The Piedmont System is a collection of equipment for efficiently removing the juice from sweet sorghum stalks for the production of ethanol. The concept is to separate the whole stalks into pith and rind-leaf fractions, pass only the pith fraction through a screw press, and thus achieve an improvement in juice expression efficiency and press capacity. The operation of three alternative harvesting/processing systems were modeled and compared using computer simulation to determine which system could produce sweet sorghum juice and deliver it to a central plant at the lowest cost per liter of potential ethanol produced. In addition, an energy analysis was done to determine the net energy gain. System A cut the sorghum stalks and hauled them to a crossroads site where they could be stored up to 30 days before juice expression. System B separated the pith and rind-leaf fractions in the field, and juice expression was accomplished at a nearby site. No storage was possible for System B. System C cut the stalks like System A, but then a mobile processor moved through the field to separate the pith and rind-leaf fractions. It was found that the cost of producing feedstock with System C ($0.87/L) was significantly higher than either System A ($0.56/L) or System B ($0.63/L). While the System A cost was slightly lower than that of System B, it is recommended that both Systems A and B should be studied further since small adjustments to the model could eliminate the advantage of System A over System B. Increases in whole-stalk yield and juice sugar level would lower the cost of all three systems by as much as 43%. As the price of energy rises, sweet sorghum is expected to gain an economic advantage over com as a feedstock for ethanol, because of its higher energy ratio. If the by-products are used to produce ethanol through cellulose conversion, the overall energy ratio for sweet sorghum was calculated to be 1.1 compared to 0.8 for corn. The energy ratio if only liquid fuels are considered was 7.9 for sweet sorghum compared to 4.5 for corn. / Ph. D.

Communities of different sizes in Saskatchewan seeking economic opportunities have shown interest in ethanol production because of the perceived benefits a region can capture from such a project. In spite of this interest and the perceived benefits, no information on the type and magnitude of economic impacts which would accrue to different sized communities existed. This study was undertaken to fill this information gap by establishing facts on the economic impacts various levels of communities could capture from ethanol-cattle production complexes. Since Saskatchewan communities operate in a hierarchical fashion and are classified into seven levels using central place theory, questions concerning economic development should be viewed in a regional hierarchical framework. A seven-region hierarchically-based interregional input-output model for the Saskatchewan economy was constructed using the Supply-Demand Pool (SDP) method in combination with the logical assumptions regarding trade patterns within the central place region. It was assumed that higher-level regions are surplus regions in goods produced by non-primary sectors, and hence ship excess supply to producers and final users in the dominated lower-level regions and outside of the province. On the other hand, it was assumed that the hinterland region dominates trade in goods in the primary sectors. The hinterland earned income by producing and supplying goods and services in the primary sectors to the higher-level regions and outside the province. The model consisted of 14 aggregated sectors seven household sectors, and allowed for net flows of labour income through commuting patterns of workers who resided in the seven regions. At the same time the consumption expenditures of residents in a particular region were adjusted for outshopping purchases. The estimated model was used to assess the economic impacts from both the construction and operation phase of an integrated ethanol-cattle production complex across six hierarchical regions. The major findings of this study were that, under both phases of the project, intraregional output and labor income impacts occurring in the high level regions were larger than those in the lower-level regions. Also, the higher-level regions experienced larger interregional impacts and had spillover coefficients of smaller magnitude compared to lower-level regions. The intraregional output and labor income impacts tended to decrease as one moves down the hierarchy from top to bottom regions. On the other hand, the spillovers or leakages were increasing as one moves down the hierarchy from higher-level regions to lower-level regions. The higher-level regions have more diversified economies and smaller leakages of income and spending than lower-level regions. On the other hand, lower-level regions experienced large income leakages through input purchases and consumer spending in neighbouring higher-level regions. The results indicate that lower-level regions will not benefit more than higher-level regions from the development of an integrated ethanol-cattle production complex. Thus, if the goal of public funding of ethanol projects is to maximize impacts in the project-region, then higher-level regions would be preferred to lower-level regions. This raises a concern that the opportunity of pursuing regional development through ethanol processing may not reach all those communities who need it the most, especially the smaller communities. On the other hand, if the objective of rural development is to solve the problems of rural communities, the policy-makers, could target lower-level regions specially those experiencing economic decline. It is important to mention that integrated ethanol-cattle production continues to enjoy subsidies from the governments. (Abstract shortened by UMI.)

