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Este trabalho foi teve como objetivo avaliar o desempenho do tratamento aerado combinando biomassa aderida e suspensa, em diferentes condições de temperatura (25ºC, 27ºC, 45ºC e 55ºC), na remoção da matéria orgânica. Foi utilizada uma água residuária sintética simulando o efluente da indústria de geleias e compotas de frutas. Os dois reatores operados foram construídos em aço inox com diâmetro de 15 cm, 58,0 cm de altura e volume útil de 10,25 L, sendo 5,125 L preenchidos com meio suporte. O experimento se deu em duas fases. Na primeira (75 dias) o reator R1 foi operado a 25ºC e o R2 a 45ºC, na segunda (60 dias) a 27ºC e 55ºC, respectivamente. O TDH variou de 10,39h a 11,86h e a carga orgânica volumétrica aplicada de 2,82 kg.m-3.d-1 a 3,51 kg.m-3.d-1. As maiores eficiências de remoção de DQO foram observadas nos reatores R1(25ºC) e R2(45ºC): 80,27±11,97% e 78,41±6,41%, respectivamente. Estas médias não diferiram entre si. A colonização do meio suporte foi satisfatória, exceto a 55ºC onde se verificou a diminuição da aderência da biomassa. Foi observado o intumescimento do lodo nas duas fases experimentais, provavelmente devido à alta biodegradabilidade da água residuária, e um maior valor de SSV no efluente dos sistemas termofílicos. Os ensaios cinéticos apontaram para uma menor dependência do sistema na parcela suspensa da biomassa para a eficiência global. A análise do DGGE mostrou diminuição na diversidade entra a biomassa aderida do reator mesofílico (25ºC) e a biomassa aderida do reator termofílico (45ºC), entretanto, esta mudança não foi tão evidente de 45ºC para 55ºC. / The aim of this study was to investigate the attached and suspended biomass performance in the organic matter removal of a synthetic jams and jellies wastewater at different temperature (25ºC, 27ºC, 45ºC and 55ºC). Two stainless steel reactors, 15 cm diameter and 58 cm high were used. The working volume was 10,25 L and the support medium occupied 5,125 L. The experiment was developed in two stages. The first stage lasted 75 days, the R1 and R2 reactors operated at 25ºC and 45ºC, respectively. The second stage lasted 60 days and the reactors operated at 27ºC and 55ºC, respectively. The HRT ranged between 10,39h and 11,86h and the volumetric load between 2,82 kg.m-3.d-1 to 3,51 kg.m-3.d-1.The highest removal efficiencies of COD occurred in R1(25ºC) and R2(45ºC) reactors: 80,27±11,97% and 78,41±6,41%, respectively. These results were not statistically different. The colonization of the support medium was satisfactory, except at 55ºC, as in this condition it was observed decreased adhesion of biomass. Bulking occurred in both stages of the experiment, probably due to the high biodegradability of this wastewater, and a highest value of MLVSS in the effluent of the thermophilic systems. The kinect experiments appointed that the suspended biomass play a minor role in the global efficiency of the system. The DGGE analysis have shown reduction in diversity when the temperature increases from 25ºC to 45ºC, nevertheless, this change was not so clear from 45ºC to 55ºC.

