This study determined the potential feasibility of surface catalyzed Fenton treatment to remediate soil and groundwater contaminated with bis(2-chloroethyl ether (BCEE), bis(2-chloroethoxy) methane (BCEM), and 1,2-dichloroethane (1,2-DCA) among other contaminants. Parameters that affect the contaminant loss rate such as pH, hydrogen peroxide concentration and solid/water ratio were systematically evaluated. Batch reactors were set-up utilizing either contaminated or uncontaminated soil that was mixed with synthetic groundwater containing the contaminants of interest. The results show an increase in contaminant reduction with a decrease in pH, an increase in hydrogen peroxide concentration, or an increase in the solid/water ratio. For the same set of conditions, contaminant reduction was greater for systems utilizing contaminated soil as compared to the systems containing uncontaminated soil. In addition, specific oxygen uptake rates were measured for an activated sludge exposed to different dilutions of untreated and surface catalyzed Fenton treated water to evaluate whether the residual BCEE, BCEM, and 1,2 DCA as well as their oxidation by products were potentially inhibitory or can potentially serve as a substrate for the activated sludge. The measured specific oxygen uptake rates show that the surface catalyzed Fenton treatment enhanced the biodegradability of the contaminated groundwater and served as a substrate for the activated sludge. / Master of Science

During ferrochrome (FeCr) production, three types of generic chromium (Cr) containing wastes are generated, i.e. slag, bag filter dust (BFD) and venturi sludge. The loss of these Cr units contributes significantly to the loss in revenue for FeCr producers. In this study, the liberation of Cr units was investigated utilising two case study waste materials, i.e. BFD from a semi-closed submerged arc furnace (SAF) operating on acid slag and the ultrafine fraction of slag (UFS) originating from a smelter operating with both open and closed SAFs on acid slag. A detailed material characterisation was conducted for both case study materials, which included particle size distribution, chemical composition, chemical surface composition and crystalline content. Cr liberation was achieved utilising two methods, i.e. aqueous ozonation and the advanced oxidation method. Various advanced oxidation processes could be applied. However, the advanced oxidation processes considered in this study was the use of gaseous ozone (O3) in combination with hydrogen peroxide (H2O2). Controlling parameters such as the influence of pH, ozonation contact time, waste material solid loading, gaseous O3 concentration and temperature on Cr liberation were investigated for the aqueous ozonation process. The influence of pH, volume H2O2 added and the method of H2O2 addition were considered for the advanced oxidation process. Results indicated that with aqueous ozonation, limited Cr liberation could be achieved. The maximum Cr liberation achieved was only 4.2% for BFD by varying the process controlling parameters. The Cr liberation for UFS was significantly lower than that of the BFD. The difference in the results for the two waste materials was attributed to the difference in characteristics of the materials. The Cr content in BFD was mostly related to chromite and/or altered chromite particles, while the Cr content of the UFS was mostly related to FeCr particles. It is possible that the Cr(III) present in the chromite and/or partially altered chromite might be more susceptible to oxidation to Cr(VI) than the metallic Cr(0) present in the FeCr. During ozonation, aqueous O3 spontaneously decomposes to form hydroxyl (OH•) radicals, which are very strong oxidants in water. The above-mentioned Cr liberation observed was related to the formation of the OH• radicals during the spontaneous decomposition of aqueous O3. This was indicated especially by enhanced Cr liberation at higher pH values, which was attributed to the acceleration of the spontaneous decomposition to OH• radicals at higher pH levels. The advanced oxidation method gave significantly higher Cr liberation results for both case study materials considered, achieving Cr liberations of more than 21%. The advance oxidation processes improve normal oxidation methods. In this study, the H2O2 used in combination with O3 enhanced the formation of the OH• radicals that are responsible for the oxidation of Cr. The Cr liberation levels achieved are possibly not high enough to be feasible for industrial purposes. However, a further investigation of the advanced oxidation process could optimise the process to yield even higher Cr liberation. / MSc (Chemistry), North-West University, Potchefstroom Campus, 2014

