Thesis (Ph. D.)--Ohio State University, 2008. / Title from first page of PDF file. Includes bibliographical references (p. 106-108).

Thesis (Ph. D.)--Mechanical Engineering, Georgia Institute of Technology, 2006. / Wick, Tim, Committee Member ; Neitzel, Paul, Committee Member ; Fyhrie, David, Committee Member ; Garcia, Andres, Committee Member ; Guldberg, Robert, Committee Chair. Vita.

Thesis (Ph. D. in Chemical Engineering)--Vanderbilt University, Aug. 2005. / Title from title screen. Includes bibliographical references.

Thesis (Ph. D.)--Ohio State University, 2006. / Title from first page of PDF file. Includes bibliographical references (p. 211-229).

Effective treatment of wastewater is an important process in reducing the environmental impact of industry and human activity. Although conventional water treatment systems can adequately remove the principle components of waste (i.e. substances that can be represented the majority of biological and chemical oxygen demand) several materials are poorly or slowly removed. Tertiary treatment polishing processes are therefore required to remove these contaminants to ensure complete wastewater treatment. This thesis reports investigations made using film reactors that are used to remove recalcitrant materials such as ammonia- nitrogen and endocrine disrupters that although present in low concentrations, if left untreated can have a strong impact on the environment. Film reactors potentially offer several process advantages over conventional activated sludge treatments systems as they allow very long residence time and contact with high concentrations of fixed microbes with the low concentrations of pollutants so enhancing kinetic performance and efficiency of the process. Two reactor configurations, a partial fixed bed (PFBR) and moving bed biofilm reactors (MBBR) were investigated. A thirty liter reactor with a working volume of 16 liters was constructed and contained fixed microbial films on either free suspended or fixed beds plastic packing (K2 AnoxKaldnes). The investigation of ammonia-nitrogen oxidation showed that after a suitable acclimation period (2 weeks) that ammonia was oxidise rapidly reducing the feed concentrations of 35 mg/L to < 2 mg/L in the effluent. To assess the performance for ammonia-nitrogen removal the reactors operated for long periods (up to 3 months) with continuous feed using the reactor in either PFBR or MBBR modes in addition of 17alpha-ethynylestradiol (EE2) and mestranol (MeEE2), the endocrine disrupting compounds commonly found in municipal wastewater. These substances is derived from a synthetic hormones if found in the natural environment can reduced the productivity of the fish as this can cause feminization in aquatic organisms with disastrous consequences on fish populations. The MBBR and PFBR systems were used to investigate the co-metabolism of ammonia-nitrogen, 17alpha-ethynylestradiol (EE2) and mestranol from model waste water feed containing 35 mg/L of ammonia-nitrogen and 100 mug/L of 17alpha-ethynylestradiol (EE2) and mestranol (MeEE2). A kinetic analysis of the systems were made and for the PFBR reactor, the specific growth rate, mumax of 7.092 d-1 with saturation constants, Ks of 1.574 mg/L. The kinetic analysis for the MBBR system was 6.329 d-1 for the mumax with the K.S of 0.652 mg/L. When the PFBR was used removal of EE2 represents 70% MeEE2 was removed. MBBR were shown to be more effective and efficient in removing ammonia-nitrogen reducing the levels under good conditions to > 2 mg/L while the PFBR could also achieve 2 mg/L. The MBBR system was also more competent in the removal of 17alpha-ethynylestradiol (EE2) and mestranol compared to PFBR. This work demonstrates that there are considerable advantages to using thin film reactors as polishing step for the tertiary treatment of waste waters when to compared to other processes in reducing the inorganic pollutants as endocrine disrupting compounds. The significance of these results is discussed in this context.