Este trabalho foi teve como objetivo avaliar o desempenho do tratamento aerado combinando biomassa aderida e suspensa, em diferentes condições de temperatura (25ºC, 27ºC, 45ºC e 55ºC), na remoção da matéria orgânica. Foi utilizada uma água residuária sintética simulando o efluente da indústria de geleias e compotas de frutas. Os dois reatores operados foram construídos em aço inox com diâmetro de 15 cm, 58,0 cm de altura e volume útil de 10,25 L, sendo 5,125 L preenchidos com meio suporte. O experimento se deu em duas fases. Na primeira (75 dias) o reator R1 foi operado a 25ºC e o R2 a 45ºC, na segunda (60 dias) a 27ºC e 55ºC, respectivamente. O TDH variou de 10,39h a 11,86h e a carga orgânica volumétrica aplicada de 2,82 kg.m-3.d-1 a 3,51 kg.m-3.d-1. As maiores eficiências de remoção de DQO foram observadas nos reatores R1(25ºC) e R2(45ºC): 80,27±11,97% e 78,41±6,41%, respectivamente. Estas médias não diferiram entre si. A colonização do meio suporte foi satisfatória, exceto a 55ºC onde se verificou a diminuição da aderência da biomassa. Foi observado o intumescimento do lodo nas duas fases experimentais, provavelmente devido à alta biodegradabilidade da água residuária, e um maior valor de SSV no efluente dos sistemas termofílicos. Os ensaios cinéticos apontaram para uma menor dependência do sistema na parcela suspensa da biomassa para a eficiência global. A análise do DGGE mostrou diminuição na diversidade entra a biomassa aderida do reator mesofílico (25ºC) e a biomassa aderida do reator termofílico (45ºC), entretanto, esta mudança não foi tão evidente de 45ºC para 55ºC. / The aim of this study was to investigate the attached and suspended biomass performance in the organic matter removal of a synthetic jams and jellies wastewater at different temperature (25ºC, 27ºC, 45ºC and 55ºC). Two stainless steel reactors, 15 cm diameter and 58 cm high were used. The working volume was 10,25 L and the support medium occupied 5,125 L. The experiment was developed in two stages. The first stage lasted 75 days, the R1 and R2 reactors operated at 25ºC and 45ºC, respectively. The second stage lasted 60 days and the reactors operated at 27ºC and 55ºC, respectively. The HRT ranged between 10,39h and 11,86h and the volumetric load between 2,82 kg.m-3.d-1 to 3,51 kg.m-3.d-1.The highest removal efficiencies of COD occurred in R1(25ºC) and R2(45ºC) reactors: 80,27±11,97% and 78,41±6,41%, respectively. These results were not statistically different. The colonization of the support medium was satisfactory, except at 55ºC, as in this condition it was observed decreased adhesion of biomass. Bulking occurred in both stages of the experiment, probably due to the high biodegradability of this wastewater, and a highest value of MLVSS in the effluent of the thermophilic systems. The kinect experiments appointed that the suspended biomass play a minor role in the global efficiency of the system. The DGGE analysis have shown reduction in diversity when the temperature increases from 25ºC to 45ºC, nevertheless, this change was not so clear from 45ºC to 55ºC.

Reaction water, a high-strength COD (chemical oxygen demand) petrochemical effluent, is generated during the Fischer-Tropsch reaction in the SASOL Synthol process at SASOL SynFuels, Secunda, South Africa. Distillation of the reaction water to remove non- and oxygenated hydrocarbons yields approximately 25 - 30 ML/d of an organic (carboxylic) acid-enriched stream (average COD of 16 000 mg/L) containing primarily C2 – C5 organic acids, light oils, aldehydes, ketones, cresols and phenols. Together with the Oily sewer water (API) and Stripped Gas Liquor (SGL) process streams, this process effluent is currently treated in ten dedicated activated sludge basins. However, the successful operation of these activated sludge systems has proven to be difficult with low organic loading rates (3.5 kg COD/m3.d) low COD removal efficiencies (<80 %) and high specific air requirements (60 - 75 m3 air/kg CODrem). It is hypothesised that these operational difficulties can be attributed to organic shock loadings, variation in volumetric and hydraulic loadings, as well as variations in the composition of the various process streams being