The activated sludge process is one of the most commonly employed domestic and industrial waste treatment process. Different types of mathematical models have been proposed for design and operation of this process, most of which do not consider the relationship between the sludge settling characteristics and the aeration unit performance. This project studies the validity of a model developed by La Motta (2004b) which links the operating parameters of an activated sludge system and the classical limiting flux sludge settling theory. Favorable results were obtained demonstrating that the model predicts very similar values of the parameters of the system in comparison with the parameters observed in an activated sludge pilot plant that is located within installations of the Marrero Wastewater Treatment Plant, New Orleans, Louisiana. This research also demonstrated that the model is a helpful tool for the design and operation of an activated sludge system.

La Digestion Anaérobie (DA), ou méthanisation, est un procédé qui permet le traitement de déchets organiques et la production d’énergie renouvelable sous forme de biogaz. La DA par voie sèche permet en particulier la valorisation de substrats solides, offrant plusieurs possibilités aux traitements de résidus d’origine agricole tels les fumiers, des substrats constitués d’un mélange de paille, fèces et urine accumulés dans les litières des étables. Parmi les technologies disponibles en méthanisation, les « leach-bed reactors » (LBRs), constituent une option valide mais toutefois peu connue et peu développée soit au niveau scientifique qu’industriel.Dans le but d’optimiser ce procédé, plusieurs problématiques ont été affrontées : (i) la caractérisation bio-physico-chimique du fumier et du potentiel énergétique exprimé dans un LBR; (ii) l’optimisation de l’inoculation des réacteurs et de la température de digestion ; (iii) la co-digestion du fumier avec un substrat facilement biodégradable et la problématique reliées à la gestion des acides gras volatiles (AGVs) ainsi produits.Les résultats montrent que le fumier est un substrat lentement biodégradable qui nécessite un long temps de digestion. Cependant, il s’agit d’un déchet agricole adapté à la valorisation par méthanisation et dont les rendements de dégradation et de production de méthane en LBRs sont intéressants industriellement. Ce substrat est par conséquent une ressource organique précieuse dans le contexte agricole.Il a été montré que le fumier bovin contient une population méthanogène active capable de démarrer un procédé de digestion anaérobie efficacement sans l’ajout d’un inoculum externe spécifique, autant en mode mésophile que thermophile. Une analyse économique a démontré que cette propriété peut être exploitée afin de diminuer les coûts d’investissement initiaux d’un projet à l’échelle industrielle, en favorisant de cette manière le développement de la filière. De plus, les résultats montrent que pour la digestion du fumier en LBRs le mode thermophile ne comporte aucun intérêt par rapport à la production finale de méthane (qui est similaire pour les deux régimes) et que, au contraire, la valorisation par cogénération du méthane produit en thermophile diminue le rendement de production électrique surtout à cause d’une production de méthane très importante en début de digestion. Le régime mésophile parait donc être le mode de fonctionnement le plus adapté dans ce contexte.Enfin, le rôle joué par la percolation du lixiviat sur la mobilisation des AGV accumulés dans la fraction solide a été mis en lumière dans un réacteur de co-digestion traitant une fraction de lentement biodégradable (le fumier) et une fraction facilement biodégradable. Une stratégie a été développée afin d’étudier le problème de l’extraction et de la consommation des AGV dans le but d’améliorer le rendement global du procédé.Pour conclure, ce travail a permis d’optimiser certains paramètres fondamentaux dans la gestion d’un LBR. Cette technologie s’est révélée efficace dans le traitement du fumier, autant en mono-digestion qu’en co-digestion avec un substrat facilement biodégradable. Ces recherches montrent que l’utilisation des LBR est appropriée au contexte agricole et que la modification des paramètres de contrôle permet à ce procédé de répondre efficacement aux problématiques du terrain. Ce travail représente une avancée significative vers la compréhension et le développement des LBRs pour le traitement des résidus agricole et, plus globalement, des énergies renouvelables mobilisant des biomasses agricoles / Anaerobic Digestion (AD) is a process which allows the treatment of organic waste and the production of renewable energy. In particular, dry AD allows the treatment of solid organic substrates, offering several possibilities to the enhancement of agricultural waste such as spent livestock bedding (a mixture of straw, faeces and urine). Among the available biotechnologies in AD, leach-bed reactor (LBRs) is a promising but yet poorly known process both at scientific and industrial level.In