelo extrato solúvel de soja, representado pelas bebidas obtidas pelos tratamentos 2 e 4, verificou-se a necessidade de 3h e 2h30min respectivamente, para o pH aproximar de 4,6. Em relação à acidez expressa em g ácido láctico/L, várias bebidas não atingiram o valor estabelecido pelo padrão de identidade de bebidas lácteas (BRASIL, 2005 a), variando entre todos os tratamentos. Percebeuse ainda que o tempo para atingir o valor máximo das velocidades instantâneas de crescimento das bactérias lácticas e estreptococos atingiram 3h, independente do substrato utilizado na fermentação, enquanto, empregando a cultura probiótica, a velocidade máxima de crescimento de bactérias lácticas (dX/dt) ocorreu em 2h no tratamento com base láctea (Trat. 3) e 1h na bebida com substituição parcial da base láctea (Trat. 4). As máximas velocidades instantâneas relativas às culturas de estreptococos nos tratamento 3 e 4 ocorreram em 3 e 1h respectivamente. Quanto aos dX/dt máximos referente ao crescimento de lactobacilos verificou-se a necessidade de 2h e 1h respectivamente, enquanto para os organismos probióticos foi de 2h, em substrato base láctea e 1h quando do emprego de substrato com substituição parcial da base láctea por extrato de soja. / It was studied the kinetics from production of milk drinks by fermentation maintained at 42 ° C in a batch system. The drinks were prepared from a base of skimmed milk and whey sweet cheese with a partial replacement performed with soluble extract of soybean powder, and the employment of 2 lactic commercial crops, represented by the traditional culture, containing Streptococcus salivarius subsp. thermophilus and Lactobacillus delbrueckii subsp. bulgaricus and the probiotic culture, containing S. thermophilus, L. bulgaricus, Bifidobacterium e Lactobacillus acidophilus. The process was monitored by the analysis of pH - digital pHmetro (GEHAKA, PG1000), acidity (g lactic acid / L) - titration with 0.1 N NaOH solution, using as an indicator of phenolphthalein solution 1.0%and the total counts of organisms. Being held at the beginning of fermentation (t = 0) until the pH near the pH 4.6. For lacitcal total count of bacteria, lactobacilli, streptococci and probiotic organisms were employed MRS Agar, Agar MRS acidified with 0.05% HCl-L-cysteine, M17 and Agar Agar MRS added of 0.3% of extract of bile, respectively. The aliquots withdrawn from the fermentation process were diluted in water peptone 0.1%. Inoculated up 1mL of dilution in means and then mixed up the plates that were then subjected to incubation in hermetic jars in temperature of 42°C for 48 hours using a producer of microaerophilic (Anaerobac - Probac do Brasil). The speeds of instant production of lactic acid (g/L/h) and cellular growth (CFU/L/h) were obtained from the model of Sinclair and Cantero (1990).The drink, produced with only basic substrate containing milk and traditional culture (Trat.1) was that needed more time (3:30) to the pH of 4.6 approaches, and that when the employment of culture containing probiotic organisms, even with substrate (Trat. 3), the time needed was 3h. When the partial replacement of the solid soluble extract of soybean, represented by drinks obtained by treatments 2 and 4, there is a need for 3 and 2:30 respectively, to bring the pH of 4.6. As the acidity in g lactic acid / L, it was found that several drinks not reached the value set by standard of identity for milk drinks (BRASIL, 2005 a) ranging from all treatments. It was noticed that the time to achieve the maximum speeds of instant speed of growth of lactic acid bacteria streptococci and reached its peak in 3h, independent of the substrate used in fermentation, while employing the probiotic culture, it was found that the maximum speed of growth of lactic acid bacteria occurred in 2h in treatment based milk (Trat. 3) and in 1h drink with a partial replacement of basic milk (Trat. 4). The maximum speeds instant on the cultures of Streptococci treatment in 3 and 4 occurred in 3 and 1 h respectively. For dX / dt maximum for the growth of lactobacilli there is a need to 1h and 2h respectively, while the bodies of probiotics was 2h, when the employment base substrate of milk and 1am when the employment of substrate with a partial replacement of the database by extract soya milk.

No description available.