During ferrochrome (FeCr) production, three types of generic chromium (Cr) containing wastes are generated, i.e. slag, bag filter dust (BFD) and venturi sludge. The loss of these Cr units contributes significantly to the loss in revenue for FeCr producers. In this study, the liberation of Cr units was investigated utilising two case study waste materials, i.e. BFD from a semi-closed submerged arc furnace (SAF) operating on acid slag and the ultrafine fraction of slag (UFS) originating from a smelter operating with both open and closed SAFs on acid slag. A detailed material characterisation was conducted for both case study materials, which included particle size distribution, chemical composition, chemical surface composition and crystalline content. Cr liberation was achieved utilising two methods, i.e. aqueous ozonation and the advanced oxidation method. Various advanced oxidation processes could be applied. However, the advanced oxidation processes considered in this study was the use of gaseous ozone (O3) in combination with hydrogen peroxide (H2O2). Controlling parameters such as the influence of pH, ozonation contact time, waste material solid loading, gaseous O3 concentration and temperature on Cr liberation were investigated for the aqueous ozonation process. The influence of pH, volume H2O2 added and the method of H2O2 addition were considered for the advanced oxidation process. Results indicated that with aqueous ozonation, limited Cr liberation could be achieved. The maximum Cr liberation achieved was only 4.2% for BFD by varying the process controlling parameters. The Cr liberation for UFS was significantly lower than that of the BFD. The difference in the results for the two waste materials was attributed to the difference in characteristics of the materials. The Cr content in BFD was mostly related to chromite and/or altered chromite particles, while the Cr content of the UFS was mostly related to FeCr particles. It is possible that the Cr(III) present in the chromite and/or partially altered chromite might be more susceptible to oxidation to Cr(VI) than the metallic Cr(0) present in the FeCr. During ozonation, aqueous O3 spontaneously decomposes to form hydroxyl (OH•) radicals, which are very strong oxidants in water. The above-mentioned Cr liberation observed was related to the formation of the OH• radicals during the spontaneous decomposition of aqueous O3. This was indicated especially by enhanced Cr liberation at higher pH values, which was attributed to the acceleration of the spontaneous decomposition to OH• radicals at higher pH levels. The advanced oxidation method gave significantly higher Cr liberation results for both case study materials considered, achieving Cr liberations of more than 21%. The advance oxidation processes improve normal oxidation methods. In this study, the H2O2 used in combination with O3 enhanced the formation of the OH• radicals that are responsible for the oxidation of Cr. The Cr liberation levels achieved are possibly not high enough to be feasible for industrial purposes. However, a further investigation of the advanced oxidation process could optimise the process to yield even higher Cr liberation. / MSc (Chemistry), North-West University, Potchefstroom Campus, 2014

This research involved an investigation of the application and reaction mechanisms of UV/H₂O₂ for the simultaneous removal of regulated halogenated disinfection byproducts (DBPs) and odorous aldehydic algal byproducts in the presence of geosmin and 2-methylisoborneol, which are earthy-musty odorants that commonly occur in drinking water. UV/H₂O₂ is an expensive advanced oxidation process that is used to successfully control geosmin and 2-methylisoborneol. The aqueous oxidation of odorous aldehydes and halogenated DPBs were compared to that of the earthy-musty odorants and the changes to the sensory properties of the drinking water were examined. Geosmin, 2-methylisoborneol, heptadienal, decadienal, and nonadienal, hexanal, and the two most prevalent classes of DBPs, trihalomethanes (THMs) and haloacetic acids (HAAs) were oxidized by UV photolysis alone and the UV/H₂O₂ process with 6 mg/L H₂O₂ and realistic ng/l to μg/L concentrations of the test compounds. The di-, and tri-brominated THMs and HAAs were substantially (80-99%) removed by direct UV