Σε αυτή την μελέτη παρασκευάστηκαν ηλεκτρόδια Pt-RuO2-TiO2 και χαρακτηρίστηκαν με περίθλαση ακτίνων Χ (X-ray diffraction - XRD), φασματοσκοπία φωτοηλεκτρονίων από ακτίνες Χ (X-ray photoelectron spectroscopy - XPS), ηλεκτροχημικές τεχνικές και πειράματα ρόφησης-οξείδωσης μονοξειδίου του άνθρακα (CO stripping). Ερευνήθηκε η μείωση της περιεκτικότητας σε Pt και RuO2 χωρίς απώλειες της ηλεκτροκαταλυτικής ενεργότητας. Το TiO2 επιλέχθηκε λόγω της χημικής του σταθερότητας και του χαμηλού κόστους. Βρέθηκε ότι περιεκτικότητα σε TiO2 μέχρι 50% οδηγεί σε αύξηση της ηλεκτροχημικά ενεργής επιφάνειας (EAS) του ηλεκτροδίου. Η ηλεκτροχημικά ενεργή επιφάνεια (EAS) του ηλεκτροδίου Pt(25%)-RuO2(25%)-TiO2(50%) ήταν μεγαλύτερη του ηλεκτροδίου Pt(50%)-RuO2(50%), ενώ για περιεκτικότητα σε TiO2 μεγαλύτερη από 65% η EAS μειώνεται δραματικά. Το παραπάνω συμπέρασμα στηρίχθηκε σε μετρήσεις του φορτίου της αναγωγικής κορυφής των κυκλικών βολταμογραφημάτων και σε πειράματα ρόφησης-οξείδωσης του CO (CO stripping). Όλα τα δείγματα χρησιμοποιήθηκαν και ως άνοδοι κατά τη διάρκεια ηλεκτροχημικής οξείδωσης μεθανόλης, αιθανόλης και γλυκερόλης. Και στις τρεις περιπτώσεις το ηλεκτρόδιο Pt(25%)-RuO2(25%)-TiO2(50%) παρουσίασε τη μεγαλύτερη ηλεκτροκαταλυτική ενεργότητα. Η παρατηρούμενη αυξημένη απόδοση των ηλεκτροδίων που παρασκευάστηκαν αποδόθηκε στην αυξημένη διασπορά της Pt και του RuO2, στο σχηματισμό μικρότερων κρυσταλλιτών Pt και RuO2 με την πρόσθεση TiO2, καθώς επίσης και σε ηλεκτρονιακές αλληλεπιδράσεις μεταξύ των μετάλλων και του TiO2. / In this study Pt-RuO2-TiO2 electrodes were prepared and characterised by X-ray Diffraction (XRD), X-ray Photoelectron Spectroscopy (XPS), electrochemical techniques and CO stripping. The minimization of the Pt and RuO2 loading without electrocatalytic activity losses was explored. TiO2 was chosen due to its chemical stability and low cost. It was found that TiO2 loading up to 50% resulted in an increase of the Electrochemically Active Surface (EAS). The EAS of Pt(25%)-RuO2(25%)-TiO2(50%) was higher than that of Pt(50%)-RuO2(50%) while for TiO2 loadings higher than 50% the EAS diminished. The above conclusion has been confirmed by following the charge of the platinum reduction peak on cyclic voltammograms and by CO stripping experiments. All samples were used as anodes during electrochemical oxidation of methanol, ethanol and glycerol. In all cases the Pt(25%)-RuO2(25%)-TiO2(50%) electrode exhibited better electrocatalytic activity than the Pt(50%)-RuO2(50%) anode. The observed higher performance of this electrode has been attributed to the enhanced dispersion of Pt and RuO2 particles, the formation of smaller crystallites of Pt and RuO2 by the addition of TiO2 and the electronic interactions between metals and TiO2.