order to develop this process, several issues have been studied: (i) the bio-physico-chemical characterization of spent animal bedding and its digestion potential in LBRs; (ii) the optimization of the start-up and the operating temperature of the digesters; (iii) the co-digestion of spent animal bedding with an easily-degradable substrate and the issues connected to the management of the volatile fatty acids (VFAs) produced.The results showed that spent animal bedding is a slowly-degradable substrate which needs a long digestion time. However, it is a substrate suitable to be treated through AD displaying high degradation and methane production rates when processed in LBRs. This substrate is, therefore, a valuable organic resource in the agricultural context.Spent animal bedding was shown to contain an active methanogenic population able to start the process efficiently, both in thermophilic and mesophilic temperature, without requiring a specific external inoculation. An economic study at industrial scale proved that this peculiarity can be used to diminish the investment costs and then promote the development of this process. Moreover, thermophilic temperature was proved to be less advantageous over mesophilic condition. In fact, despite the very close methane yield reached in both temperature range, the different biogas production rates in thermophilic conditions would lead to a reduction of the final electric energy production in this condition. Mesophilic temperature was then shown to be the best operating condition for this process.Finally, the role played by the leachate recirculation in the mobilization of the VFAs accumulating in the solid bulk was highlighted in the case of a reactor co-digesting slowly- (spent livestock bedding) and easily-degradable substrates. A strategy was even proposed to efficiently face such a problem by optimizing both the VFA extraction and consumption with the objectives of increasing the overall process efficiency.In the end, this work allowed to optimize some important parameters for the correct management of the LBRs. This technology was proved to be efficient in the treatment of spent livestock bedding, both as a sole substrate or in co-digestion with an easily-degradable substrate. This research study demonstrates that LBRs is an adapted process for the agricultural context and this technology can easily answer to the full scale issues usually encountered. This work represents a significant advance towards the comprehension and development of LBRs to treat agricultural waste and, more generally, to the development of renewable energies based on biomass

The main goal of this work has been that of optimizing the operating conditions of a biofilter, intended for the control of methane, an important greenhouse gas widely emitted by older or smaller landfill installations.The specific objectives were: (1) to select a suitable packing material (of organic or inorganic type); (2) to optimize the concentrations of input nutrients, mainly consisting of nitrogen, phosphorus, potassium and copper, which are intended to be introduced via the nutrient solution; (3) to determine the optimized values of the most important design parameters, such as the methane inlet load (which depends on the air flow rate and the inlet methane concentration); and (4) to model the biofilter performance. Firstly, the comparison of the two packing materials, one of organic type, and the other of inorganic type, has revealed that the latter was the more appropriate material for the methane biofiltration. Then, through the use of the selected packing material, the influence of each individual nutrient on the efficiency of the process has been investigated.The results obtained have shown that both nitrogen and phosphorus concentrations have to be controlled, while potassium and copper were revealed as being nutrients of only minor importance. Secondly, the optimization of the inlet gas flow rate and of the inlet methane concentration (and consequently, of the methane inlet load also), has been performed. According to the results of the studies, these parameters require good control during methane biofiltration because a limitation in biofilter performance could otherwise be induced. In addition, it was noted that the increase in the inlet gas flow rate led generally to a greater decrease of the methane conversion than the one induced by the inlet methane concentration. Finally, a new method, based on the use of solid extracts sampled from the methane biofilter, has been applied to the determination of methane biofilter kinetic parameters. Following this study, a steady state model of the methane biofiltration, taking into consideration the important operational parameters, as identified previously, has been developed. One particular feature of this model is that it takes into consideration the influence of the biofilter average temperature.The prediction results, obtained with the use of the model, have been successfully compared with the experimental results.