photolysis mechanism at the same UV/H₂O₂ dose required for removing 95% of geosmin and 65% of 2-methylisoborneol with faster reaction rates for the more bromine substituted compounds. The C-Br bond cleavage is the first step of brominated HAAs degradation by UV photolysis, and followed by either of two second steps: reaction with oxygen producing peroxyl radical or interaction with water molecule causing O-H insertion/H-Br elimination. Trichloromethane and mono-, di-, and tri-chlorinated HAAs were not substantially removed under the same conditions used for the brominated compounds. The principal removal mechanism was by the reaction with hydroxyl radical for the UV/H₂O₂ process. The second order reaction rate constants were on the order of 10⁶ - 10⁸ M⁻¹ s⁻¹ with faster reaction rates for the less chlorine substituted compounds. Based on the reaction rates, hydrogen and halogen ion balance, and isotope effect, both hydrogen abstraction and electron transfer reaction were involved in the first steps of the chlorinated HAA degradation. Three odorous aldehydes - heptadienal, decadienal, and nonadienal - were removed faster than geosmin or 2-methylisoborneol, and direct UV photolysis was the principal reaction mechanism for the removal of these unsaturated aldehydes. Hexanal was poorly removed. In sensory tests, new odors such as sweet or chalky odors were produced while the concentration and initial odor intensity of these fishy/grassy-smelling aldehydes were reduced with increasing exposure time to UV/H₂O₂. Carbonyl compounds were detected as products of the UV photolysis of nonadienal. These carbonyls were not removed by further UV irradiation, which was thought to be partially related with production of new odors. The results indicate that the UV/H₂O₂ is effective to control both odorous compounds and brominated DBPs. This process can be seasonally applied to control both contaminants especially, in the warm summer when both odorants and DBPs have their higher concentrations. Removal of brominated DBPs can be a significant addition to water utilities that have difficulty in meeting regulatory levels for these highly toxic compounds. The result on the removal of odorous aldehydes indicate that new types of odors were produced from the oxidation of odorous aldehydes suggesting sensory test coupled with chemical analysis should be considered in designing oxidation process to control recalcitrant odorants. / Ph. D.

O lodo gerado em processos de galvanoplastia é classificado pela ABNT NBR 10.004/04 como perigoso (classe I). Na literatura encontram-se poucos estudos referentes à recuperação do cromo presente no lodo gerado em sistemas de tratamento de efluentes de indústrias de galvanoplastia. Neste sentido, o presente estudo avaliou a remoção do cromo presente no lodo de galvanoplastia por meio de dois processos, visando avaliar à eficiência técnica e a viabilidade econômica de ambos. O Processo 1 consistiu na remoção do cálcio utilizando o ácido cítrico, seguida de lixiviação ácida. Na etapa de oxidação, variou-se a temperatura em 40ºC, 60ºC e 80ºC e no tempo de 30, 60 e 90 minutos, tendo em vista que a eficiência do processo de oxidação depende da temperatura e tempo. Nesta etapa do processo as concentrações de peroxido de hidrogênio (H2O2) utilizadas foram de 1,50, 3,00 e 4,50 mol.L-1. O Processo 2 realizou a oxidação do cromo sem efetuar as etapas de extração do cálcio e a lixiviação ácida. A oxidação do cromo ocorreu pelo mesmo método apresentado no Processo 1. A caracterização elementar da amostra determinou que o principal elemento constituinte do lodo é o cálcio (20,05% em massa), e que dentre os metais pesados destacam-se o cromo e o níquel (6,52% e 4,33% em massa, respectivamente). A maior eficiência de remoção do cálcio foi obtida na razão mássica de 8,00 (ácido cítrico/hidróxido de cálcio), com 51,76% em massa, seguida pela razão mássica de 5,50 com 36,75% em massa e 2,50 com 24,83% em massa. O melhor resultado de oxidação do cromo no Processo 1 foi obtido com tempo de 30 minutos, temperatura de 60ºC e concentração de peroxido de hidrogênio de 3,00 mol.L-1, com eficiência de 41,09% em massa. No Processo 2, obteve-se a remoção de 37,96% em massa de cromo a temperatura de 80ºC, por uma hora e 3,00 mol.L-1 de peróxido de hidrogênio. Avaliando os custos para remoção do cromo dos dois processos, determinou-se que o Processo 1 foi mais oneroso que o 2, porém ambos não apresentaram viabilidade econômica para aplicação em escala industrial. Nos dois processos efetuou-se a