Made available in DSpace on 2014-10-09T12:35:07Z (GMT). No. of bitstreams: 0 / Made available in DSpace on 2014-10-09T14:00:26Z (GMT). No. of bitstreams: 0 / Dissertação (Mestrado) / IPEN/D / Instituto de Pesquisas Energeticas e Nucleares - IPEN-CNEN/SP

Orientador: Silvio Roberto Andrietta / Tese (doutorado) - Universidade Estadual de Campinas, Faculdade de Engenharia Quimica / Made available in DSpace on 2018-08-06T08:57:55Z (GMT). No. of bitstreams: 1 Porto_LiadeMendonca_D.pdf: 3965643 bytes, checksum: af08099e2fd964cfed91edc4842675e0 (MD5) Previous issue date: 2006 / Resumo: Este trabalho consiste em determinar o modelo que melhor descreve a fermentação alcoólica industrial, em sistemas contínuos de reatores de mistura em série. Para determinação dos parâmetros cinéticos foi desenvolvido um programa utilizando os dados de análises feitas em amostras retiradas de usinas em operação. Dos modelos testados, o Tosseto (2002), Lee; Pagan; Rogers (1983) e Levenspiel (1980), não apresentaram incoerência física nem problema de convergência sendo estes indicados para descrever a cinética da fermentação alcoólica. Os parâmetros cinéticos comuns aos modelos apresentaram valores semelhantes, onde o parâmetro Ks' limitação pelo substrato, foi de 3,0:t 0,4, o valor da concentração limite pelo produto inibidor, Pmáx' foi 92:t 9 e o fator exponencial de inibição pelo produto, YN, foi 5,3:t 0,9. O fator de inibição pelo substrato do modelo Tosseto (2002), Ki, foi 27:t 5 . O parâmetro X máx ' inibição pela massa celular, e YM, fator exponencial desta inibição, para o modelo Lee; Pagan; Rogers (1983) foram 1O0:t 1 e 0,9:t 0,1, respectivamente. A escolha pelo modelo Tosetto (2002) para implementação do programa de simulação do processo foi devido à tentativa de uma maior abrangência na obtenção das constantes cinéticas devido à possibilidade de inibição pelo substrato. A simulação em regime permanente trata-se da resolução equações algébricas dos balanços de massa do sistema e é capaz de dimensionar a etapa de fermentação de novas plantas a serem implantadas, enquanto que a simulação em regime transiente, tem o intuito de avaliar modificações durante a operação da usina e as equações diferenciais obtidas a partir dos balanços de massa devem ser resolvidas por método numérico, que neste caso foi utilizado o Runge-Kutta de quarta ordem / Abstract: This work aimed to determinate a model that best describes the industrial scale alcoholic fermentation in continuous serial mixing reactors. Software was developed in order to establish the kinetics parameters, using analysis data performed on samples from operating plants. The models described by Tosseto (2002), Lee; Pagan; Rogers (1983) and Levenspiel (1980), did not display physical incoherence or even convergence problems that described alcoholic fermentation kinetics. The kinetics parameters shown in all models presented similar values, like K (substrate limitation) was 3,0:t 0,4, Pmáx (limited product concentration) was 92:t 9 and YN (product inhibition power factor) was 5,3:t 0,9. The K (substrate inhibition) studied by Tosseto (2002) was 27:t 5. X máx (cell mass inhibition) and YM (cell mass inhibition factor power) were respectively 1O0:t 1 and 0,9:t 0,1 to Lee; Pagan; Rogers (1983). The kinetics parameters abranger due the substrate inhibition obtained by Tosetto (2002) this model was chosen in order to implement the simulating software. The stady state simulation is about system' s mass balance algebric equations resolution and is capable to dimension the fermentation step in new plants to be implanted while the unstady state simulation have the intention to evaluate modifications during the plant operation and the differential equations obtained from mass balance must be resolved by numerical methods, in this case, was used the fouth order Runge-Kutta / Doutorado / Desenvolvimento de Processos Biotecnologicos / Doutor em Engenharia Química