treated. Due to the fact that the Fischer-Tropsch (Synthol) reaction water constitutes 70 % of the COD load on the activated sludge systems, alternative processes to improve the treatment cost and efficiency of the Fischer-Tropsch acid stream are being investigated. Various studies evaluating the aerobic and anaerobic treatment of Fischer-Tropsch reaction water alone in suspended growth wastewater treatment systems have proven unsuccessful. High rate fixed-film processes or biofilm reactors, of which the fluidised-bed reactors are considered to he one of the most effective and promising processes for the treatment of high-strength industrial wastewaters, could he a suitable alternative. The primary aim of this study was to evaluate the suitability of biological fluidised-bed reactors (BFBRs) for the treatment of Fischer-Tropsch reaction water. During this study, the use of aerobic and anaerobic biological fluidised-bed reactors (BFBR), using sand and granular activated carbon (GAC) as support matrices, were evaluated for the treatment of a synthetic effluent analogous to the Fischer-Tropsch reaction water stream. After inoculation, the reactors were operated in batch mode for 10 days at a bed height expansion of 30% and a temperature of 30 ºC to facilitate biofilm formation on the various support matrices. This was followed by continuous operation of the reactors at hydraulic retention times (HRTs) of 2 days. While the COD of the influent and subsequent organic loading rate (OLR) was incrementally increased from 1 600 mg/L to a maximum of 20 000 mg/L and 18 000 mg/L for the aerobic and anaerobic reactors, respectively. Once the maximum influent COD concentration had been achieved the OLR was further increased by decreasing the HRTs of the aerobic and anaerobic reactors to 24h and 8h, and 36h, 24h and 19h, respectively. The dissolved O2 concentration in the main reactor columns of the aerobic reactors was constantly maintained at 0.50 mg/L. Chemical Oxygen Demand (COD) removal efficiencies in excess of 80 % at OLR of up to 30 kg COD/m3.d were achieved in the aerobic BFBRs using both sand and GAC as support matrices. Specific air requirements were calculated to be approximately 35 and 41 m3 air/kg CODrem for the BFBRs using sand and GAC as support matrices, respectively. The oxygen transfer efficiency was calculated to be approximately 5.4 %. At high OLR (> 15 kg COD/m3.d) significant problems were experienced with plugging and subsequent channelling in the BFBR using GAC as support matrix and the reactor had to be backwashed frequently in order to remove excess biomass. Despite these backwash procedures, COD removal efficiencies recovered to previous levels within 24 hours. In contrast, no significant problems were encountered with plug formation and channelling in the BFBR using sand as support matrix. In general the overall reactor performance and COD removal efficiency of the aerobic BFBR using sand as support matrix was more stable and consistent than the BFBR using GAC as support matrix. This BFBR was also more resilient to variations in operational conditions, such as the lowering of the hydraulic retention times and changes in the influent pH. Both aerobic reactors displayed high resilience and COD removal efficiencies in excess of 80 % were achieved during shock loadings. However, both reactors were highly sensitive to changes in pH and any decrease in pH below the pKa values of the volatile fatty acids in the influent (pKa of acetic acid = 4.76) resulted in significant reductions in COD removal efficiencies. Maintenance of reactor pH above 5.0 was thus an essential facet of reactor operation. It has been reported that the VFA/alkalinity ratio can be used to assess the stability of biological reactors. The VFA/alkalinity ratios of the aerobic BFBRs containing sand and GAC as support matrices were stable (VFNalkalinity ratios of < 0.3 - 0.4) until the OLR increased above 10 kg/m3.d. At OLRs higher than 10 kg/m3.d the VFA/alkalinity ratios in the BFBR using sand support matrix increased to 4, above the failure limit value of 0.3 - 0.4. In contrast the VFA/alkalinity ratios of the BFBR using GAC support matrix remained stable until an OLR of 15 kg/m3.d