oxidação do cromo presente no lodo de galvanoplastia, permitindo a sua remoção parcial neste resíduo. Com isso obtiveram-se ganhos ambientais, pela diminuição deste elemento no resíduo de galvanoplastia, que na maioria das vezes é disposto em aterros classe I, gerando um passivo ambiental. / The sludge generated in electroplating processes is classified by NBR 10.004/04 as a hazardous material (class I). In the literature, few studies report the recovery of chromium present in the electroplating sludge generated in the industries. In this sense, the present study conducted the removal of chromium in the electroplating sludge through two different processes, aiming to evaluate their efficiency and economic viability. The first process removed calcium through the use of citric acid being performed by varying the ratio of citric acid/calcium hydroxide (2.5, 5.5 and 8.0). Then, were performed the leaching of the samples. According to the literature, the efficiency of the oxidation process varies depending on the reaction temperature, time and concentration of hydrogen peroxide. For this reason, samples were heated to a temperature ranging from 40°C, 60°C and 80°C. Also, were conducted variations in the concentrations of hydrogen peroxide (1.5, 3.0 and 4.5 mol.L-1) and reaction time (30, 60 and 90 minutes). The second Process consisted in the chrome recovery by using the galvanic sludge without removal of the calcium and acid leaching. The chrome oxidation occurred by the same method shown in Process 1. Elemental characterization of the samples determined that the primary sludge constituent was calcium (20.05% by weight), and in terms of heavy metals, the chromium and the nickel (6.52% and 4.33% by mass, respectively). Most of calcium removal efficiency was obtained at a rate of 8 with 51.76% by mass, then the ratio of 5.50 to 36.75% by mass and 2.50 to 24.83% by mass. The best oxidation result of chromium in Process 1 was obtained using a time of 30 minutes, 60°C and hydrogen peroxide concentration of 3 mol.l-1, with 41.09 wt% efficiency. In Process 2 was obtained the removal of 37.96% by mass of chromium temperature of 80°C, for one hour and 3,00 mol.l-1 of hydrogen peroxide. Evaluating the costs for chrome removal of the two processes was determined that the Process 1 was more costly than 2, but both showed no economic feasibility for implementation on an industrial scale. However, in both cases occurred the oxidation of chromium present in the electroplating sludge, allowing its removal from the residue. Thus, environmental gains have been achieved by the reduction of this element in electroplating waste, which mostly is intended for landfill class I, generating an environmental liability.

No processo UV/H2O2, oxidar o substrato a CO2 e água resulta em um elevado consumo de H2O2. Então, esse processo tem sido proposto como um pré-tratamento para reduzir a toxicidade a níveis seguros para o tratamento biológico posterior. Por essa razão, é necessário estudar o progresso da reação, pois a toxicidade de alguns intermediários formados durante a oxidação pode ser mais elevada que a do composto inicial. Neste trabalho, os experimentos foram realizados em um reator tubular fotoquímico, contendo em seu eixo uma lâmpada de vapor de mercúrio de baixa pressão, conectado a um tanque de recirculação. O processo UV/H 2O2 é aplicado no tratamento de água contendo fenol (50500mg C.L-1). Os resultados demonstraram que o principal produto da oxidação primária é o catecol, indicando que a hidroxilação ocorre predominantemente na posição orto. A abertura do anel aromático leva à formação de ácidos orgânicos, o que explica a diminuição do pH durante a reação. Foram identificados os seguintes ácidos: fórmico, oxálico, maleico e malônico. Na etapa seguinte desse trabalho, dois modelos cinéticos foram desenvolvidos. Os modelos foram baseados nas reações químicas e fotoquímicas iniciadas pelos radicais hidroxila gerados pela fotólise do peróxido de hidrogênio. Foram utilizados os valores encontrados na literatura para os parâmetros fotoquímicos e constantes cinéticas das reações fotoquímicas. Os resultados experimentais foram utilizados para estimar as constantes cinéticas das reações que envolvem os compostos aromáticos. No primeiro modelo foram contempladas todas as reações fotoquímicas envolvidas e, no segundo, apenas as consideradas mais significantes. Os resultados das simulações considerando os parâmetros ajustados mostraram uma melhor concordância com os dados experimentais para o primeiro