Em biorreatores de agitação mecânica (STR), a circulação e a mistura do fluido são influenciadas pela configuração do equipamento e pela disposição dos impelidores e aspersores de gás. Já em biorreatores airlift, sua geometria e, principalmente, o tipo e forma de aspersão de oxigênio, têm primordial efeito tanto na transferência de oxigênio quanto no crescimento microbiano e na formação de produtos. Para o cultivo de Aspergillus oryzae IPT-301, o suprimento de oxigênio é um parâmetro fundamental, em razão do metabolismo unicamente aeróbio deste microrganismo. Neste contexto, analisou-se o transporte de massa gasosa em ambos os equipamentos, contendo fluidos com viscosidades distintas: água destilada e diferentes concentrações de soluções de pectina. Com estudos de mecânica dos fluidos, correlações matemáticas empíricas para determinação do coeficiente volumétrico de transferência de oxigênio (KLa) foram utilizadas para relacionar os resultados experimentais com os calculados. A produção de pectinases também foi avaliada nesses equipamentos. O meio de cultivo continha sais nutrientes, extrato de levedura, glicose e pectina cítrica. Avaliaram-se diferentes configurações de impelidores Rushton e pitched blade, além de várias geometrias de aspersores de gás, tais como ferradura de aço inoxidável, pedra sinterizada, aeradores de aquário e de latão e funis de vidro sinterizado. Em STR, a análise fatorial mostrou que os maiores incrementos de KLa foram com a combinação de impelidores Rushton, em água, com aspersor do tipo aquário a 700rpm e 1,71L/L/min; em airlift, com o aspersor aquário, alocado na região externa do tubo interno, e com o aspersor pedra sinterizada. O modelo proposto por Miller (1974) foi o mais adequado para determinar a potência requerida pelos fluidos deste trabalho, em STR e sob aeração. O modelo de Wang et al. (1979), com adaptações, ajustou-se aos dados com água; e para as soluções de pectina, a correlação descrita por Badino Jr. et al. (2001) foi melhor ajustada. Três ensaios para produção enzimática foram processados em STR: ambos com três impelidores Rushton, aspersores dos tipos ferradura (A), aquário (B) e aquário com meio com pectina desesterificada (C). Em airlift, foram testadas as condições produtivas com os aspersores do tipo aquário (externo) (A), pedra sinterizada (B) e aquário (externo), com pectina desesterificada (C). Em STR, o melhor resultado de KLa, em meio isento de células, foi na condição C (29,88h-1), bem como vantagens econômicas como o menor tempo de permanência da máxima frequência dos agitadores (tf,máx) (A: 23h; B: 8,5h; C:5h). Porém, resultado superior de máxima produção de pectinases foi na condição B (A: 24,60U/mL; B: 25,53U/mL; C: 13,36U/mL) em tf,máx inferior à condição A. Em airlift, o transporte de oxigênio, em meio isento de células, foi mais favorecido em A (21,96h-1), bem como o menor tempo máximo para manter a máxima vazão específica do gás (A: 29h; B: 72h; C: 57h). Além disso, a máxima atividade enzimática foi superior na mesma condição (A: 24,61U/mL; B: 21,94U/mL; C: 2,29U/mL). Assim, conclui-se que, desde que planejadas as condições operacionais e de processo de produção de pectinases de A. oryzae, ambos os biorreatores podem ser aplicados na produção de pectinases fúngicas. / Submitted by Ana Guimarães Pereira (agpereir@ucs.br) on 2016-04-29T14:18:46Z No. of bitstreams: 1 Dissertacao Fernando Henrique Stuani.pdf: 2953600 bytes, checksum: 1ab57ebbd31c1cc7c4c0b5c2b729cdd5 (MD5) / Made available in DSpace on 2016-04-29T14:18:46Z (GMT). No. of bitstreams: 1 Dissertacao Fernando Henrique Stuani.pdf: 2953600 bytes, checksum: 1ab57ebbd31c1cc7c4c0b5c2b729cdd5 (MD5) Previous issue date: 2016-04-29 / Coordenação de Aperfeiçoamento de Pessoal de Nível Superior,CAPES / In stirred tank reactors (STR), circulation and mixing of fluid are influenced by the reactor configuration and by how the impellers and the gas spargers are arranged in them. On the other hand, in airlift bioreactors, their geometry and especially the type and form of oxygen sparging have an effect on both oxygen transfer and on microbial growth and product formation. Oxygen supply for the cultivation of Aspergillus oryzae IPT-301 is a key parameter due to the aerobic metabolism of this microorganism. In this context, oxygen transfer in both equipments was analyzed. They contained fluids with different viscosities: distilled water and different concentrations of pectin solutions. Through the use of fluid mechanics studies, empirical mathematical correlations were used in order to determine the volumetric oxygen transfer coefficient (KLa) to match experimental and calculated results. Pectinase production was also assessed in those devices. The culture medium contained salts, yeast extract, glucose and citrus pectin. Different Rushton and pitched blade impeller configurations were evaluated, as well as various gas sparger geometries, such as stainless steel horseshoe, sintered stone, aquarium and brass spargers, and also sintered glass funnels. In STR, factorial design showed that the largest KLa value was obtained with the combination of Rushton impellers, in water, with the aquarium sparger, at 700rpm and 1.71L/min; in airlift, with the same sparger, put in the outer space of the inner tube and with the sintered stone sparger. The empirical correlation proposed by Miller (1974) was the most suitable one to determine the power requirement by the fluids in this work, in STR and under aeration. The correlation proposed by Wang et al. (1979), with adaptations, was better adjusted to the data set with water; the correlation described by Badino Jr. et al. (2001) was better suited for pectin solutions. Three tests for enzyme production were processed in STR: with three Rushton impellers, in all of them, and horseshoe (A), aquarium (B) and aquarium with non-esterified pectin medium (C) spargers. In airlift, enzyme production was tested with aquarium (external) (A), sintered stone (B) and aquarium (external) with non-esterified pectin (C) spargers. In STR, the best result of KLa in cell-free medium was provided in condition C (29.88h-1), as well as economic advantages such as shorter length of maintenance of the maximum impeller speed (tf,máx) (A: 23h; B: 8.5h; C: 5h). Nonetheless, higher pectinase production was obtained in condition B (A: 24.60U/mL; B: 25.53U/mL, C: 13.36U/mL) in tf,máx shorter than in condition A. In airlift, higher oxygen transfer in cell-free medium was obtained in condition A (21.96h-1), as well as the lowest length of maintenance of the maximum specific gas flow rate (A: 29h; B: 72h; C: 57h). Furthermore, maximum enzyme activity was higher in the same condition (A: 24.61U/mL; B: 21.94U/mL, C: 2.29U/mL). Thus, we conclude that if the operational conditions for pectinase production by A. oryzae are well planned, both bioreactors can be applied for the production of fungal pectinases.