was obtained, where the VFA/alkalinity ratios then increased to > 3. Towards the end of the study when an OLR of approximately 25 kg/m3.d was obtained the VFA/alkalinity ratios of both the BFBRs using sand and GAC as support matrices increased to 9 and 6 respectively, indicating the decrease in reactor stability and acidification of the process. Total solid (TS) and volatile solid (VS) concentrations in the aerobic BFBRs were initially high and decreased over time. While the total suspended solids (TSS) and volatile suspended solids (VSS) concentrations were initially low and increased over time as the OLR was increased, this is thought to be as a result of decreased HRT leading to biomass washout. The anaerobic BFBR using sand as support matrix never stabilised and COD removal efficiency remained very low (< 30 %), possibly due to the high levels of shear forces. Further studies concerning the use of sand as support matrix were subsequently terminated. An average COD removal efficiency of approximately 60 % was achieved in the anaerobic BFBR using GAC as a support matrix at organic loading rates lower than 10 kg COD/m3.d. The removal efficiency gradually decreased to 50 % as organic loading rates were increased to 20 kg COD/m3.d. At OLRs of 20 kg COD/m3.d, the biogas and methane yields of the anaerobic BFBR using GAC as support matrix were determined to be approximately 0.38 m3 biogas/kg CODrem (0.3 m3 biogas/m3reactor vol.d), and 0.20 m3 CH4/kg CODrem (0.23 m3 CH4/m3reactor vol.d), respectively. This value is 57 % of the theoretical maximum methane yield attainable (3.5 m3 CH4/kg CODrem). The methane yield increased as the OLR increased, however, when the OLR reached 8 kg/m3.d the methane yield levelled off and remained constant at approximately 2 m3 CH4/m3reactor vol.d. Although the methane content of the biogas was initially very low (< 30 %), the methane content gradually increased to 60 % at OLRs of 20 kg COD/m3.d. The anaerobic BFBR using GAC as support matrix determined that as the OLR increased (>12 kg/m3.d), the VFA/alkalinity ratio increased to approximately 5, this is indicative of the decrease in stability and acidification of the process. The anaerobic BFBR using GAC as support matrix experienced no problems with plug formation and channelling. This is due to the lower biomass production by anaerobic microorganisms than in the aerobic reactors. The TS and VS concentrations were lower than the aerobic concentrations but followed the same trend of decreasing over time, while the TSS and VSS concentrations increased due to decreased HRTs. The anaerobic BFBR was sensitive to dramatic variations in organic loading rates, pH and COD removal efficiencies decreased significantly after any shock loadings. Compared to the activated sludge systems currently being used for the biological treatment of Fischer-Tropsch reaction water at SASOL SynFuels, Secunda, South Africa, a seven-fold increase in OLR and a 55 % reduction in the specific air requirement was achieved using the aerobic BFBRs. The methane produced could also be used as an alternative source of energy. It is, however, evident that the support matrix has a significant influence on reactor performance. Excellent results were achieved using sand and GAC as support matrices in the aerobic and anaerobic BFBRs, respectively. It is thus recommended that future research be conducted on the optimisation of the use of aerobic and anaerobic BFBRs using these support matrices. Based on the results obtained from this study, it can be concluded that both aerobic and anaerobic treatment of a synthetic effluent analogous to the Fischer-Tropsch reaction water as generated by SASOL in the Fischer-Tropsch Synthol process were successful and that the application of fluidised-bed reactors (attached growth systems) could serve as a feasible alternative technology when compared to the current activated sludge treatment systems (suspended growth) currently used. Keywords: aerobic treatment, anaerobic treatment, biological fluidised-bed reactors, petrochemical effluent, Fischer-Tropsch reaction water, industrial wastewater. / Thesis (M. Omgewingswetenskappe)--North-West University, Potchefstroom Campus, 2004.