modelo. As constantes cinéticas deste modelo para as reações nas quais o fenol é oxidado a catecol (k14) e hidroquinona (k15) foram 2,60x108L.mol-1.s-1 e 1,03x108L.mol-1.s-1, respectivamente. As constantes cinéticas para a oxidação do catecol (k17) e hidroquinona (k18) encontradas foram 1,41x108L.mol-1.s-1 e 2,02x108L.mol-1.s-1, respectivamente. Também foi observada elevada correlação entre as constantes k14 e k17 e entre k15 e k18. / In the UV/H2O2 process, the oxidation of the substrate to CO2 and water results in high H2O2 consumption. Due to this fact the process has been proposed as a pretreatment to reduce toxicity to safe levels prior to biological treatment. Thus, it is necessary to study the reaction progress because some intermediate compounds may be more toxic than the initial compound. In the present study experiments were carried out in a lab-scale tubular photochemical reactor with a low-pressure mercury vapor lamp placed in its axis, connected to a recirculation tank. The UV/H2O2 process was applied to the degradation of an aqueous solution containing phenol as a model pollutant (concentration range: 50-500mg.L-1). The experimental results indicated that orto-hydroxylation (catechol formation) was predominant. The cleavage of the aromatic ring resulted in the production of organic acids, which caused the pH decrease over the reaction time. The following acids were detected: formic, oxalic, maleic and malonic. The experimental results were used to estimate kinetic rate constants for the reactions involving aromatic compounds according to two kinetic models based on chemical and photochemical reactions, initiated by hydrogen peroxide photolysis to produce hydroxyl radical. Numerical values of chemical reaction rate constants and photochemical parameters were taken from literature. The first model considered all photochemical while the second model considered the most significant ones. The parameter fitting results showed better agreement with experimental values based on the first model. The resulting values for the rate constants according to this model were as follows: 2.60x108L.mol-1.s-1 for phenol oxidation to catechol, and 1.03x108L.mol-1.s-1 for phenol oxidation to hydroquinone by hydrogen peroxide. The reaction rate constants for the oxidation of catechol, and hydroquinone by hydrogen peroxide are 1.41x108L.mol-1.s-1 and 2.01x108L.mol-1.s-1, respectively. A high correlation was observed between constants k14 and k17, and between k15 and k18.

O descarte de embalagens vazias dos agrotóxicos sem fiscalização e controle pode gerar problemas ambientais, afetando a saúde do homem, dos animais e da vida silvestre. Entre os inseticidas comerciais, o clorpirifós tem uma importância significativa por ser amplamente utilizado e persistente no ambiente. O ataque do radical hidroxila, OH é o processo mais eficiente de oxidação química de compostos orgânicos. A degradação de clorpirifós induzida por radiação gama foi estudada em amostras de água e em embalagens de polietileno. Embalagens de polietileno de alta densidade coextrudada em camadas sobrepostas, COEX, contaminadas com clorpirifós foram irradiadas com radiação gama em fonte de Co-60 do tipo \"Gammacell\" e do tipo \"irradiador de grande porte\". As análises de clorpirifós e solventes, assim como dos subprodutos formados foram realizadas por cromatografia a gás associada à espectrometria de massa. A radiação ionizante se mostrou uma técnica eficiente na degradação do inseticida clorpirifós nestas embalagens. / The discharge of empty plastic packaging of pesticides can be an environmental concern causing problems to human health, animals and plants if done without inspection and monitoring. Among the commercial pesticides, chlorpyrifos has significant importance because of its wide distribution and extensive use and persistence. The hydroxil OH atack is the most efficient process of chemical oxidation. The radiation-induced degradation of chlorpyfifos in liquid samples and in polyethylene pack was studied by gamma-radiolysis. Packaging of high density polyethylene tree layer coextruded, named COEX, and water samples contaminated with chlorpyrifos, were irradiated using both, a multipurpose Co-60 gamma irradiator and a gamma source with 5,000 Ci total activity, Gammacell type. The chemical analysis of the chlorpirifos and by-products were made using a gas chromatography associated to the mass spectrometry. Gamma radiation was efficient for removing chlorpyrifós from the plastic packaging in all studied cases.