Made available in DSpace on 2014-10-09T12:35:07Z (GMT). No. of bitstreams: 0 / Made available in DSpace on 2014-10-09T14:00:26Z (GMT). No. of bitstreams: 0 / As células a combustível do tipo PEM (Próton Exchange Membrane) alimentadas diretamente por hidrogênio são consideradas as mais promissoras para a geração de energia elétrica, entretanto o uso de hidrogênio como combustível nestas células apresenta ainda alguns inconvenientes operacionais e de infra-estrutura, o que dificulta o seu uso. Assim, nos últimos anos, uma célula a combustível que utiliza um álcool diretamente como combustível (DAFC - Direct Alcohol Fuel Cell) tem despertado bastante interesse, particularmente aquelas que são alimentadas pelos combustíveis metanol ou etanol, pois apresentam várias vantagens, como por exemplo, a não necessidade de estocar hidrogênio ou gerá-lo através da reforma de hidrocarbonetos.Porém, células que utilizam diretamente metanol como combustível, apresentam correntes relativamente baixas e a oxidação completa do etanol é dificultado pela quebra da ligação CC e também há a formação de intermediários fortemente adsorvidos no eletrocatalisador de platina, como o monóxido de carbono (COads), resultando em baixos potenciais operacionais na célula.Para minimizar o efeito causado pelos venenos catalíticos faz-se necessária a adição de outros metais na composição do eletrodo de Pt. Tais metais devem atuar na reação fornecendo sítios para a adsorção de espécies que contenham oxigênio (OH ou H2O), em potenciais inferiores ao potencial de adsorção de OH na Pt.Este trabalho apresenta estudos da reação de eletro-oxidação destes álcoois, nos meios ácido e alcalino, sobre os eletrocatalisadores Pt/C, PtAu/C e PtAuBi/C, utilizando o método da redução via feixe de elétrons. Os eletrocatalisadores PtAuBi/C foram preparados com diferentes composições atômicas a fim de se avaliar o efeito da adição de bismuto. Os experimentos foram caracterizados por voltametria cíclica e cronoamperometria, utilizando a técnica do eletrodo de camada fina porosa, obtendo informações em relação às atividades dos catalisadores, perfis eletroquímicos e suas estabilidades em relação ao tempo de operação. Os eletrodepósitos foram examinados usando análise de energia dispersiva de raios-X (EDX) e microscopia eletrônica de varredura (MEV) a fim de determinar a composição de fases, o tamanho e a distribuição das nanopartículas metálicas no suporte. Os resultados eletroquímicos mostraram para oxidação eletroquímica de metanol, no meio alcalino, que o catalisador de PtAu/C apresentou melhor atividade eletrocatalítica e, no meio ácido, o catalisador Pt/C foi mais efetivo com relação às demais formulações preparadas e os eletrocatalisadores PtAuBi/C apresentaram-se pouco efetivos. No caso da oxidação do etanol, os dados eletroquímicos mostraram que, no meio ácido os catalisadores PtAu e Pt/C possuem comportamentos similares e os catalisadores PtAuBi/C demonstram baixa atividade. No meio alcalino, o sistema PtAuBi/C obteve melhor desempenho em relação aos demais catalisadores, obtendo maiores valores de correntes à baixos potenciais. / Dissertação (Mestrado) / IPEN/D / Instituto de Pesquisas Energeticas e Nucleares - IPEN-CNEN/SP

Made available in DSpace on 2016-08-19T12:56:45Z (GMT). No. of bitstreams: 1 Dissertacao Darlan.pdf: 2834733 bytes, checksum: f7d35c098bddf8713fbdbe733565fdef (MD5) Previous issue date: 2013-07-12 / During several years, adulterated gasoline has been commercialized across all Brazil. Often such product has higher alcohol content, water traces or organic solvents insertion (e.g. paint thinner and/or turpentine). The use of nonconforming gasoline, in the short and long terms, has several problems for consumers, for the vehicle and the environment. Thus, this work aims to propose a low cost technique for analyzing gasoline blends, in relation to its oxygenated addition. Both capacitance and dielectric constant (relative permittivity) were determined by means of a high precision LCR-meter, using a metal concentric sensor. Therefore, gasoline blends were prepared by adding 16, 18, 20, 22, 24, 26, 28 and 30% of AEAF to the initial petroleum-based fuel and their dielectric constants were measured at frequencies of 0.3, 0.4, 0.5 and 0.6 kHz. The same samples were analyzed by the reference method, the Test Tube Test. According to statistical modeling, the frequency of 0.6 kHz showed the most significant results for all samples. The results show that at 95% confidence level, there is no significant difference between the two methods, indicating a good correlation between the proposed method and then standard one. However, when the density was used as evaluating parameter, instead of dielectric constant, for the same samples, a substantial discrepancy of the obtained values were observe, suggest a low sensibility of such methodology. / Vários são os casos de não conformidade da gasolina comercial, principalmente pelo excesso de etanol, ou ainda pela adição de água ou solventes leves como thinner e aguarrás. O uso de gasolina não conforme, a curto e longo prazo, traz diversos problemas para o consumidor, para o veículo e ao meio ambiente. No presente trabalho estudou-se a qualidade da gasolina tipo C, comercializada nos postos revendedores de combustível, no que diz respeito à concentração de álcool etílico anidro combustível (AEAC). Análises estas, realizadas através de medidas de constante dielétrica (permissividade relativa) utilizando sensor capacitivo. Misturas de gasolina A e AEAC foram preparadas nas concentrações de 16, 18, 20, 22, 24, 26, 28 e 30% de AEAC, sendo suas constantes dielétricas medidas nas frequências de 0,3; 0,4; 0,5 e 0,6 kHz. Utilizando tratamento estatístico verificou-se que a frequência de 0,6 kHz apresentou resultados mais significativos para leitura de AEAC das misturas preparadas. Nessa mesma frequência, amostras comerciais de gasolina e amostras de gasolinas não conformes contaminadas com gasolina A e AEAC foram submetidas à análise. As mesmas amostras foram submetidas à análise pelo método de referência, o Teste da Proveta. Os resultados obtidos mostram que, no nível de confiança de 95%, não há diferença significativa entre os dois métodos. Medidas de massas específicas também foram realizadas com as misturas gasolina A e AEAC (16 a 30%) para modelamento de curva de calibração com finalidade de determinar o teor de AEAC e posterior comparação com os resultados oriundos da constante dielétrica e do teste da proveta, entretanto, o método não se mostrou eficiente para análise das amostras de gasolina comercial e amostras de gasolinas não conformes analisadas.

