iv, 235 leaves : ill. / Title page, contents and abstract only. The complete thesis in print form is available from the University Library. / Thesis (Ph.D.)--University of Adelaide, Dept. of Organic Chemistry, 1972

Thesis (Ph.D.) -- University of Adelaide, Dept. of Organic Chemistry, 1972.

Thesis (Ph.D.)--York University, 2007. Graduate Programme in Earth and Space Science. / Typescript. Includes bibliographical references (leaves 116-121). Also available on the Internet. MODE OF ACCESS via web browser by entering the following URL: http://gateway.proquest.com/openurl?url_ver=Z39.88-2004&res_dat=xri:pqdiss&rft_val_fmt=info:ofi/fmt:kev:mtx:dissertation&rft_dat=xri:pqdiss:NR29331

Thesis (Ph. D.)--University of Wisconsin--Madison, 1968. / Typescript. Vita. eContent provider-neutral record in process. Description based on print version record. Includes bibliographical references.

No description available.

Thesis (Ph. D.)--University of Washington, 1998. / Vita. Includes bibliographical references (leaves [269]-277).

In this work, a differential biofiltration reactor was used to explore the potential of metabolic uncouplers to improve pollutant (toluene) degradation rates. Metabolic uncouplers were reported to reduce the cell mass in activated sludge systems, but are untested in biofilters and the current work is the first to report the impact of different metabolic uncouplers in a biofilter. Initially soil was used as a biofilter bed and later experiments were conducted in pure cultures in a biofilm reactor. A simple diffusion system was developed to generate the desired concentration of toluene to the system. Gas chromatography and a carbon dioxide analyzer were connected online to the reactor which improved the precision of the data collected and also the robustness of the measurements. Preliminary experiments including effect of substrate concentration, different nutrients and temperature were done to optimize the conditions before starting the metabolic uncoupler screening studies in soil. Based on the results, inlet toluene concentration between 180 ppm and 250 ppm was used throughout the studies. Also it was found that the toluene degraders were nitrogen limited. Temperature studies showed that the elimination capacity (EC) increased with increasing temperature, from 34 ± 1.4 g.m-3.h-1 to 49.8 ± 2.6 g.m-3.h-1 for temperatures of 20 to 45 oC, respectively. Nine potential metabolic uncouplers were screened in batch serum bottles. The nine uncouplers tested were dinitrophenol (dNP), p-nitrophenol (pNP), benzoic acid (BA), carbonylcyanide p-trifluoromethoxy phenylhydrazone (FCCP), carbonylcyanide m-chloromethoxy phenylhydrazone (CCCP), pentachlorophenol (PCP), malonic acid (MA), m-chlorophenol (mCP) and 2, 4, 6-trichlorophenol (TCP). Other than dNP and pNP (nitrogen containing uncouplers), seven other uncouplers were further tested in the differential biofilter reactor. Only PCP and TCP increased the toluene degradation rate significantly. PCP increased the toluene degradation rate by 35% at 140 µM, whereas 4051 µM TCP increased the rate by 18%. Though FCCP behaved as a classical uncoupler when compared with others, the EC increase was not significant. Five toluene degraders were isolated from soil subjected to toluene and were identified using 16s rDNA/18s rDNA analysis. Out of five, two potential toluene degraders, Stenotrophomonas maltophilia and Pseudomonas putida were used to develop a biofilm reactor. PCP, TCP and CCCP were tested in the biofilm reactors and found that PCP increased the surface elimination capacity (SEC) by 85% at 140 µM in S. maltophilia biofilm reactor and CCCP increased the SEC by 27% at 1 µM in P. putida biofilm reactor. Finally a simple model was developed to calculate the energy uncoupling coefficient for non-growth systems like ours to quantitatively represent the uncoupling mechanism.

No description available.