Šiuo tyrimu buvo siekiama nustatyti koreliaciją tarp karvių didžiojo prieskrandžio turinio fermentacinių procesų aktyvumo rodiklių ir pieno produkcijos rodiklių. Taip pat - nustatyti karvių didžiojo prieskrandžio fermentacinių procesų rodiklių tarpusavio koreliaciją. Bandomosios LJ karvės (n=5) buvo tirtos ganykliniu ir tvartiniu laikotarpiais. Buvo ištirti šie didžiojo prieskrandžio fermentacijos rodikliai: pH, redukcinis bakterijų aktyvumas, gliukozės rūgimo reakcija, pirmuonių skaičius, lakiųjų riebalų rūgščių kiekis. Taip pat - pieno rodikliai: pieno kiekis, pieno riebalai, pieno baltymai, pieno laktozė, šlapalas. Koreliacijos koeficientai (rS) buvo apskaičiuoti pagal Spearman‘ą. Gauti rezultatai yra statistiškai nepatikimi, išskyrus, koreliaciją tarp didžiojo prieskrandžio pirmuonių ir pieno riebalų (rS = 0.9, p = 0,037) bei pirmuonių skaičiaus ir pieno baltymų (rS = 0.9, p = 0,037) tvartiniu laikotarpiu. Pastovią koreliaciją tvartiniu ir ganykliniu laikotarpiais išlaikė pirmuonių skaičius ir pieno kiekis (rS = –0,8 (p>0,05). Koreliacija, tarp redukcinio bakterijų aktyvumo ir pirmuonių skaičiaus, bei koreliacija, tarp lakiųjų riebalų rūgščių (LRR) ir pirmuonių skaičiaus, tiek tvartiniu ( atitinkamai rS = 0,872, p>0,05; rS = 0,1, p>0,05), tiek ganykliniu laikotarpiais (atitinkamai rS = 0,289, p>0,05; rS = 0,707; p>0,05), išliko teigiama. Neigiama koreliacija tvartiniu (rS = –0,205, p>0,05) ir ganykliniu (rS = –0,408, p>0,05) laikotarpiais išliko tarp redukcinio bakterijų... [toliau žr. visą tekstą] / This study was designed to determine a correlation between rumen fermentation process activity rates and milk production, also to establish a correlation between the rumen fermentation indicators. The study group was consisted of five LJ cows, which were tested during indoor and outdoor periods. In this study we have measured ruminal pH, bacterial activity reduction, glucose fermentation reaction, number of protozoa and volatile fatty acids also milk indicators such as milk fat, milk proteins, milk lactose, and milk urea. Correlation coefficients (rS) were calculated according to Spearman. The results are not statistically significant, except correlation results during the stable period between rumen protozoa count and milk fat (rS = 0.9, p = 0.037) also between number of protozoa and milk proteins (rS = 0.9, p = 0.037). A correlation constant between number of protozoa and quantity of milk (rs = -0.8, p < 0.05) was stable during both periods. During indoor and outdoor periods correlation between reduction activity of bacteria and number of protozoa, volatile fatty acids (VFA) and number of protozoa, (respectively, rS = 0.87, p<0.05, rS = 0 1, p> 0.05 and rS = 0.289, p> 0.05, rS = 0.707, p> 0.05) remained positive. During both periods negative correlation remained between reduction activity of bacteria and VFA (respectively rS = -0.205, p> 0.05, rS = -0.408, p <0.05).

Orientadores: Rubens Maciel Filho, Aline Carvalho da Costa / Dissertação (mestrado) - Universidade Estadual de Campinas, Faculdade de Engenharia Quimica / Made available in DSpace on 2018-08-07T06:46:12Z (GMT). No. of bitstreams: 1 Mantovaneli_IvanaCristinaCordeiro_M.pdf: 4744367 bytes, checksum: 648b4b28d0ad3fff1bfeda9851005fc1 (MD5) Previous issue date: 2005 / Resumo: A utilização do etanol como combustível tem muitas vantagens; ele tem competido economicamente com a gasolina e diversos outros combustíveis, substituindo-os em várias utilidades. Desta forma, existe um grande interesse em se otimizar todos os passos da produção de etanol. Apenas um conhecimento profundo da dinâmica do processo gera uma operação ótima, e este pode ser conseguido através de simulações realizadas usando um modelo preciso. Muitos modelos fenomenológicos foram desenvolvidos considerando condições industriais, mas estes só são válidos para condições específicas nas quais foram determinados, invalidando a predição do modelo em outras condições. Mudanças acontecem normalmente em uma unidade industrial e a re-estimação freqüente dos parâmetros do modelo é usualmente difícil e demorada. O objetivo deste trabalho é desenvolver um modelo híbrido neuronal para o processo de fermentação alcoólica usando balanços de massa combinados com redes neuronais do tipo Functional Link. Será implementado um esquema para atualização dos pesos da rede sempre que esta não descrever o comportamento dinâmico da planta. O modelo desenvolvido será usado para descrever um processo real no lugar dos modelos fenomenológicos existentes, já que estes têm sido capazes de descrever o processo apenas por curtos espaços de tempo / Abstract: The use of ethanol as a fuel has many advantages; it has economically competed with gasoline and others fuels, substituting them in various uses. Thus, there is a great interest in optimizing all the steps of ethanol production. Only a detailed knowledge of the process dynamics can lead to optimal operation and this can be achieved through simulation using an accurate model. Many phenomenological models were developed considering industrial fermentations, but they are only valid for specific conditions. Changes occur frequently in an industrial unity and frequent reestimation of model parameters is usually expensive and time consuming. The objective of this work is to develop a hybrid neural model for the alcoholic fermentation process using mass balances combined with Functional Link Neural Networks. A scheme to update network weights always that it does not describe plant behavior accurately is implemented. The developed model is used to describe an industrial process substituting the existing phenomenological models, since they have been able to describe the process only for short periods / Mestrado / Desenvolvimento de Processos Biotecnologicos / Mestre em Engenharia Química