>Magister Scientiae - MSc / This study explores the use of UV-assisted reduction method to synthesise the catalysts, aiming at reducing synthesis time. The Pd and Au catalyst loading is kept at 5 wt% in order to reduce the cost associated with high loading (20 wt%) of platinum group metals. The synthesised catalysts have SnO2 incorporated in them for two purposes, one being to activate the chemical reaction by absorbing UV-light and the second one is to serve as a promoter for binary and ternary catalysts. All the synthesised electrocatalysts in this study were denoted as Au/10wt%SnO2-C, Au/15wt%SnO2-C, Au/20wt%SnO2-C, Au/40wt%SnO2-C, Au/60wt%SnO2-C, Pd/10wt%SnO2-C, Pd/15wt%SnO2-C, Pd/20wt%SnO2-C, Pd/40wt%SnO2-C, Pd/60wt%SnO2-C and PdAu/10wt%SnO2-C respectively. The UV-assisted reduction method was proved to be effective with the obtained results from TEM, SEM, XRD and electrochemical studies. TEM micrographs revealed nanoparticles of Pd, Au and SnO2 which were proved by the measured d-spacing values corresponding to the element’s structures. The measured average particle size ranged from 3.05 to 14.97 nm for the electrocatalysts. The XRD profiles confirmed the face centred cubic of Pd, Au and tetragonal structures of SnO2. These electrocatalysts showed varied activity towards the oxidation of alcohols namely, methanol, ethanol, ethylene glycol and glycerol in alkaline electrolyte The cyclic voltammetry results showed improved performance towards the oxidation of glycerol on Au-based electrocatalysts, highest current density of 22.08 mA cm-2 than on Pd-based electrocatalysts. Pd-based electrocatalysts were more active towards the oxidation of ethanol than Au-based electrocatalysts with the highest current density of 19.96 mA cm-2. The co-reduced PdAu on 10wt%SnO2-C electrocatalysts showed the lowest current density of 6.88 mA cm-2 for ethanol oxidation when compared to Pd/10wt%SnO2-C and Au/10wt%SnO2-C. Linear sweep voltammograms showed more negative onset potentials on Pd-based electrocatalysts than Au-based electrocatalysts. The more negative onset potential obtained on Pd-based electrocatalysts was observed for ethanol oxidation. These results correspond to the trend observed in literature for ethanol oxidation being more favoured on Pd-based electrocatalysts whereas the polyalcohol oxidation is more favoured on Au-based electrocatalysts. The best performing and most stable electrocatalyst among the Au-based electrocatalysts is Au/10wt%SnO2-C and Pd/10wt%SnO2-C for the Pd-based electrocatalysts.

A mixed integer programming model is developed to determine a logistical design for maximizing rates of return to harvest, storage, transportation, and bioreflning of herbaceous crop residue for production of biofuels and feed for ruminant animals. The primary objective of this research is to identify the optimal location, scale, and number of pretreatment and biorefinery plants in northeastern North Dakota. The pretreatment and biorefinery plants are modeled under the assumption that they utilize recent technological advancement in AFEX and Simultaneous Saccharification and Fermentation, respectively. Potential feedstocks include wheat straw, barley straw, Durum straw, and com stover. Results indicate that the minimum ethanol rack price that will effectively trigger the production of cellulosic ethanol is $1.75 per gallon.

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.