Submitted by Ana Guimarães Pereira (agpereir@ucs.br) on 2017-06-28T19:23:07Z No. of bitstreams: 1 Dissertacao Analia Borges Folle.pdf: 186844 bytes, checksum: 69bcf521f0587de7f849e1ff68ab8974 (MD5) / Made available in DSpace on 2017-06-28T19:23:07Z (GMT). No. of bitstreams: 1 Dissertacao Analia Borges Folle.pdf: 186844 bytes, checksum: 69bcf521f0587de7f849e1ff68ab8974 (MD5) Previous issue date: 2017-06-28 / Coordenação de Aperfeiçoamento de Pessoal de Nível Superior, CAPES.

Thesis (MTech: Chemical Engineering))--Cape Peninsula University of Technology, 2012 / The microbial ferrous-iron oxidation process plays a significant role in bioleaching, providing ferric-iron (Fe3+) − a strong oxidising agent for the dissolution of most sulphide minerals. An extensive literature review has shown that several studies have been carried out on microbial ferrous-iron oxidation, mostly in stirred tank reactors and in conditions close to optimum. However, limited studies have been carried out on this subject in the context of heap bioleach situation. Despite the fact a packed column system may be used to represent heap bioleaching, most of the studies on microbial ferrous-iron oxidation in such systems were carried out under flooded/fluidised conditions which do not adequately represent solution flow dynamics in a heap system. The microbial ferrous-iron oxidation kinetics of Leptospirillum ferriphilum were studied at substrate loading rates of 0.17 – 0.5 g.L-1h -1 (dilution rates 0.033 – 0.1 h-1). The study was conducted in a packed column with a view to investigating the kinetics in a system which simulates the solution flow dynamics of a typical heap bioleach operation. Glass marbles, 15 mm in diameter, were used as reactor packing. The microbial oxidation kinetics were investigated in a continuous mode at the desired loading rates. The pH of the bioreactor was maintained at pH 1.45 ± 0.05 and the aeration at 15 mL.s-1. Both Monod and Hansford models were used to describe the biooxidation kinetics.

