This thesis examines the bioleaching of six different Canadian nickel sulphide ores at pH levels above what is generally considered optimum (~ 2). The majority of work discussed in this thesis was conducted with a low-grade metamorphosed ultramafic nickel sulphide ore from Manitoba, Canada (Ore 3), which is not currently exploitable with conventional technologies. The ore contains 21% magnesium and 0.3% nickel. Nickel is the only significant metal value, and is present primarily as pentlandite. A substantial fraction of the magnesium is present as the serpentine mineral lizardite, making processing difficult with conventional pyro- and biohydrometallurgical techniques. The work with this ore has two equally important objectives: to minimize magnesium mobilization and to obtain an acceptable level of nickel extraction. Batch stirred-tank bioleaching experiments were conducted with finely ground ore ( 147 µm) with temperature and pH control. The first phase of experimentation examined the effect of pH (2 to 6) at 30 °C, and the second phase examined all combinations of three pH levels (3, 4 and 5) and five temperatures (5, 15, 22.5, 30, and 45 °C).

This thesis examines the bioleaching of six different Canadian nickel sulphide ores at pH levels above what is generally considered optimum (~ 2). The majority of work discussed in this thesis was conducted with a low-grade metamorphosed ultramafic nickel sulphide ore from Manitoba, Canada (Ore 3), which is not currently exploitable with conventional technologies. The ore contains 21% magnesium and 0.3% nickel. Nickel is the only significant metal value, and is present primarily as pentlandite. A substantial fraction of the magnesium is present as the serpentine mineral lizardite, making processing difficult with conventional pyro- and biohydrometallurgical techniques. The work with this ore has two equally important objectives: to minimize magnesium mobilization and to obtain an acceptable level of nickel extraction. Batch stirred-tank bioleaching experiments were conducted with finely ground ore ( 147 µm) with temperature and pH control. The first phase of experimentation examined the effect of pH (2 to 6) at 30 °C, and the second phase examined all combinations of three pH levels (3, 4 and 5) and five temperatures (5, 15, 22.5, 30, and 45 °C).

This thesis examines the bioleaching of six different Canadian nickel sulphide ores at pH levels above what is generally considered optimum (~ 2). The majority of work discussed in this thesis was conducted with a low-grade metamorphosed ultramafic nickel sulphide ore from Manitoba, Canada (Ore 3), which is not currently exploitable with conventional technologies. The ore contains 21% magnesium and 0.3% nickel. Nickel is the only significant metal value, and is present primarily as pentlandite. A substantial fraction of the magnesium is present as the serpentine mineral lizardite, making processing difficult with conventional pyro- and biohydrometallurgical techniques. The work with this ore has two equally important objectives: to minimize magnesium mobilization and to obtain an acceptable level of nickel extraction. Batch stirred-tank bioleaching experiments were conducted with finely ground ore ( 147 µm) with temperature and pH control. The first phase of experimentation examined the effect of pH (2 to 6) at 30 °C, and the second phase examined all combinations of three pH levels (3, 4 and 5) and five temperatures (5, 15, 22.5, 30, and 45 °C).

This thesis examines the bioleaching of six different Canadian nickel sulphide ores at pH levels above what is generally considered optimum (~ 2). The majority of work discussed in this thesis was conducted with a low-grade metamorphosed ultramafic nickel sulphide ore from Manitoba, Canada (Ore 3), which is not currently exploitable with conventional technologies. The ore contains 21% magnesium and 0.3% nickel. Nickel is the only significant metal value, and is present primarily as pentlandite. A substantial fraction of the magnesium is present as the serpentine mineral lizardite, making processing difficult with conventional pyro- and biohydrometallurgical techniques. The work with this ore has two equally important objectives: to minimize magnesium mobilization and to obtain an acceptable level of nickel extraction. Batch stirred-tank bioleaching experiments were conducted with finely ground ore ( 147 µm) with temperature and pH control. The first phase of experimentation examined the effect of pH (2 to 6) at 30 °C, and the second phase examined all combinations of three pH levels (3, 4 and 5) and five temperatures (5, 15, 22.5, 30, and 45 °C).