Increasing freshwater scarcity is making reclamation of wastewater effluent more economically attractive as a means of preserving freshwater resources. The use of an integrated membrane system (IMS), the combination of micro/ultra-filtration (MF/UF) followed by reverse osmosis (RO) membranes, represents a key process for municipal wastewater reuse. A major drawback of such systems is the fouling of both the MF/UF and RO membranes. The water to be treated by the IMS system varies from one wastewater treatment plant (WWTP) to another, and its fouling propensity changes correspondingly. It is thus preferable to conduct pilot trials before implementing a full-scale plant. This thesis aims to look at the sustainability of IMS technology dedicated to indirect potable reuse (IPR) in terms of fouling minimisation and cost via a 600 m3 .d- 1 pilot plant. Wastewater reuse plants, using IMS, as well as statistical methods for membrane optimisation were reviewed. Box-Behnken design was used to define optimum operating envelopes of the pilot plant for both the microfiltration and the reverse osmosis in terms of fouling minimisation. Same statistical method was used to enhance the efficiency of the MF cleaning-in place through bench-scale test. Data from the pilot plant MF process allow to determine relationship between reversible and irreversible fouling, and operating parameters and feed water quality. Life cycle cost analysis (LCCA) of the both trains (MF/RO/AOP and MF/AOP) of the pilot plant was performed and compared with the LCCA of two full-scale plant.

ABSTRACT The increase of carbon dioxide (CO2) concentration in the atmosphere has become a severe environmental problem, since it could cause global warming due to greenhouse effects. Thus, the reduction of CO2 emission to tackle the greenhouse effect has become one of the most important tasks for sustainable development. The outcomes of this study would be valuable to evaluate the feasibility of applying photocatalytic reduction process to remove CO2 from the atmosphere as well as the flue gas. This study investigated the photocatalytic reduction of CO2 in a self-designed batch UV/TiO2 photocatalytic reactor. The photocatalysts tested included commercial TiO2 (Degussa P-25) and synthesized TiO2 via modified sol-gel process (i.e. NO3-/TiO2 and SO42-/TiO2). Stainless steel supports coated with TiO2 were packed in the batch reactor. The initial concentrations of CO2 ranged from 0.5% to 7.5%. The reductants investigated included hydrogen (H2), water vapor (H2O), and hydrogen with water vapor (H2+H2O). The incident UV light with wavelength of 365 nm was irradiated by a 15-watt low-pressure mercury lamp. The photocatalytic reaction was conducted continuously for approximately 48 hours. Reactants and products were analyzed quantitatively by a gas chromatography with a flame ionization detector followed by a methaneizer (GC/FID-Methaneizer). Experimental results indicated that stainless steel coated with TiO2 had better photoreduction efficiency than that of quartz glass. The optimal operating conditions of CO2 photoreduction were observed by using H2 over SO42-/TiO2, which could produce major products of CO and CH4 and minor products of C2H4 and C2H6. Sulfuric acid used as a stabilizer in the sol-gel process could produce TiO2 of high specific surface area. Results obtained from the operating parameter tests showed that the photoreduction rate increased with the initial concentration of carbon dioxide and resulted in more product accumulation. Higher photoreduction efficiency of carbon dioxide was observed by using the hydrogen (H2) than water vapor (H2O). The photoreduction rate of carbon dioxide increased with reaction temperature, which promoted the formation of products. In addition, proper water vapor (ie. relative humidity of water vapor =25%~75%) could increase the photoreduction efficiency. However, the photoreduction efficiency decreased white it was close to (ie. relative humidity of water vapor =75%~100%). Concurred with previous researches, the reaction rate of major products over SO42-/TiO2 were higher than previous investigations of CO2 photoreduction. This study proposed the reaction pathway using hydrogen and/or water vapor as the reductants. Moreover, a one-site Langmiur-Hinshewood kinetic model (L-H model) was successfully applied to simulate the reaction rate of CO2 during the photoreduction reaction process.