Thesis (MTech (Chemical Engineering))--Cape Peninsula University of Technology, 2009 / The main purpose of this study was to quantify the growth and oxygen mass transfer kinetic parameters of the filamentous bacterium Streptomyces coelicolor, immobilised on the external surface of a ceramic membrane in a continuously operated pressurised Membrane Gradostat Bioreactor (MGR). One of the most important and critical parameters required when studying biofilms, are the growth kinetics, as they can be utilised to model both the mass transfer and biological reactions occurring within the biofilm. Single fibre MGR's (SFMGR) were operated using a pneumatic system to supply humidified pressurised air to the extra capillary space (ECS) and pressurised growth medium to the lumen of the ceramic membrane. Two growth media; a complex growth medium, ISP2, and a defined growth medium, were tested and supplied to the lumen of the ceramic membrane in the dead-end mode

Thesis submitted in fulfilment of the requirements for the degree DOCTOR TECHNOLOGIAE: ENGINEERING: CHEMICAL In the FACULTY OF ENGINEERING At the CAPE PENINSULA UNIVERSITY OF TECHNOLOGY 2009 / The white rot fungus, Phanerochaete chrysosporium strain BKMF-1767 (ATCC 24725), produces the extracellular enzymes, Lignin peroxidase (LiP) and Manganese peroxidase (MnP), that constitute the major route for lignin degradation by this organism. LiP and MnP have also been shown to play a major role in aromatic pollutant degradation. Due to the need for continuous production of LiP and MnP, a fixed-film bioreactor, classified as a membrane gradostat reactor (MGR), was developed. The implementation of batch-reactor operational parameters to the MGR system was found to be ineffective, thus creating the need for further research to improve the operational aspects of the MGR system to optimise its capabilities for continuous and industrial-scale operations. The research undertaken in this study, provides information that can be used to classify the dissolved oxygen (DO) transport kinetics into immobilised fixed-films of P. chrysosporium. Operational limitations of the MGR relating to environmental stresses in the bioreactor during operation and to biofilm deterioration, including limitations of DO mass transport, oxidative stress, trace element accumulation and polysaccharide storage in the fungal biomass, were evaluated in single capillary MGR systems (SCMGRs). These conditions were identified as existing in the continuous MGR systems. From DO profiles, the oxygen consumption and flux into the biofilms, including the distribution of DO, was determined to be dependent on the immobilised biofilm’s age. Younger biofilms showed higher DO distribution than older biofilms even when aeration was directed to the extracapillary space (ECS) of the reactor against the biofilm’s surface. An increase in anaerobic zone thickness was observed to be increasing with an increase in biofilm thickness. Although, DO kinetic parameters were comparable with those obtained in submerged mycelia pellets, higher oxygen consumption values were observed in biofilms grown in the SCMGRs. The limitations of MGR were identified as: 1) poor DO distribution in immobilised biofilms because of b-glucan production and storage in the immobilised biomass, resulting in ethanol production; 2) the peroxidation of lipids of the biofilms, which in turn will affect the long-term performance of the biomass caused by oxygenation and 3) trace element ion accumulation enhanced by b-glucan production. Furthermore, trace element ion accumulation was higher in the MGRs than in batch cultures using the same nutrient medium. The development of a perfluorocarbon (PFC) emulsion for the MGRs to counteract these limitations was investigated. The compatibility of the emulsion with oxygen-carrying capacity was shown with an improvement in biomass generation, LiP/MnP production and overall consumption of primary substrates, mainly glucose and ammonium tartrate, in batch cultures. The emulsions investigated were based on the addition of oxygen carriers: Perfluorooctyl bromide (PFOB), Bis-(Perfluorobutyl) ethene (PFBE) and Perfluoropropylamine (PFPA), using Pluronic F 68 (PF 68) as the surfactant. Concentrations of 10 to 30% (w/v) PFC and 8.5% (w/v) PF 68 were tested successfully in batch cultures. The emulsions containing 10% (w/v) PFCs resulted in improved biomass performance as opposed to emulsions with higher PFC oil concentrations. An emulsion containing 10% (w/v) PFOB was used to evaluate its efficacy in the SCMGRs, as the biomass yield and overall enzyme production were superior to PFPA and PFBE-based emulsions with similar oil concentrations. After successfully applying PFOB and PF 68 to the SCMGRs, the following results were obtained: 1) reduced ethanol production; 2) reduced trace element accumulation; 3) lower b-glucan production and 4) improved DO-penetration ratio in immobilised biofilms.