Reaction water, a high-strength COD (chemical oxygen demand) petrochemical effluent, is generated during the Fischer-Tropsch reaction in the SASOL Synthol process at SASOL SynFuels, Secunda, South Africa. Distillation of the reaction water to remove non- and oxygenated hydrocarbons yields approximately 25 - 30 ML/d of an organic (carboxylic) acid-enriched stream (average COD of 16 000 mg/L) containing primarily C2 – C5 organic acids, light oils, aldehydes, ketones, cresols and phenols. Together with the Oily sewer water (API) and Stripped Gas Liquor (SGL) process streams, this process effluent is currently treated in ten dedicated activated sludge basins. However, the successful operation of these activated sludge systems has proven to be difficult with low organic loading rates (3.5 kg COD/m3.d) low COD removal efficiencies (<80 %) and high specific air requirements (60 - 75 m3 air/kg CODrem). It is hypothesised that these operational difficulties can be attributed to organic shock loadings, variation in volumetric and hydraulic loadings, as well as variations in the composition of the various process streams being treated. Due to the fact that the Fischer-Tropsch (Synthol) reaction water constitutes 70 % of the COD load on the activated sludge systems, alternative processes to improve the treatment cost and efficiency of the Fischer-Tropsch acid stream are being investigated. Various studies evaluating the aerobic and anaerobic treatment of Fischer-Tropsch reaction water alone in suspended growth wastewater treatment systems have proven unsuccessful. High rate fixed-film processes or biofilm reactors, of which the fluidised-bed reactors are considered to he one of the most effective and promising processes for the treatment of high-strength industrial wastewaters, could he a suitable alternative. The primary aim of this study was to evaluate the suitability of biological fluidised-bed reactors (BFBRs) for the treatment of Fischer-Tropsch reaction water. During this study, the use of aerobic and anaerobic biological fluidised-bed reactors (BFBR), using sand and granular activated carbon (GAC) as support matrices, were evaluated for the treatment of a synthetic effluent analogous to the Fischer-Tropsch reaction water stream. After inoculation, the reactors were operated in batch mode for 10 days at a bed height expansion of 30% and a temperature of 30 ºC to facilitate biofilm formation on the various support matrices. This was followed by continuous operation of the reactors at hydraulic retention times (HRTs) of 2 days. While the COD of the influent and subsequent organic loading rate (OLR) was incrementally increased from 1 600 mg/L to a maximum of 20 000 mg/L and 18 000 mg/L for the aerobic and anaerobic reactors, respectively. Once the maximum influent COD concentration had been achieved the OLR was further increased by decreasing the HRTs of the aerobic and anaerobic reactors to 24h and 8h, and 36h, 24h and 19h, respectively. The dissolved O2 concentration in the main reactor columns of the aerobic reactors was constantly maintained at 0.50 mg/L. Chemical Oxygen Demand (COD) removal efficiencies in excess of 80 % at OLR of up to 30 kg COD/m3.d were achieved in the aerobic BFBRs using both sand and GAC as support matrices. Specific air requirements were calculated to be approximately 35 and 41 m3 air/kg CODrem for the BFBRs using sand and GAC as support matrices, respectively. The oxygen transfer efficiency was calculated to be approximately 5.4 %. At high OLR (> 15 kg COD/m3.d) significant problems were experienced with plugging and subsequent channelling in the BFBR using GAC as support matrix and the reactor had to be backwashed frequently in order to remove excess biomass. Despite these backwash procedures, COD removal efficiencies recovered to previous levels within 24 hours. In contrast, no significant problems were encountered with plug formation and channelling in the BFBR using sand as support matrix. In general the overall reactor performance and COD removal efficiency of the aerobic BFBR using sand as support matrix was more stable and consistent than the BFBR using GAC as support matrix. This BFBR was also more resilient to variations in operational conditions, such as the lowering of the hydraulic retention times and changes in the influent pH. Both aerobic reactors displayed high resilience and COD removal efficiencies in excess of 80 % were achieved during shock loadings. However, both reactors were highly sensitive to changes in pH and any decrease in pH below the pKa values of the volatile fatty acids in the influent (pKa of acetic acid = 4.76) resulted in significant reductions in COD removal efficiencies. Maintenance of reactor pH above 5.0 was thus an essential facet of reactor