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Appendix B Calculation of Proposed Decentralized AD Plant 114
Assumptions Size of the community: 5,000 Total waste generated by the community: 5 t/d (Waste generation in low-income countries is 1.0 kg/p/d (Bogner et al., 2007) Weight of organic waste: 60 % of total waste = 0.60 x 5 = 3 t/d, By applying the average waste collection efficiency i.e., 65-70% (Hoornweg and Bhada - Tata, 2012) of South Asian and East Asian regions, the resulted waste quantity: 2.0 t/d or 2000 kg/d TS of waste: 18 % (please refer to Table B-2) VS of waste: 84 %TS (please refer to Table B-2) Density of pretreated waste: 1000 kg/m 3 (please refer to Table B-2 of Appendix B) Reactor working volume: 75 % of total volume Operating conditions (loading rate and retention) and methane yield used for design calculations have been taken from results of run 2 of phase II pilot experiment as given in Table B-1. Table B-1 Operating Conditions Versus Methane Yield of Phase II Pilot Experiment Detail Run 1 Run 2 Run 3 OLR (kg VS/m 3 /d) 4.55 6.40 8.50 RT (d) 30 24 18 Methane yield (L/kg VS) 330 320 266 1. Calculations for volume of reactor Method 1: Working volume of reactor = VS (kg) to be added per day VS load (kg VS/m 3 .d) VS to be added per day = 2000 kg/d x 18/100 (TS) x 84/100 (VS) = 300 kg VS/d Working volume = 300 (kgVS/d) / 6.4 (kgVS/m 3 /d) = 46.88 m 3 Reactor total volume: 46.88 x 100/75 = 62.5 m 3 Method 2: VS to be added per day = 2000 kg/d x 18/100 (TS) x 84/100 (VS) = 300 kg VS/d Volume of organic waste = weight/density = 2000 (kg/d) / 1000 kg/m 3 = 2.0 m 3 /d Working volume of reactor (L ) = Flow rate (L/d) * RT (d) = 2000 x 24 = 48,000 L = 48 m 3 OLR at this volume = 300 (kg VS/d)/ 48 m 3 = 6.25 kg VS/ m 3 .d Working volume of reactor at OLR of 6.4 kg VS/m 3 .d = 48 x 6.25/6.4 = 46.88 m 3 Total volume: 46.88 x 100/75 = 62.5 m 3 115
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DRY ANAEROBIC DIGESTION OF MUNICIPA
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Abstract Global solid waste generat
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2.9 Characteristics of Digestates 3
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List of Tables Table Title Page 2.1
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4.20 Layout of conceptual decentral
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1.1 Background Chapter 1 Introducti
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The specific objectives of this res
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scale plants of the two processes i
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acetogens play their part to run th
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In dry anaerobic digestion, recycli
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process is inhibited and at that po
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eported, which increased with time,
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acids and increased downfall of pat
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performance of a poorly mixed (1 rp
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conventional low-solid system at th
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supply of the nutrients missing in
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2.6.2 Single-stage continuous syste
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single stage systems are DRANCO, Va
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of the solid content around 23% TS
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Substrate Feed TS (%) Reactor Type
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Second is that it has a high water
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2.9 Characteristics of Digestates D
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For instance, Mumme et al., (2010)
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Comparison of liquid and solid dige
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2.10 Management Aspects of Anaerobi
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Figure 2.11 Changing parameters dur
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amount of anaerobic fermentation re
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3.1 Inoculum and Simulations of Was
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ed pump, water circulating jacket,
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the reactor was increased from 35°
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parts (wt/wt bas is) of digestate c
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Sand drying bed (SDB) is simple, ea
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3.4.4 Estimation of GHG emissions i
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d) Calculation methods i) CH4 emiss
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Table 3.5 Analytical Methods for Va
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Biogas production 100X (NmL) Specif
Page 73 and 74: (i.e. 5.2 and 3.04 respectively, pl
Page 75 and 76: getting affected with the presence
Page 77 and 78: feedstock 2 is considered as a sudd
Page 79 and 80: 8.0) at most of the above said time
Page 81 and 82: Table 4.2 Surplus Energy of ITDAR D
Page 83 and 84: VFA 100 X (mg/L) VFA/Alk ratio 200
Page 85 and 86: the VFA concentration increased to
Page 87 and 88: The increase in GPR was almost line
Page 89 and 90: Based on our results, the best oper
Page 91 and 92: Based on this property of digestate
Page 93 and 94: Table 4.5. With curing of digestate
Page 95 and 96: application (after curing) in CH 4
Page 97 and 98: digestion, etc. Moreover, mixing of
Page 99 and 100: Figure 4.20 Layout of conceptual de
Page 101 and 102: Chapter 5 Conclusions and Recommend
Page 103 and 104: 5.2 Recommendations Following are t
Page 105 and 106: References Abdullahi, Y. A., Akunna
Page 107 and 108: Cengel, Y.A. (2003). Heat Transfer
Page 109 and 110: Forster-Carneiro, T., Pérez, M., R
Page 111 and 112: Kaparaju, P., Buendia, I., Ellegaar
Page 113 and 114: Liu, C., Yuan, X., Zeng, G., Li, W.
Page 115 and 116: Paavola, T. and Rintala, J. (2008).
Page 117 and 118: Stroot, P. G., McMahon, K. D., Mack
Page 119 and 120: Zeshan, Karthikeyan, O. P. and Visv
Page 121 and 122: Fruit and vegetable Waste Closer to
Page 123: Figure A-5 Sand drying bed for dewa
Page 127 and 128: The flow rate of 0.569 m 3 biogas/h
Page 129 and 130: Area for 910 kg dry solids = 910 (k
Page 131 and 132: = 280 m 3 /d x 0.000717 tons/m 3 (D
Page 133 and 134: Table C-1 Operational Parameters of
Page 135 and 136: Run Time GPR % CO2 % CH4 Methane Yi
Page 137 and 138: Appendix D Data of Phase II Pilot E
Page 139 and 140: Table D-3 Characteristics of Feed a
Page 141 and 142: Methodology Methodology for for Ene
Page 143 and 144: Q = Heat transfer rate or heat loss
Page 145: Calculation of GHG Emission Potenti
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