Bioprocesses for air pollution control can generally be categorized as bioscrubber, biofilter, and biotrickling filter systems. These processes have been proven to be economical and effective for control of volatile organic compounds (VOCs) with concentrations of <1,000 mg C m-3 in gas streams. First, an activated sludge aeration tank (W x L x H = 40 x 40 x 300 cm) with a set of 2 mm orifice air spargers was utilized to treat gas-borne VOCs (toluene, p-xylene, and dichloromethane) in air streams. The effects of liquid depth (Z), aeration intensity (G/A), the overall mass transfer rate of oxygen in clean water (KLaO2), the Henry¡¦s law constant of the tested VOC (H), and the influent gaseous VOC concentration (C0) on the efficiency of removal of VOCs were examined and compared with a literature-cited model. Results show that the measured VOC removal efficiencies and those predicted by the model were comparable at a G/A of 3.75 ¡V 11.25 m3 m-2 hr-1 and C0 of around 1,000 ¡V 6,000 mg m-3. Experimental data also indicate that the designed gas treatment reactor with KLaO2 = 5 ¡V 15 hr-1, could achieve > 85% removal of VOCs with H = 0.24 ¡V 0.25 at an aerated liquid depth of 1 m, and > 95% removal of dichloromethane with H = 0.13 at a 1 m liquid depth. The model predicts that, for gas treatment in common activated sludge tanks, with KLaO2 = 5 ¡V 10 hr-1, depth = 3 ¡V 4.5 m, G/A = 9 ¡V 18 m3 m-2 hr-1, > 92% VOC removal can be achieved with operating parameters of Z of 3.0 m and KLaVOC/(G/A) of about 0.28 m-1, for VOCs with H < 0.3, such as most oxygen-containing hydrocarbons with low molecular weights, and benzene, toluene, ethylbenzene, and dichloromethane. Second, an activated sludge aeration tank and a sieve-plate column with six sieve plates were utilized to treat gas-borne VOCs in air streams. The tank was used for the biodegradation of the absorbed VOCs from the column which utilized the activated mixed liquor drawn from the tank as a scrubbing liquor. This research proposed a model for VOC absorption to a down-flow activated sludge liquor in a sieve-plate column. The experimental setup consisted of a pilot-scale activated-sludge tank and a sieve-plate tower, as demonstrated. The sieve-plate tower was constructed from a 25 x 25 x 162 cm (W x L x H) acrylic column with six custom-made sieve plates. Each plate has 382 holes which are 3 mm in diameter arranged on a square pitch. The holes give an open area of 3.82% of the whole plate area for gas flow. Two 25 mm-i.d. down-comer pipes were also equipped to allow for the downflow of the activated sludge liquor. Ports were provided at the column inlet, outlet, and each plate for gas and liquid sampling. Experiments were conducted and the model verified based on the results of tests on the removal efficiencies of isopropyl alcohol (IPA), toluene and p-xylene in the system operated at a range of influent VOC concentrations, air application rates, and liquid/gas flow ratios (L/G). The model developed by a material balance for the gaseous- and liquid-VOC over each plate of the column was developed and experimentally verified in this study. Superficial gas velocity over the column plate (U), number of plates (N), volumetric liquid-phase VOC-transfer coefficient (KLaVOC), aerated liquid depth over the plate (Z), volumetric liquid/gas flow-rate ratio (L/G), dimensionless Henry¡¦s law coefficient of the VOC to be absorbed (H), VOC content of the influent scrubbing liquor (xN+1), and the biodegradation rate constant of the VOC in the activated sludge mixed liquor (k) are among the affecting parameters to the effectiveness of the VOC removal. Model application by the model for effects of affecting parameters on the VOC removal effectiveness indicates that L/G, plate number N, biodegradation rate constant k, Henry¡¦s law constant of VOC H are among the important ones. A L/GH of greater than 2 and N of around 6 are enough for the effective (>90%) removal of the influent VOCs with H < 0.01 if no biodegradation occurred in the column. However, a N of over 16 is required for the influent VOCs with H of around 0.2. Biodegradation with a rate constant of around 100 hr-1 in the column greatly improves the column performance.