A presença de produtos farmacêuticos no meio ambiente é uma questão emergente, devido à crescente resistência bacteriana. As tecnologias utilizadas em instalações de tratamento de água não são eficientes para remover todos os resíduos farmacêuticos e os efeitos dessas substâncias não são bem conhecidos. No presente trabalho, estudou-se a degradação do antibiótico sulfametoxazol (SMX) por fotólise. O SMX é uma sulfonamida, um dos grupos de antibióticos mais utilizados. A fotodegradação de SMX em solução aquosa foi realizada por radiação UVC, sendo o composto transformado por meio de absorção de fótons de comprimento de onda igual a 254 nm. Os experimentos foram conduzidos em um reator fotoquímico anular tubular feito de vidro Pirex (volume irradiado de 3,9 L). A irradiação foi feita por uma lâmpada de mercúrio de baixa pressão de 36 W posicionada ao longo do eixo do reator. Utilizaram-se 5,5 L de solução aquosa do antibiótico (10-50 mg/L). Os efeitos das concentrações iniciais de SMX e do pH (5, 7 ou 9) foram estudados a partir de um projeto experimental Doehlert. Os resultados indicaram remoções de SMX superiores a 99% em até 30 minutos de exposição à radiação UVC. A análise estatística dos resultados em termos do tempo necessário para redução de 50% da concentração inicial de SMX e da taxa inicial de degradação confirmou que para maior quantidade inicial do antibiótico é possível observar que o pH interfere na resposta, indicando que a fotólise do SMX é mais lenta em meio básico. Por outro lado, para concentrações iniciais mais baixas, não é possível afirmar se o pH interfere ou não na velocidade de degradação de SMX, já que esta ocorre muito rapidamente. Os compostos resultantes da degradação do SMX mostraram-se recalcitrantes, obtendo-se remoções de COT menores que 7%. Medidas de toxicidade baseadas na inibição da luminescência da bactéria Vibrio fischeri, segundo o método Microtox 500®, indicaram aumento de toxicidade das soluções aquosas após irradiação. Além disso, bioensaios respirométricos sugeriram que os produtos gerados na degradação são mais favoráveis à oxidação em sistemas biológicos de tratamento. / The presence of pharmaceuticals in the environment is an emerging issue due to the increasing bacterial resistance. The technologies used in sewage and wastewater treatment plants are not efficient to remove all pharmaceutical residues and the effect of these substances is not well known. In this work, the degradation of the antibiotic sulfamethoxazole (SMX) by photolysis has been studied. SMX belongs to the sulfonamides group, one of the first groups of antibiotics used. The photodegradation of SMX in aqueous solution was carried out by UV radiation, in which the target compound is transformed by absorbing photons with wavelength 254 nm. The experiments were carried out in an annular photochemical reactor made of Pyrex glass (irradiated volume of 3.9 L). The irradiation was provided by a 36 W low-pressure mercury vapor lamp set along the reactor axis. A total volume of 5.5 L of aqueous solution (10-50 mg/L) was used. The effects of SMX initial concentration and pH (5, 7 or 9) were studied according to a Doehlert experimental design. The results showed SMX removals greater than 99% after 30 minutes of UVC irradiation. Statistical analysis of the results in terms of the time needed to remove 50% of SMX initial concentration and the initial degradation rate showed that pH affects the response for higher initial amounts of antibiotic, showing that SMX photolysis is slower in basic medium. On the other hand, for lower initial concentrations, it is not possible to confirm wether pH affects the removal rate or not, because the decrease of SMX concentration is very fast. The compounds resulting from SMX degradation were shown to be recalcitrant, with TOC removals not greater than 7%. Bioassays based on the inhibition of Vibrio fischeri luminescence showed an increase of the toxicity of irradiated aqueous solutions. Moreover, respirometric bioassays suggested that the degradation products produced by SMX degradation are more favorable to oxidation in biological treatment systems.