Abstract This study investigated the optimal operating parameters on road dust removal by a flusher. It aimed at enhancing road flushing efficiency, analyzing particle size range, and establishing a flushing model. This study explored main roads by collecting road dusts in Kaohsiung metropolitan area in October 2001. The roads were classified by road dust loading (RDL) as follows: level A (minor, RDL<1g/m2), level B (normal, RDL=1~5g/m2), level C (abnormal, RDL=5~11g/m2), and level D (serious, RDL= 11~25g/m2). The frequency of road flushing was recommended as follows: Level D roads were flushed every day to maintain RDL≤20g/m2. Level C roads were flushed every day, while level B roads were flushed every two days, to keep RDL≤10g/m2. Level A roads were flushed every week to maintain RDL≤5g/m2. A pilot-scale road-flush testing field was designed for this particular study to investigate the influence of operating parameters on road flushing efficiency. The findings indicated that flat-fan type nozzle demonstrated higher flushing efficiency than hollow-cone type nozzle, and that the flushing speed and the distance of the nozzle away from the ground were correlated negatively with the road flushing efficiency, whereas the pressure of nozzle and RDL was correlated with the road flushing efficiency. The results suggested that, in the condition of eighty percent of flushing efficiency, the optimal operating parameters were flushing speed of 15km/hr, the pressure of nozzle of 2.0kg/cm2, the distance away from the ground of 30cm, the angle of 40o, and the particle size less than 150£gm. The results showed that particle size was correlated negatively with the road flushing efficiency under various operating parameters of flushing for different road levels. Beside, the road flushing efficiency was above 80% for silt with particle size less than 75£gm. However, for particle size larger than 850£gm, the road flushing efficiency was up to 40%. It concluded that the road flushing efficiency of fine particles was better than that of coarse particles. After conducting dimensionless analysis and multiple regression analysis, the model of road flushing efficiency can be shown as follows, ¡]R¡×0.8276¡^ where £b is the road flushing efficiency, U is the flusher speed (m/s), P is the water injecting pressure (N/m2), W is the road dust loading (kg/cm2), H is the distance of nozzle away from the ground (m), q is the amount of water per square meter (m3/m2), and £c is the angle of nozzle spread. In this model, RDL is negatively correlated with U, W and H. Moreover, the road flushing efficiency increases with water injection pressure and flow rate. On the basis of the above model, the average percentage of error was approximately 0.28%. In this study, the optimal operating parameters of a flusher were that the flushing speed of 10km/hr, water injecting pressure of 2.0kg/cm2, the distance of nozzle away from the ground of 20cm, and the water injecting angle of 45o. However, depending upon the road cleanness levels, the optimal operating parameters could be varied. For instance, the distance of the nozzle away from the ground should be increased up to 30cm in order to prevent the damage from uneven roads or cavities. The experiments showed that 30cm of the height was a better option due to the road flushing efficiency was only 2% lower while compared with that of 20cm. After the analysis of experimental data, the results can serve as the operation condition for road flushing practice as authorities concerned. The operating parameters proposed in this study could be useful for basic design of a high-efficiency flusher. Moreover, the model of road flushing efficiency can be further applied to predict the road flushing efficiency.

