Experimental Study of Biodegradation of Ethanol and Toluene Vapors

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avoid oxygen insufficiency. The performance equation of a fedbatch bioreactor can be easily derived from the material balance equations for the biomass and substrate as follows: dX dt FX = rx − (2-15) V dS dt F = ( S f − S) − r s (2-16) V where F is the flow rate of the fresh media, S f is the concentration of substrate in the feed, and V is the volume of fluid in the reactor. The volume of fluid in the reactor changes with the addition of liquid feed, F. 2.4.3 Continuous Stirred Tank Reactor (CSTR) The continuous stirred tank reactor (CSTR) is an ideal steady state reactor. The reactants are charged continuously into the stirred tank and the product is continuously discharged from the reactor. Thorough mixing keeps a uniform concentration throughout the reactor. The performance equation of a CSTR for the substrate can be derived from the steady state version of the material balance equation as: r s F = ( S f − S) (2-17) V in which S is the substrate concentration in the output stream and S f is the substrate concentration in the feed; F is the flow rate of the fresh media which is the same as the output liquid flow rate to keep the liquid volume in the reactor, V, constant. 2.4.4 Plug Flow Reactor The other ideal steady state reactor is called a plug flow reactor. The reactants are charged continuously into one end of a pipe and the product is continuously 30
discharged from the other end. The flow pattern in the ideal reactor is plug or piston flow with no back mixing. The performance equation of a single plug flow reactor for the substrate can be obtained from the material balance as: V F S = −∫ S f dS r s (2-18) 2.4.5 Reactors for Biochemical Processes (Bioreactors) Many factors such as cost of equipment, scale of production, stability and safety, that can affect the choice of an optimum reactor. The most important single factor is the reaction kinetics. A poor choice of reactor type can increase the cost of reactor construction and operation as much as two orders of magnitude. For example, the volume of a CSTR reactor needed for 99% conversion for a first order reaction (or even zero and second order) is as much as 100 times more than a plug flow reactor (Levenspiel, 1972). However, the nature of many biochemical reactions resembles autocatalytic reactions which strongly favours the use of CSTRs instead of plug flow reactors (Levenspiel, 1972). 31
Page 1 and 2: BIOREMEDIATION OF VOLATILE ORGANIC
Page 3 and 4: ABSTRACT The mass transfer of ethan
Page 5 and 6: effect on the growth of P. putida.
Page 7 and 8: ACKNOWLEDGMENT Of the countless peo
Page 9 and 10: TABLE OF CONTENTS PERMISSION TO USE
Page 11 and 12: 4.3 Batch Growth on Ethanol and Ben
Page 13 and 14: LIST OF FIGURES Figure 3-1. Schemat
Page 15 and 16: Figure 5.3 (b) Simulation of ethano
Page 17 and 18: Figure 5-16. Continuous removal of
Page 19 and 20: NOMENCLATURE a - Interfacial area,
Page 21 and 22: CHAPTER ONE - INTRODUCTION 1.1 Air
Page 23 and 24: esults (van Groenestijn and Hesseli
Page 25 and 26: experimental results are presented
Page 27 and 28: Table 2.2 VOC Emissions in the U.S.
Page 29 and 30: (paint shop effluents, for instance
Page 31 and 32: combustion provides 70 to 90% air p
Page 33 and 34: used to degrade ethanol vapours and
Page 35 and 36: g m -3 . This would suggest that th
Page 37 and 38: treatment, This excessive biomass f
Page 39 and 40: The simultaneous degradation of tol
Page 41 and 42: emoves only water-soluble gases. Wa
Page 43 and 44: 2.2.6 Pseudomonas It is well known
Page 45 and 46: 2.3.2 Growth Models with Inhibition
Page 47 and 48: where µ is the total specific grow
Page 49: 2.4.1 Batch Reactor In a batch reac
Page 53 and 54: element solution consisted of (gram
Page 55 and 56: growth on ethanol, 20-48 hours for
Page 57 and 58: Gas phase samples of toluene were c
Page 59 and 60: Inlet sampler Exit sampler To fume
Page 61 and 62: Once the oxygen meter indicated a s
Page 63 and 64: centrifuged and the supernatant was
Page 65 and 66: where k L a is the volumetric mass
Page 67 and 68: Figure 4-2a shows ethanol liquid co
Page 69 and 70: coefficient (k L a) in the well-mix
Page 71 and 72: calculated by dividing the gas volu
Page 73 and 74: Average bubble diameter, mm 8 7 6 5
Page 75 and 76: Bioflow III bioreactor. Equation (4
Page 77 and 78: 3.5 y=Ln(S0/S) 3 2.5 2 1.5 1 y = 12
Page 79 and 80: Ethanol and biomass concentration,
Page 81 and 82: 4.3.2 Batch Growth on Benzyl Alcoho
Page 83 and 84: Biomass and benzyl alcohol concentr
Page 85 and 86: ethanol loading was beyond the maxi
Page 87 and 88: Table 4-2. Comparison of bioremedia
Page 89 and 90: Biomass, benzyl alcohol and toluene
Page 91 and 92: 4.4.3 Toluene-ethanol Bioremediatio
Page 93 and 94: Substrate and biomass concentration
Page 95 and 96: Biomass and benzyl alcohol concentr
Page 97 and 98: Biomass and benzoic acid concentrat
Page 99 and 100: ethanol. These results clearly indi
Page 101 and 102:
CHAPTER FIVE - MATHEMATICAL MODELIN
Page 103 and 104:
The stoichiometry of the biomass sy
Page 105 and 106:
synthesis and in the ethanol catabo
Page 107 and 108:
1 max Y ex = − 0.635 + 2δ + K 3
Page 109 and 110:
Biomass Eq.5-18 Benzyl Alcohol Eq.5
Page 111 and 112:
r x r N -1.27 -1 0 1 0 0 -0.2 0 0 2
Page 113 and 114:
φ = −θ b ⋅ν (5-31) φ b = 1.