Biotreatment for air pollution control can generally be categorized as biofilter, bioscrubbing and biotrickling filter systems. Generally, biotreatments could be effective and more economical treatment for containment waste gas if designed and operated properly. A two stage down-flow biofilter (2.18 m in height and 0.4 m¡Ñ0.4 m in cross-sectional area) was constructed to develop a biofilter packed only with fern chips for the removal of air-borne propylene glycol monomethyl ether acetate (PGMEA). Both stages were packed with fern chips of 0.30 m in height and 0.40 m ¡Ñ0.40 m in cross section. Fern chips could avoid the shortcomings of traditional media, such as compaction, drying, and breakdown, which lead to the performance failure of the biofilters. In addition, the fern chip medium has the following merits: (1) simplicity in composition, (2) low pressure drop for gas flow (< 20 mmH2O m-1), (3) simple in humidification, nutrient addition, pH control, and metabolite removal, (4) economical (USD$ 174 ¡V 385 m-3), and (5) low weight (wet basis around 290 kg m-3). Results indicate that with operation conditions of media moisture content controlled in the range of 50 ¡V 74%, media pH of 6.5 ¡V 8.3, EBRT (empty bed retention time) of 0.27 ¡V 0.4 min, influent PGMEA concentrations of 100 to 750 mg m-3, volumetric organic loading of < 170 g m-3 h-1, and nutrition rates of Urea-N 66.0 g m-3.day-1, KH2PO4-P 13.3 g m-3.day-1 and milk powder 1.0 g m-3 day-1, the fern-chip packed biofilter could achieve an overall PGMEA removal efficacy of around 94%. Instant milk powder or liquid milk was essential to the good and stable performance of the biofilter for PGMEA removal. An activated sludge aeration basin (20 cm i.d., 140 cm height) equipped with either a coarse air diffuser (a plastic pipe perforated with 56 orifices of 2 mm in diameter) or a fine diffuser (porous plastic type with 100-micrometer pores) was utilized to treat an air-borne hydrophobic VOC (toluene, 700 ¡V 800 mg m-3). The purposes of this study were to test the influences of both MLSS and diffuser type on the VOC removal efficiency. Results show that higher MLSS (mixed liquor suspended solids) such as 10,000 ¡V 40,000 mg L-1 in the mixed liquor did not enhance greatly the transfer and removal of the introduced toluene. Instead, activated sludge basins with a normal MLSS (e.g., 2,000 ¡V 4,000 mg L-1) in the mixed liquor and an efficient gas diffusion system with volumetric VOC transfer coefficient of around 10 ¡V 15 h-1 can be used for the removal of hydrophobic VOCs from the introduced gas. For achieving a removal of over 95% of the introduced toluene or similar hydrophobic VOCs, commercial air diffusers for aerobic biological wastewater treatment basins can be used with a submerged liquid depth of over 0.40 m over the diffusers and an aeration intensity (air flow rate/basin cross-sectional area) of lower than 5.0 m3 m-2 h-1.