This study investigated the feasibility of glassfiber filter coated with titanium dioxide (TiO2) on removing indoor VOCs using photocatalytic technology, which could further expand the electronic filter¡¦s function . First of all, we coated the titanium dioxide (TiO2) photocatalysts on the glassfiber filter with chemical vapor desposition (CVD) method, then dried it at 120¢J, and calcined it to prepare a nano-sized TiO2 coated filter . Secondly, we collected VOC samples in a printery and analyzed their chemical components. The main components of VOCs (benzene¡Btoluene and acetone) were then conducted in a self-designed laboratory-scaled batch photocatalytic reactor. The decomposition of acetone for different operating parameters, including initial VOC concentration, CVD coating time, and calcination temperature, was further conducted. Besides, a nano-sized photocatalyst indoor air purifier was self-designed for this particular study. The air purifier consists of a set of near-UV light source, a nano-sized photocatalyst glassfiber filter, a stainless shelter, and a circulating fan. The air purifier was tested to ascertain its capability on the removal of indoor VOCs in a well-tight environmental chamber. The testing results indicated the nano-sized photocatalyst glassfiber filter can be used to remove indoor VOCs . In the final stage, a nano-sized TiO2 photocatalyst electronic air cleaner was self-designed for this particular further study in a printery. The air cleaner consists of a set of UV light source, a nano-sized photocatalyst glassfiber filter, a set of electronic filter, carborn filter and a pain coated steel plate shelter. The air cleaner was tested to ascertain its capability on the removal of indoor VOCs in a return air channel of air condition system. The testing results indicated that the nano-sized photocatalyst glassfiber filter can be used to remove indoor VOCs

No description available.

Yes / The Reverse Osmosis (RO) input parameters have key roles in mass transport and performance indicators. Several studies can be found in open literature. However, an experimental research on evaluating the brackish water RO input parameters influence on the performance metrics with justifying the interference between them via a robust model has not been addressed yet. This paper aims to design, construct, and experimentally evaluate the performance of a 50 m3/d RO pilot-plant to desalinate brackish water in Shahid Chamran University of Ahvaz, Iran. Water samples with various salinity ranging from 1000 to 5000 ppm were fed to a semi-permeable membrane under variable operating pressures from 5 to 13 bar. By evaluating permeate flux and brine flowrate, permeate and brine salinities, membrane water recovery, and salt rejection, some logical relations were derived. The results indicated that the performance of an RO unit is largely dependent on feed pressure and feed salinity. At a fixed feed concentration, an almost linear relationship was found to relate feed pressure and both permeate and brine flowrates. Statistically, it was found that 13 bar feed pressure results in a maximum salt rejection of 98.8% at a minimum permeate concentration of 12 ppm. Moreover, 73.3% reduction in permeate salinity and 30.8% increase in brine salinity are reported when feed pressure increases from 5 to 13 bar. Finally, it is concluded that the water transport coefficient is a function of feed pressure, salinity, and temperature, which is experimentally estimated to be 2.8552 L/(m2 h bar).

Many industrial processes would require enormous amounts of water, which could ultimately result in wastewater. Water scarcity in many parts of the world makes this situation unsustainable. In order to reuse wastewater in industrial processes or for other purposes, wastewater must be treated properly. In industrial wastewater treatment, electrocoagulation-flotation (ECF) can be used to dissolve sacrificial electrodes and produce metal coagulant in-situ by applying a current to the electrodes. The reactor design and electrode configuration can profoundly affect the performance of electrocoagulation-flotation (ECF). While most conventional ECF reactors use an open-vertical electrode configuration in rectangular cells, mixing is limited by vertical electrodes that make a barrier and disrupt the flow hydrodynamics. The effects of these factors may influence removal efficiency, flow hydrodynamic, floc formation, and flotation/settling characteristics. The present work aimed to optimize