O efluente fenólico em estudo apresenta a relação DBO5/DQO (Demanda Bioquímica de Oxigênio/ Demanda Química de Oxigênio) igual a 0,15, ou seja caracteriza-se por ser um efluente não biodegradável. No tratamento inicial do efluente utilizou-se ozônio, na presença do sal de ferro II proveniente da solução de sulfato ferroso heptaidratado 0,82 mol. L-1 e do peróxido de hidrogênio , que possui a finalidade catalítica na formação dos radicais hidroxilas, com alto poder de oxidação da matéria orgânica. Nesta etapa foi estudado a união dos processos oxidativos O3/UV e Foto-Fenton, Foram tratados 3 L do efluente fenólico in natura em um reator fotocatalítico com lâmpada ultravioleta. Em todos os experimentos o pH e a temperatura do meio reacional foram controlados. Os experimentos foram executados segundo um planejamento de Taguchi L16, no qual a variável entrada de maior importância para a degradação da matéria orgânica foi o peróxido de hidrogênio. As variáveis respostas analisadas foram a concentração do Carbono Orgânico Total, Demanda Química de Oxigênio e Fenóis Totais. No planejamento de Taguchi L16 foram selecionadas as variáveis significativas para o processo de degradação do efluente fenólico, a fim de serem otimizadas através do Método de Superfície de Resposta (MSR Foto-Fenton e O3/UV). O método de otimização MSR Foto-Fenton foi eficiente na degradação do composto fenólico, sendo assim a melhor condição experimental da planilha de otimização foi a de número 10 e corresponde a uma redução de COT= 54,68%, DQO=78,73% e Fenois Totais= 98,1%. Os parâmetros controlados do processo para essa condição foram: pH=3, temperatura de 30 ºC, potência ultravioleta de 28 W e reagente Fenton (H2O2= 48,3g e Fe+2 =5,95g), que corresponde a relação mássica H2O2 /Fe+2 igual a 8. / The phenolic effluent in this study has the rate DBO5/DQO (Biochemical Oxygen Demand / Biochemical Oxygen Demand) equal to 0.15, which is characterized by an effluent to be non-biodegradable. In the initial treatment of phenol was used ozone in the presence of iron salt II from the solution of ferrous sulfate heptahydrate 0.82 mol. L-1 and hydrogen peroxide, which has the purpose in the catalytic formation of hydroxyl radicals with high oxidation power of organic matter. In this stage, was studied the union of the oxidative process O3/UV and Photo-Fenton. The effluent was treated about 3 L about in a photocatalytic reactor with UV lamp. In all experiments, the pH and temperature of the reaction medium were control. The experiments are being carried out to a Taguchi L16 design, in which the input variable of greatest importance to the degradation of organic matter was hydrogen peroxide. The response variable analyzed was given by the concentration of Total Organic Carbon (TOC) and Chemical Oxygen Demand (COD) and Total Phenols (FT). In planning Taguchi L16 significant variables were selected for the degradation process of phenolic wastewater in with purpose of to be optimized by Response Surface Method (RSM Photo-Fenton and O3/UV). The optimization method was efficient photo-Fenton degradation of phenolic compound, so the best experimental condition spreadsheet optimization was the number 10 and corresponds to a reduction of TOC = 54.68%, COD = 78,73% and Total Phenols= 98.1%. The controlled process parameters for this condition were: pH = 3, temperature of 30 ° C, power of 28 W ultraviolet and Fenton reagent (H2O2= 48,3g and Fe+2 = 5,95g), corresponding to mass ratio H2O2 / Fe +2 = 8.

Submitted by JOSIANE SANTOS DE OLIVEIRA (josianeso) on 2017-05-25T11:43:55Z No. of bitstreams: 1 Alisson Schons_.pdf: 2733792 bytes, checksum: 704c4ce2631dfdbe7af1fc3c3e324404 (MD5) / Made available in DSpace on 2017-05-25T11:43:56Z (GMT). No. of bitstreams: 1 Alisson Schons_.pdf: 2733792 bytes, checksum: 704c4ce2631dfdbe7af1fc3c3e324404 (MD5) Previous issue date: 2016-02-24 / CAPES - Coordenação de Aperfeiçoamento de Pessoal de Nível Superior / UNISINOS - Universidade do Vale do Rio dos Sinos / O lixiviado de aterro sanitário tem se caracterizado pela alta concentração de matéria orgânica recalcitrante, nitrogênio amoniacal e compostos tóxicos. Compostos orgânicos recalcitrantes são raramente removidos por processos tradicionais de tratamentos de efluentes, o que dificulta o atendimento aos padrões de lançamento de efluentes. Da mesma forma, o descarte do esgoto doméstico gerado pelas comunidades precisa também de tratamentos prévios para não impactar o meio ambiente. Devido às características do esgoto doméstico, com baixas concentrações de matéria orgânica carbonácea e cor em relação ao lixiviado, vem permitindo que o tratamento combinado desses efluentes seja uma alternativa