Page 115 and 116:
The data sets used to evaluate the
Page 117 and 118:
Figures 5.4a and 5.4b present 95% c
Page 119 and 120:
Ethanol and biomass concentration (
Page 121 and 122:
Ethanol measured (C-mol/L) 0.3 0.25
Page 123 and 124:
Figures 5.5 (a-d) demonstrate the s
Page 125 and 126:
Benzyl alcohol and biomass concentr
Page 127 and 128:
Benzyl alcohol measured (C-mol/L) 0
Page 129 and 130:
x = 5 ∑ i= 1 x N i (5-40) where x
Page 131 and 132:
ethanol in a steady state mode is l
Page 133 and 134:
where ν 1 , ν 2 , ν 3, ν 4 are
Page 135 and 136:
Biomass concentration, g/L 1.5 1 0.
Page 137 and 138:
φ T =ν 4 (5-53b) φx = −ν 1 (5
Page 139 and 140:
In this study, a metabolic model ha
Page 141 and 142:
Equations (5-34) and (5-35) and the
Page 143 and 144:
ATP 1 = Y max ATP r x + m ATP ⋅ C
Page 145 and 146:
Ethanol, biomass and ammonium conce
Page 147 and 148:
Figure 5-13a shows that the lower t
Page 149 and 150:
Biomass, substrate concentrations,
Page 151 and 152:
C e DKe = (5-63) μ − D m Equatio
Page 153 and 154:
corresponds with the value associat
Page 155 and 156:
Biomass and ethanol concentrations
Page 157 and 158:
than 4.0 mg/L at all dilution rates
Page 159 and 160:
Biomass, benzyl alcohol and ammonia
Page 161 and 162:
negligible ( y out , e = 0) , and e
Page 163 and 164:
Figure 5-17 shows the results at a
Page 165 and 166:
Biomass Concentrations, g/L 3.5 3 2
Page 167 and 168:
C x ( 1 max Q max = ⋅{ D( Cb0 −
Page 169 and 170:
1.2 g/L, the system could not be op
Page 171 and 172:
The continuous models can capture a
Page 173 and 174:
• Air stripping coefficients obta
Page 175 and 176:
Toluene acts as an inhibitor on the
Page 177 and 178:
Bruining, W. J., G. E. H. Joosten,
Page 179 and 180:
Falatko, D. M., and J. T. Novak, 19
Page 181 and 182:
Keuning, S., and D. Jager, 1994.
Page 183 and 184:
Orshansky, F., and N. Narkis, 1997.
Page 185 and 186:
Togna, A. P, M. Singh, 1994. “Bio
Page 187 and 188:
APPENDIX A. Important Metabolic Pat
Page 189 and 190:
III. Toluene Pathway (Adapted from
Page 191 and 192:
Appendix B. Calibration Procedure a
Page 193 and 194:
Figure B-2. Pseudomonas putida (ATC
Page 195 and 196:
Appendix B-3. Calibration of Chemic
Page 197 and 198:
Appendix B-4. Calibration of Toluen
Page 199 and 200:
Appendix C. Experimental Results: A
Page 201 and 202:
Probe response time, s 12 10 8 6 4
Page 203 and 204:
Appendix C-2. Fed-batch Operation B
Page 205 and 206:
Appendix D: Mathematical Solutions
Page 207 and 208:
The microscopic model allows the fo
Page 209 and 210:
13δ Y o , = 0.585 2 x = (D-24) (8K
Page 211 and 212:
2 σ = −1.3E − 06 (E-11) Y xe Y
Page 213:
Biomass, ethanol, and acetic acid c
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Experimental Study of Biodegradation of Ethanol and Toluene Vapors

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