the ECF process by developing an innovative electrode configuration. A variety of parameters were examined to determine the effectiveness of the removal of contaminants from industrial wastewater that had turbidity, emulsified oil, and heavy metals (Si, Zn, Pb, Ni, Cu, Cr, and Cd), as well as stirring speed and foaming. Additionally, the experimental results of the innovative electrode configuration were compared with those of the conventional rectangular cell with plate electrode configuration. Based on the results, the innovative electrode configuration consumed approximately 20% less energy than a conventional ECF for operating times of 10, 20, 30, 32, 48, and 70 minutes. As a result of the enhanced flow hydrodynamic, the formed gas bubbles tilted toward the center, significantly reducing foam formation. There was also an investigation of the dominant operating parameters for electrocoagulation-flotation (ECF) that could affect the removal efficiency, including current density (CD), initial pH, electrolytic conductivity, dosage of coagulant, operating time, initial turbidity concentration, and stirring speed. In addition, a novel approach has been proposed for evaluating EC performance and selecting an appropriate process for removing sludge based on the intake's initial concentration. Keywords: Electrode configuration, electrocoagulation process, electro-flotation, energy consumption, removal efficiency, Electrochemical treatment, Aluminium electrode, Turbidity removal, TOC removal, operating parameters, computational fluid dynamics, Reynolds number, mass transfer, pH evolution.:Table of Contents Abstract 7 1. Introduction 16 1.1. The electrocoagulation process 17 1.2. Problem statement 19 1.3. Objectives 20 1.4. Scope of the work 21 2. Literature survey 23 2.1. Industrial wastewater and treatment methods 24 2.1.1. Impact of industrial growth 24 2.1.2. An analysis of global industrial growth based on statistics 25 2.1.3. Extensive sources of industrial effluent 26 2.1.4. Wastewater and reserve rehabilitation in industry 34 2.1.5. Applied techniques in industrial wastewater treatment 40 2.2. Electrocoagulation (ECF) 50 2.3. Comparison of EC with other treatment methods 50 2.4. Basic concepts and theory of coagulation and electrocoagulation 53 2.5. Electrocoagulation applications 58 2.5.4. Textile industry 60 2.5.5. Leather Tanning Industry 61 2.5.6. Metal-bearing industrial effluents 61 2.5.7. Pulp and paper industry 62 2.5.8. Petroleum refinery 63 2.6. Type and Configuration of the Electrodes 64 2.6.1. Case of Al electrodes 66 2.6.2. Case of Fe electrodes 68 2.7. Reactor design 71 2.6. Modeling 72 2.6.1. Kinetics 73 2.7. Impact of electrocoagulation operating condition on contaminant removal efficiency 75 2.7.1. Effect of current density 75 2.7.2. Effect of initial pH 75 2.7.3. Effect of operating time 76 2.7.4. Effect of electro conductivity 76 2.7.5. Effect of stirring speed 77 2.7.6. Effect of concentration 77 2.7.7. Effect of gap between the electrodes 77 2.7.8. Effect of temperature 78 2.8. Economical aspects and cost analysis 78 3. Material and methods of the tests 80 3.1. Test procedure 1: Impact of operating parameters on removal of turbidity 81 3.1.1. Operating conditions 81 3.1.2. EC cell construction and electrode arrangement 82 3.1.3. Synthetic wastewater 85 3.1.4. Analytical methods and EC procedure 86 3.1.5. Anodic and cathodic reactions 87 3.1.6. Electrical double layer and particle stability 89 3.2. Test procedure 2: Spiral electrode configuration 91 3.2.1. Experimental Setup 91 3.2.2. Sampling and analytical measurements 95 3.2.3. Experimental procedure 95 4. Results and discussion 97 4.1. Test procedure 1: Impact of operating parameters on removal of turbidity 98 4.1.1. Effect of current density (CD) 98 4.1.2. Effect of initial pH 100 4.1.3. Effect of electrolytic conductivity 104 4.1.4. Effect of coagulant dosage, electrode and energy consumption 106 4.1.5. Effect of current density and operating time on initial turbidity concentration 107 4.1.6. Effect of stirring speed 111 4.1.7. Effect of electrode passivation 112 4.2. Test procedure 2: Spiral electrode configuration 115 4.2.1. Removal efficiency of contaminants 115 4.2.2. Effect of stirring speed and ECF configuration on removal efficiency 119 4.2.3. Energy consumption and voltage rise 123 4.2.4. Foaming effect 126 4.3. Computational Fluid Dynamics (CFD) Simulation 128 5. Conclusions and future work 138 5.1. Conclusions 139 5.2. Future works 142 References 143 6. Appendix 159