Depuis le début des années 2000, la station d’épuration n’est plus seulement perçue comme une installation industrielle traitant les eaux résiduaires urbaines afin d’en minimiser leurs impacts sur le milieu naturel, mais aussi comme un moyen de récupérer des ressources : eau, nutriments, énergie. Ce travail de thèse traite de cette dernière ressource, l’énergie. Comment tendre vers la station d’épuration auto-suffisante en énergie, voire encore productrice d’énergie sans en affecter l’efficacité de traitement? A l’aide d’une filière de traitement ancienne revisitée : le procédé A/B (Adsorption/Bio-oxydation), le bilan énergétique de la station peut tendre vers la neutralité en réduisant les demandes liées à l’aération et en optimisant la production de biogaz. Ce travail de doctorat se concentre principalement sur la méthanisation des boues issues de ce procédé A/B afin d’en connaître leurs caractéristiques et leur digestibilité, de les comparer avec la digestion anaérobie de boues davantage connues et enfin d’utiliser ces résultats pour dresser le bilan énergétique du procédé A/B, ceci à partir des données récoltées sur un pilote de 50 m3/j installé sur la station d’épuration de Kranji à Singapour. Les boues A et B présentent respectivement les productions spécifiques de méthane respectives de 290 et 135 LCH4/kgMVentrante en conditions mésophiles. Le procédé A/B avec ses deux étages de boues activées permet de capter un maximum de carbone en première étape de traitement pour le transférer directement en digestion. En effet, la production totale de boues provient à 90% des boues A et seulement à 10% des boues B ce qui porte à 95% la production de méthane attribuée aux boues A. Ces résultats induisent une production d’énergie supérieure par rapport à une filière de traitement conventionnelle avec un seul étage de boues activées. Par ailleurs, ce procédé permet de diminuer les besoins en aération pour le traitement des pollutions carbonée et azotée, tout en gardant les mêmes efficacités de traitement. Il est ainsi possible de conclure que la filière de traitement des eaux usées en procédé A/B présente un degré d’efficacité énergétique proche de 300% (ratio entre l’énergie électrique produite à partir du biogaz et la consommation énergétique liée à l’aération), ce qui représente 73% d’auto-suffisance énergétique globale en considérant le cas de la station de Kranji en boues activées conventionnelles traitant les pollutions en carbone et en azote. / Since the early 2000’s, wastewater treatment plants (WWTP) have not been only seen as a mean to reduce the impact of the harmful emissions towards water bodies but also as a way to recover the resources contained in the raw wastewater: water, nutrients and energy. This doctorate seeks to study the latter one. How to tend to the energy self-sufficient or even energy positive WWTP without altering its treatment efficiencies? Using an old wastewater treatment process: the A/B process (Adsorption/Bio-oxidation) and state-of-the-art technologies, the energy autarky of a WWTP can become a reality by reducing its electricity consumption related to the aeration and by optimizing its energy production through anaerobic digestion. This work mainly focuses on the anaerobic digestion of the sludge produced by the A/B process. It aims at evaluating their characteristics and digestibility and thus at comparing these to the ones of better-known sludge such as primary, secondary and mixed sludge from a conventional wastewater treatment system. Eventually, these results with the addition of data collected on a 50 m3/d A/B process pilot plant on the Water Reclamation Plant of Kranji, Singapore, are used to draw the energy balance of the A/B process and to try to make a comparison to conventional systems. The A/B process produces the A and B sludge which respectively show specific methane productions of 290 and 135 LCH4/kgVSintroduced in mesophilic anaerobic digestion and can be considered quite similar to primary and secondary sludge respectively from conventional WWTPs. With its two stages of activated sludge, this process enables the early entrapment of carbon to be directly transferred to the digesters. Indeed, 90% of the sludge production comes from the A sludge in matter of Volatile Solids, which brings to 95% the biogas production to be ascribed to this sludge. Hence, the A/B process does produce more energy than a conventional single-stage activated sludge. It also reduces the aeration demand for the biological treatment of the carbon and nitrogen pollutions whilst complying with the same treatment performances. Drawing the energy balance of the A/B process leads to the conclusions that this process presents an energy efficiency of 300% by comparing only the electrical needs for the aeration (40-70% of the whole plant demand) and the electricity production from biogas generation, which, at the end, represents an energy self-sufficiency of 73% considering the Kranji conventional water reclamation plant.