operation. It has been reported that the VFA/alkalinity ratio can be used to assess the stability of biological reactors. The VFA/alkalinity ratios of the aerobic BFBRs containing sand and GAC as support matrices were stable (VFNalkalinity ratios of < 0.3 - 0.4) until the OLR increased above 10 kg/m3.d. At OLRs higher than 10 kg/m3.d the VFA/alkalinity ratios in the BFBR using sand support matrix increased to 4, above the failure limit value of 0.3 - 0.4. In contrast the VFA/alkalinity ratios of the BFBR using GAC support matrix remained stable until an OLR of 15 kg/m3.d was obtained, where the VFA/alkalinity ratios then increased to > 3. Towards the end of the study when an OLR of approximately 25 kg/m3.d was obtained the VFA/alkalinity ratios of both the BFBRs using sand and GAC as support matrices increased to 9 and 6 respectively, indicating the decrease in reactor stability and acidification of the process. Total solid (TS) and volatile solid (VS) concentrations in the aerobic BFBRs were initially high and decreased over time. While the total suspended solids (TSS) and volatile suspended solids (VSS) concentrations were initially low and increased over time as the OLR was increased, this is thought to be as a result of decreased HRT leading to biomass washout. The anaerobic BFBR using sand as support matrix never stabilised and COD removal efficiency remained very low (< 30 %), possibly due to the high levels of shear forces. Further studies concerning the use of sand as support matrix were subsequently terminated. An average COD removal efficiency of approximately 60 % was achieved in the anaerobic BFBR using GAC as a support matrix at organic loading rates lower than 10 kg COD/m3.d. The removal efficiency gradually decreased to 50 % as organic loading rates were increased to 20 kg COD/m3.d. At OLRs of 20 kg COD/m3.d, the biogas and methane yields of the anaerobic BFBR using GAC as support matrix were determined to be approximately 0.38 m3 biogas/kg CODrem (0.3 m3 biogas/m3reactor vol.d), and 0.20 m3 CH4/kg CODrem (0.23 m3 CH4/m3reactor vol.d), respectively. This value is 57 % of the theoretical maximum methane yield attainable (3.5 m3 CH4/kg CODrem). The methane yield increased as the OLR increased, however, when the OLR reached 8 kg/m3.d the methane yield levelled off and remained constant at approximately 2 m3 CH4/m3reactor vol.d. Although the methane content of the biogas was initially very low (< 30 %), the methane content gradually increased to 60 % at OLRs of 20 kg COD/m3.d. The anaerobic BFBR using GAC as support matrix determined that as the OLR increased (>12 kg/m3.d), the VFA/alkalinity ratio increased to approximately 5, this is indicative of the decrease in stability and acidification of the process. The anaerobic BFBR using GAC as support matrix experienced no problems with plug formation and channelling. This is due to the lower biomass production by anaerobic microorganisms than in the aerobic reactors. The TS and VS concentrations were lower than the aerobic concentrations but followed the same trend of decreasing over time, while the TSS and VSS concentrations increased due to decreased HRTs. The anaerobic BFBR was sensitive to dramatic variations in organic loading rates, pH and COD removal efficiencies decreased significantly after any shock loadings. Compared to the activated sludge systems currently being used for the biological treatment of Fischer-Tropsch reaction water at SASOL SynFuels, Secunda, South Africa, a seven-fold increase in OLR and a 55 % reduction in the specific air requirement was achieved using the aerobic BFBRs. The methane produced could also be used as an alternative source of energy. It is, however, evident that the support matrix has a significant influence on reactor performance. Excellent results were achieved using sand and GAC as support matrices in the aerobic and anaerobic BFBRs, respectively. It is thus recommended that future research be conducted on the optimisation of the use of aerobic and anaerobic BFBRs using these support matrices. Based on the results obtained from this study, it can be concluded that both aerobic and anaerobic treatment of a synthetic effluent analogous to the Fischer-Tropsch reaction water as generated by SASOL in the Fischer-Tropsch Synthol process were successful and that the application of fluidised-bed reactors (attached growth systems) could serve as a feasible alternative technology when compared to the current activated sludge treatment systems (suspended growth) currently used. Keywords: aerobic treatment, anaerobic treatment, biological fluidised-bed reactors, petrochemical effluent, Fischer-Tropsch reaction water, industrial wastewater. / Thesis (M. Omgewingswetenskappe)--North-West University, Potchefstroom Campus, 2004.

