Thesis - faculty.ait.ac.th - Asian Institute of Technology

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1. Obtaining endogenous sludge: 0.9 liter of fresh sludge without the substrate was obtained in a respirometer and aerated for two hours. 2. Suppressing nitrification: With high ammonia concentration during the organic oxidation, the oxygen uptake rate of nitrification process was constant. Hence, NH4Cl of concentration 70 mg/L was added. 3. Recording endogenous oxygen uptake rate (OUR): After suppressing the nitrification process, the mixture was aerated for half an hour before measuring the endogenous OUR. 4. Adding substrate: An accurate dose of substrate was injected into the respirometer and the total OUR was recorded by respirogram. Re-aeration was done once the DO concentration dropped below 2 mg/L. 3.4.2 Lead Toxicity The lead toxicity on the bacterial and yeast culture was conducted in the same manner as described in the section 3.4.1. Lead nitrate (Pb (NO3)2) was used as Lead (Pb) source. Soluble Pb concentration was varied from 0 to 20 mg/L. At each concentration, the sample was filtered with 0.45 µm membrane filter and soluble Pb concentration was analyzed using an atomic absorption spectrophotometer (AAS). 3.5 Ammonia Stripping The characteristics of leachate used for the experiment are as described in Table 3.1. The summary of the experiments conducted in order to optimize ammonia stripping is illustrated in Figure 3.4. The efficiency of ammonia stripping in ammonia removal was tested varying three parameters namely- pH, contact time and the velocity gradient. The experiments conducted are as follows: 1. Optimum pH for air stripping: The pH was varied from 9-12 (9, 10, 11, and 12) using 12 N NaOH solution. The removal efficiency of ammonia at varying pH was assessed with a velocity gradient of 2,850 s -1 for two hours. 2. Optimum velocity gradient and contact time: After the optimum pH was obtained, the velocity gradient and the contact time were varied. The velocity gradients at which the experiment was done were 1,530, 2,850, and 4,330 s -1 . The contact time was varied from 1 to 6 hours. 58
Figure 3.4 Experiments Conducted to Optimize Ammonia Stripping 3.6 Membrane Bioreactor 3.6.1 Membrane Resistance Measurement The new membrane module requires a test in order to find out the initial membrane resistance. Membrane resistance was measured based on the resistance-in-series model which provides a simple means of describing the relationship between permeate flux and trans-membrane pressure. According to this model, it is expressed by the following equation: Where: NaOH Solution J = TMP Eq. 3.1 µ Rt J = permeate flux (m 3 /m 2 .s) TMP = trans-membrane pressure (Pa) µ = permeate viscosity (Pa.s) Rt = total resistance for filtration (1/m) For further understanding of the components of membrane resistances causing the membrane clogging, the total resistance (Rt) was measured right after the run with the membrane still in its clogging condition. Rm and Rn were obtained by measuring the resistance of the membrane after being washed with tap water to remove the cake layer. The membrane resistance at the beginning of the run after chemical clean was considered as Rm. Rc Value was derived from Rt, Rm, and Rn using Equation 3.2. 59 Leachate pH Adjustment (for pH 9, 10, 11 and 12) Variation of Velocity Gradient and Contact Time (for 2, 3, 4, 5 and 6 h) Control 1,530 s -1 2,850 s -1 4,330 s -1
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APPLICATION OF MEMBRANE BIOREACTOR
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Abstract Landfill leachate is a com
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Table of Contents Chapter Title Pag
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4.5.6 Cost Analysis for Operation 1
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4.4 Effect of Free Ammonia Concentr
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4.16 COD Concentration in the Influ
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MWCO Molecular Weight Cut-off MWW M
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1.1 Background Chapter 1 Introducti
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generally unsuccessful in removal o
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2.1 Introduction Chapter 2 Literatu
Page 21 and 22: In the municipal solid waste landfi
Page 23 and 24: COD/TOC, VS/FS and VFA/TOC ratios o
Page 25 and 26: Table 2.3 presents the general leac
Page 27 and 28: Ground water 2.7.1 Seasonal Variati
Page 29 and 30: Table 2.5 Variation of COD, BOD & B
Page 31 and 32: entails the re-circulation of leach
Page 33 and 34: Table 2.8 Summary of Biokinetic Coe
Page 35 and 36: that extensive loss of nitrogen (up
Page 37 and 38: ammonia could only be achieved when
Page 39 and 40: Table 2.10 Treatment Efficiencies o
Page 41 and 42: Activated Carbon Adsorption Granula
Page 43 and 44: Colloidal material as well as metal
Page 45 and 46: iologically, physical-chemical proc
Page 47 and 48: Ammonia Stripping Air stripping of
Page 49 and 50: These systems are land intensive wh
Page 51 and 52: the biological treatment can be rep
Page 53 and 54: Table 2.16 Typical Leachate Composi
Page 55 and 56: influent reached 200 mg/L. For the
Page 57 and 58: Table 2.18 Advantages and Disadvant
Page 59 and 60: through the effluent. Different ope
Page 61 and 62: Mixed Liquor Suspended Solids and D
Page 63 and 64: 2.12 Yeasts 2.12.1 Introduction The
Page 65 and 66: Nishihara ESRC Ltd. (2001) studied
Page 67 and 68: nitrification-denitrification proce
Page 69 and 70: Table 3.1 Composition of Simulated
Page 71: 3.4.1 Ammonia Toxicity The experime
Page 75 and 76: Leachate Option Ammonia Stripping R
Page 77 and 78: MW larger than 50 kDa, (2) MW betwe
Page 79 and 80: Figure 3.7 Flowchart Showing Ammoni
Page 81 and 82: Chapter 4 Results and Discussion 4.