viável. Diante desse quadro, este trabalho visou à avaliação do tratamento combinado de esgoto doméstico da estação de tratamento de efluentes (ETE) da Unisinos e lixiviado bruto do aterro sanitário de São Leopoldo, utilizando ozônio (O3) como agente oxidante. Os efluentes foram tratados na unidade experimental composta por um reservatório com capacidade de até 500L e um reator cilíndrico de PVC com 250 mm de diâmetro e 2,20 m de altura, operando com fluxo ascencional, totalizando um volume de trabalho de 108 L e preenchido em 2/3 do seu volume total com Anel Pall de 1,5”. Realizaram-se três ensaios em bateladas, com duração de cinco horas e três ensaios com duração de duas horas, com diferentes produções de O3 de 8,9; 9,6 e 10,5 g de O3.h-1, aplicados à mistura de 2% de lixiviado de aterro sanitário (LAS) ao esgoto doméstico (2 L de LAS e 158 L de esgoto). Cada ensaio foi realizado em duplicata, sendo monitorados os seguintes parâmetros: Demanda Química de Oxigênio, Demanda Bioquímica de Oxigênio, Cor Aparente e Verdadeira, Turbidez, pH e calculada as taxas de utilização e de perda de O3. Os resultados evidenciaram que o tratamento por O3 pode ser uma alternativa de pré-tratamento de efluentes, obtendo remoções médias de DQO, DBO, CA, CV e Turbidez de até 46%, 51%, 86%, 86% e 81% respectivamente em cinco horas de ensaio e remoções médias de até 23%, 48%, 78%, 76% e 58% respectivamente em duas horas de ensaio. As maiores taxas de remoções foram alcançadas nos ensaios com maiores vazões de O2 e produções de O3 e nas duas primeiras horas de ensaio. Só foi possível o atendimento aos padrões de lançamentos de efluentes exigidos pela legislação vigente, nos ensaios com duração de cinco horas e com a maior produção de O3 e vazão de O2. O sistema de tratamento também contribuiu para uma melhora na biodegradabilidade do efluente se analisada a relação DBO/DQO e cor. Quanto as taxas de utilização e de perda de O3, verificou-se que a maior quantidade consumida de O3, ocorreu para os parâmetros indicativos de matéria orgânica e para os ensaios com a menor produção de O3. / Landfill leachate has been characterized by the high concentration of recalcitrant organic matter, ammoniacal nitrogen and toxic compounds. Recalcitrant organic compounds are rarely removed by traditional effluent treatment processes. In addition, the treatment of the leachate is colloquial to meet the discharge standards of the effluent. Likewise, the domestic sewage disposal generated by the communities also needs previous treatments to avoid impacts on the environment. Due to the characteristics of domestic sewage, with low concentrations of organic carbon in relation to the leachate, it has allowed the combined treatment of these effluents to be a viable alternative. In view of this situation, this work had the objective of evaluating the combined treatment of domestic sewage of (ETP) and the raw leachate of the San Leopoldo landfill using ozone (O3) as an oxidizing agent. Three batch trials were carried out with a scheduled duration of five hours and three trials lasting two hours, with different yields of O3 of 8.9, 9.6 and 10.5 g of O3.h-1, applied to the mixture Of 2% of landfill leachate) For domestic sewage (2L of LAS and 158L of sewage). Each assay was performed in duplicate and the following parameters were monitored: Oxygen Chemical Demand, Biochemical Oxygen Demand, Apparent and True Color, Turbidity, pH and calculated O3 utilization and loss rates. The results showed that the treatment with O3 can be an excellent alternative of pretreatment of effluents, obtaining average removals of COD, BOD, CA, CV and Turbidity of up to 46%, 51%, 86%, 86% and 81 % Respectively. Average test and removal hours of up to 23%, 48%, 78%, 76% and 58%, respectively, in two hours of testing. The highest removal rates were obtained in the tests with higher flows of O2 and yields of O3 and in the first two hours of the test. It was only possible to meet the effluent release standards required by current legislation, in trials with a duration of five hours and with the highest production of O3 and O2. The treatment system also contributed to an improvement in the biodegradability of the effluent if the BOD/COD ratio was analyzed. As for the rates of use and loss of O3, it was verified that the highest amount of O3 occurred for the parameters indicative of organic matter and for the tests with lower production of O3. The higher the O3 production, the higher the O3 loss and the greater oxidant loss may have been due to volatilization in the effluent accumulation reservoir, since there was no gas loss due to Off-gas and the method used Not Detected The residual ozone.