Onsite wastewater treatment systems (OWTSs) are a commonly used means of wastewater treatment in the Dickinson Bayou watershed which is located between Houston and Galveston. The Dickinson Bayou is classified as "impaired" by the Texas Commission on Environmental Quality due to high levels of bacteria, specifically E. coli. Failing OWTSs within the bayou's watershed are possible sources for the impairment of the bayou. Conventional OWTSs, comprised of a septic tank and a soil absorption field, rely heavily on soil treatment of effluent. The type of soils is a significant factor in treatment capabilities. In the Dickinson Bayou watershed, soils are primarily composed of clays, which are known to be problematic for conventional systems as they restrict water flow and create perched water tables. These perched water tables may contribute to surface runoff during rainfall events. The HYDRUS modeling software for water and solute flow through variably saturated media was used to simulate OWTSs in the Dickinson Bayou watershed. HYDRUS was used to simulate conventional septic systems with soil absorption fields, aerobic treatment units (ATUs) with spray dispersal systems, and mound systems. Results found that the simulated conventional systems fail due to high water tables and clay soils. However, system failure in the watershed remains uncertain due to lack of field data for validation. The alternative systems mitigate these issues, but ATUs can lead to higher contamination levels without proper maintenance. Therefore, mound systems are the suggested alternative for OWTSs in the watershed.

As the microbrewery industry expands, disposal of brewery wastewater is becoming more of a concern, both for brewery operators and for local municipal wastewater authorities. Brewery wastewater is characterized as containing high strength organics and high variability in both organic and hydraulic loading. This high variability increased the challenge of treating brewery wastewater properly. Therefore, it is significant for optimizing the operation condition for the small-scale wastewater treatment system. This study conducted a batch study and a field study for optimizing a craft brewery on-site wastewater treatment system, which is equipped with two moving bed biofilm reactors (MBBR). In the batch study, a two-factor Box-Wilson central composite design (CCD) was adopted to find optimum biomethane production conditions for the digestion of brewery wastewater with a dairy manure inoculum. The effects of two major influencing factors of temperature (T) (25-49°C) and brewery wastewater concentration (BWC) (2-9 g VS/L) on biochemical methane potential (BMP) (CH₄ yield) and CH₄ maximum production rate (Rmax) were evaluated by applying response surface methodology (RSM). All of the trials presented a high organic removal efficiency with volatile solid (VS) 82-91%, soluble chemical oxygen demand (sCOD) 77-88%, and total chemical oxygen demand (tCOD) between 47% -76%. The experiment result suggested that the first-order kinetic rate constant and biogas content (methane percentage in the biogas) can be affected by the temperature. The mesophilic regime had the highest average rate constant, and the psychrophilic regime rate constant was significantly lower than the mesophilic and thermophile regime. The conditions in the thermophile range present a high variability for the first-order rate constant. The methane ratio in the biogas increased and stabilized by the operation time. Mesophilic and thermophilic regimes obtained a stabile biogas content around 25 days, and the psychrophilic regime spent extra time to stabilized. At the end of the anaerobic digestion, the psychrophilic, mesophilic, and thermophilic regimes had an average methane percentage of 47%,65%, and 67% respectively. Optimum BMP and Rmax were achieved under conditions of 49 °C and BWC of 5g VS/L. Correspondingly, the BMP and Rmax were 141.40 mL CH₄/g VS added and 36.5 mL CH₄/ day, respectively. However, by pursuing stability the preferable operational condition T=35℃ and BWC=5 g/L is recommended, at this condition methane yield is 110.07 CH₄/g VS added and maximum methane daily production is 28.06 CH₄/ day, which is similar to the maximum result. In field study, an on-site brewery wastewater treatment system equipped with two MBBR reactors was evaluated from October 12th, 2018 to February 10th, 2020 in Beau`s All-Natural Brewing Company, Vankleek Hill, Ontario, Canada. The aim of the study was to characterize the wastewater production (flow and organic loading rate), evaluate the operating conditions and performance of the MBBR system, and recommend improvements. Discharge from the brewery is highly variable for both organic and hydraulic loading with flow balancing recommended. The MBBR full-scale reactors operated at relatively stable conditions at a surface area loading rate (SALR) of less than 25 g/m2.d and dissolved oxygen (DO) greater than 2mg/L. Kinetic rate constants for suspended growth and attached growth biomass in the reactors were found to be similar at 0.0764-0.0908 h-1, however, a much larger attached growth mass in the reactors suggests that only a fraction of the attached growth biofilm is active. Effluent recycle was shown to be effective at controlling filamentous bacteria (type-0041) sludge bulking, reducing suspended solid concentration, and sCOD concentration.