Page 83 and 84: COD Removal Effeciency (%) COD Remo
Page 85 and 86: MLSS (mg/L) 14000 12000 10000 8000
Page 87 and 88: Specific Growth Rate ( d -1 ) 0.50
Page 89 and 90: change in the predominant species w
Page 91 and 92: Table 4.4 Effect of Free Ammonia Co
Page 93 and 94: Table 4.5 Substrate Utilization by
Page 95 and 96: 4.3.1 Initial Membrane Resistance P
Page 97 and 98: when compared with the present stud
Page 99 and 100: COD Removal Efficiency (%) 90 80 70
Page 101 and 102: (2) TKN Removal Efficiency Prior to
Page 103 and 104: As there was no significant improve
Page 105 and 106: The probable reason for frequent fo
Page 107 and 108: Ammonia Concentration (mg/L) Ammoni
Page 109 and 110: concentration after treatment. Othe
Page 111 and 112: After the chemical cleaning of the
Page 113 and 114: emoval of 38%. A higher removal in
Page 115 and 116: Influent BOD (mg/L) Influent BOD (m
Page 117 and 118: (3) TKN Removal Efficiency The TKN
Page 119 and 120: Figure 4.34 gives the overall TKN r
Page 121 and 122: fraction and slowly biodegradable C
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BOD (mg/L) BOD (mg/L) 6000 5000 400
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Figure 4.39 Molecular Weight Cut-of
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COD (mg/L) 8000 6000 4000 2000 COD
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Though, the obtained COD removal ef
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cake used on the top of the membran
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Chapter 5 Conclusions and Recommend
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0.02, respectively. This can be con
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References Abeling, U., and Seyfrie
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Brown, M.J., and Lester, J.N., 1980
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Diamadopoulos, E., 1994. Characteri
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Grady, C.P.L., Daigger, G.T., and L
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Keenan, J.D., Steiner, R.L., and Fu
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Martin, G.M.A., Auzmenti, A.I., and
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Pohland, F.G., and Harper, S.R., 19
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Shin, H.S., An, H., Kang, S.T., Cho
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Visvanathan, C., Ben Aim, R., and P
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Appendix A Pictures of Experiments
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Raw Leachate YMBR Effluent BMBR Eff
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Appendix B Leachate Characteristics
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Table B-2 Acclimation of Mixed Yeas
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Appendix C Experimental Data of Bio
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y: Where: OUR at line g: This is th
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Table C-3 Experimental Results for
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Appendix D Membrane Resistance Stud
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Table D-3 Experimental Data for Det
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Table D-4 Experimental Data for Det
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Pressure (kPa) Pressure (kPa) 25 20
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Appendix E MBR without Ammonia Stri
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Day HRT (h) pH COD (mg/L) Feed Reac
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Day HRT (h) pH COD (mg/L) Feed Reac
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Table E-3 Variation in TMP with Tim
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Appendix F Ammonia Stripping Studie
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Table F-5 Pilot Scale Study on Ammo
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Table G-1 Feed, Reactor and Effluen
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Table G-3 Feed, Reactor and Effluen
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Appendix H Other Studies 179
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Table H-2 Membrane Resistance of th
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Table H-6 Chemical Cost for the Yea
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