by Yam Chi Ming. / Thesis (M.Phil.)--Chinese University of Hong Kong, 1991. / Bibliography: leaves 132-135. / TABLE OF CONTENTS / DESCRIPTIVE NOTE PAGE / ABSTRACT --- p.iii / ACKNOWLEDGEMENTS --- p.v / Chapter CHAPTER ONE： --- BACKGROUND SURVEY OF THE CHEMISTRY OF THE OXIDATION OF ORGANIC COMPOUNDS --- p.1 / Chapter 1.0 --- Introduction --- p.1 / Chapter 1.1 --- Catalytic Oxidation of Toluene --- p.4 / Chapter 1.1.1 --- Metal-catalyzed Air Oxidation of Organic Compounds --- p.4 / Chapter 1.1.2 --- Metal-catalyzed Air Oxidation of Alkyl-Aromatic Compounds --- p.11 / Chapter 1.1.3 --- Cobalt-catalyzed Air Oxidation of Toluene --- p.12 / Chapter 1.2 --- Industrial Metal-catalyzed Air Oxidation of Toluene --- p.13 / Chapter 1.3 --- Scope of this Thesis --- p.16 / Chapter CHAPTER TWO： --- EXPERIMENTAL --- p.20 / Chapter 2.1 --- Reactor System Description --- p.20 / Chapter 2.1.1 --- Liquid Sampling Unit --- p.23 / Chapter 2.1.2 --- Gas and Reagent/Catalyst Inlet --- p.23 / Chapter 2.1.3 --- Recycling Unit --- p.26 / Chapter 2.1.4 --- Vapour Disposal --- p.28 / Chapter 2.2 --- Practical Operation Consideration --- p.30 / Chapter 2.3 --- Process (Experimental) Parameter Control --- p.33 / Chapter 2.3.1 --- Gas Inlet and Input Pressure Control --- p.33 / Chapter 2.3.2 --- Gas Outlet and System Pressure Control --- p.34 / Chapter 2.3.3 --- System Temperature Control --- p.35 / Chapter 2.4 --- Data Acquisition --- p.36 / Chapter 2.5 --- Experimental Procedures --- p.38 / Chapter 2.5.1 --- Initial Operation Testing --- p.38 / Chapter 2.5.2 --- General Procedures --- p.38 / Chapter 2.5.3 --- Experimental Conditions --- p.41 / Chapter 2.5.3.1 --- Air Oxidation of Toluene --- p.41 / Chapter 2.5.3.2 --- Cobalt-catalyzed Air Oxidation of Toluene --- p.43 / Chapter 2.5.3.3 --- Silver-catalyzed Air Oxidation of Toluene --- p.47 / Chapter 2.5.3.4 --- Cobalt-Silver Co- catalyzed Air Oxidation of Toluene --- p.47 / Chapter 2.5.3.5 --- Hydrogen Peroxide Experiment --- p.47 / Chapter 2.6 --- Reactor Product Analysis --- p.48 / Chapter 2.6.1 --- Liquid Sample Analysis --- p.48 / Chapter 2.6.2 --- Cobalt (II)Analysis --- p.49 / Chapter 2.7 --- Product Identification and Confirmation by 1H Nuclear Magnetic Resonance --- p.56 / Chapter CHAPTER THREE： --- RESULTS AND DISCUSSIONS --- p.58 / Chapter 3.0 --- Introduction --- p.58 / Chapter 3.1 --- Air Oxidation of Toluene --- p.60 / Chapter 3.2 --- Cobalt-catalyzed Air Oxidation of Toluene --- p.75 / Chapter 3.3 --- Silver-catalyzed Air Oxidation of Toluene --- p.96 / Chapter 3.4 --- Cobalt-Silver Co-catalyzed Air Oxidation of Toluene --- p.106 / Chapter 3.5 --- Industrial Applications --- p.116 / Chapter CHAPTER FOUR： --- CONCLUSION --- p.126 / BIBLIOGRAPHY --- p.132 / Chapter APPENDIX I --- Computer Program for the Integrator --- p.136 / Chapter APPENDIX II --- Raw Data for the Experimental Runs --- p.140 / Chapter APPENDIX III --- Raw Data for Different Trials of Run #11 --- p.160 / Chapter APPENDIX IV --- "Raw Data for the Calibration of Benzaldehyde, Benzyl Alcohol, Benzoic Acid, Benzyl Acetate, Benzyl Benzoate and Cobalt (II)" --- p.161

In this study, a two-bed electrically-heated regenerative catalytic oxidizer (RCO) was used to test the destruction characteristics in burning toluene-borne air streams. The RCO contained two 0.152 m¡Ñ0.14 m¡Ñ1.0 m (L ¡Ñ W ¡Ñ H) beds, both packed with gravel particles with an average diameter of around 0.0111 m and a height of up to 0.875 m with a void fraction of 0.42 in the packed section. In addition, in each column catalytic particles with an average diameter of around 0.008 m were packed over the gravel particles to a height of 0.125 m. Gas temperature rise and the gas pressure drop over the beds were also studied. Experimental results reveal that, with a valve shifting time (ts) of 1.5 min, superficial gas velocities (Ug) of 0.39 and 0.86 m/s (evaluated at an influent air temperature of around 30 oC) and preset maximum destruction temperatures (TS) of 300-400 oC, only around 25% of the influent toluene (Co = 200-400 ppm) was thermally destructed with no catalyst in both beds. With the cartalyst packings and operation conditions of Ug = 0.39 m/s and Co = 200-800 ppm, destruction efficacies of around 80.9¡Ó0.8, 94.6¡Ó1.8, and 98.1¡Ó0.2 % were observed, respectively, at TS of 250, 300, and 400 oC. At Ug = 0.86 m/s and Co = 200-800 ppm, destruction efficacies of around 69.7¡Ó3.1, 93.9¡Ó1.7, and 97.8¡Ó0.4 % were observed, respectively, at TS of 250, 300, and 400 oC. It is suggested that operation conditions with Ug = 0.39-0.86 m/s (equivalent to empty-bed-residence times of 0.29-0.64 s for the gas at 30oC through the catalyst beds) and TS = 300 oC are suitable for the destruction of around 98% of the influent air with 200-800 ppm toluene. Gas temperature rises of 21 and 26 oC, respectively, were found for Ug = 0.39 and 0.86 m/s with TS = 300 oC. The Ergun equation was found to suffice in the estimation of the pressure drop when the gas flowed over the packing beds.