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Made available in DSpace on 2015-09-25T12:23:37Z (GMT). No. of bitstreams: 1 Silvia Peres de Castro.pdf: 565210 bytes, checksum: bc1094dba26205895b29d51dc104b086 (MD5) Previous issue date: 2009-08-21 / The increasing global demand for energy and the diversity of manufactured products generates diverse residues that are frequently difficult to treat or degrade. The utilization of petroleum and its derivatives cause environmental damage via oil spillages and effluents generated by diverse processes such as car washes, petrol stations, public transport companies and even industrial kitchens. In this study a biological treatment was used as an alternative to treat these pollutants, which included two basic treatments to remove organic material: an aerobic process namely activated sludge and an anaerobic process, comprising a UASB reactor. The objective of this work was to treat by biological processes, a synthetic effluent derived from petroleum which characterized physico-chemically, as having oily characteristics, to evaluate comparatively the efficiency of organic matter removal via two different processes of biodegradation. The results obtained were submitted to statistical analysis by Box Plots and ANOVA at a significance level of 5%. The experimental work with bench scale activated sludge and UASB reactors was performed at The Experimental Station for the Biological Treatment of Sewage EXTRABES in Campina Grande - PB, using effluents synthesized in the laboratory to feed the reactors at elevated loads of organic matter containing lubricating oil and surfactants. The adopted treatments had significant organic carbon removal efficiencies; with values of 23.7 to 32% for aerobic treatment and 42 to 51% with anaerobic treatment thus demonstrating that UASB treatment was the more efficient process and could be adopted for the treatment of oily and surfactant-containing effluents. / A crescente demanda de energia necessária no mundo e a diversidade de produtos obtidos geram diversos resíduos difíceis de serem tratados. A utilização do petróleo e seus derivados causam danos ambientais, estes vêm desde os derramamentos de petróleo e seus componentes até mesmo de efluentes gerados nos mais diversos processos, como em lava-jatos, postos de combustíveis, empresas de transportes públicos e até mesmo em cozinhas industriais. Neste estudo utilizar-se-á tratamento biológico, como uma alternativa para o tratamento desses poluentes, dentre estes tratamentos tem se dois processos básicos para a remoção de material orgânico que foi estudado: os sistemas de lodos ativados e os reatores UASB. O objetivo desse trabalho foi tratar através de processos biológicos, efluentes sintéticos derivados do petróleo, bem como realizar a caracterização físico-química deste efluente oleoso, e determinar comparativamente a eficiência de remoção da matéria orgânica através de processos de biodegradação biológica. Os resultados obtidos foram submetidos a métodos estatísticos: estatística descritiva de distribuição (Box Plot) e análise de variância (ANOVA) fator único, com nível de significância de 5%. O trabalho experimental foi realizado na Estação Experimental de Tratamentos Biológicos de Esgotos Sanitários EXTRABES, localizado no bairro do Tambor na cidade de Campina Grande PB. Para a realização da pesquisa foram construídos, instalados e monitorados reatores de lodo ativado e UASB em escala de bancada. Os reatores foram alimentados com efluentes sintetizados no laboratório. Com esse procedimento buscou-se tratar biologicamente efluentes com elevada carga orgânica, contendo óleo lubrificante e substâncias surfactantes. Nos tratamentos adotados foi conseguido uma eficiência de remoção significativa, o tratamento aeróbio teve remoções de 23,7 a 32,1%, no tratamento anaeróbio a remoção da matéria orgânica foi de 51 e 42%, o que mostra que o tratamento anaeróbio utilizando o reator UASB teve uma melhor remoção da matéria orgânica, podendo esses tratamentos serem adotados para o tratamento de efluentes oleosos e surfactantes.