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Appendix E Methodology for Calculation of Energy Balance 130
Methodology Methodology for for Energy Energy Balance Balance Calculation Calculation of of Inclined Inclined Reactor The The energy energy balance balance of of inclined inclined reactor reactor is is based based on on its energy consumption and energy production. production. Energy Energy is is required required for for shredding shredding the the waste waste (ES), waste feeding and withdrawal (EFW), (EFW), re-circulation re-circulation of of reactor reactor content content (ER) (ER) and and heating heating (EH) which includes energy for heating heating the the substrate substrate (EHS) (EHS) as as well well as as energy energy for for maintaining constant thermophilic temperature temperature (EMT). (EMT). The The production production of of energy energy (EP) (EP) is only from the methane produced. Method Method for for calculation calculation of of each each type type of of these these energies energies has been given in the following section. section. The The net net energy energy production production NEP NEP (MJ) (MJ) is is the the difference difference between the energy produced and consumed consumed by by the the process process that that is is shown shown in in Figure Figure 1 1 and and given by the following equation: Feeding Feeding Withdrawal Withdrawal Recirculation Recirculation Shredding Shredding Heating Heating NEP NEP = = EP EP - - ES ES – – EFW EFW – – ER – EH Figure Figure E-1 E-1 Energy Energy inputs inputs and and output output of of inclined anaerobic digester 1.1 1.1 Energy Energy Production Production The The energy energy production production EP EP (MJ) (MJ) equivalent equivalent to to methane methane and hydrogen content of the produced produced biogas biogas can can be be calculated calculated by by the the equation equation below. below. EP EP = = (MP (MP X X L.H.V. L.H.V. of of CH4) CH4) + + (HP (HP X L.H.V. of H2) where where MP MP = = methane methane production production (L (L CH4) CH4) L.H.V. L.H.V. of of CH4= CH4= 0.03618 0.03618 MJ/L MJ/L CH4 CH4 CH4 (Ruggeri (Ruggeri et et al., al., 2010) 2010) HP HP = = Hydrogen Hydrogen production production (L (L H2) H2) L.H.V. L.H.V. of of H2 H2 H2 = = 0.0108 0.0108 MJ/L MJ/L H2 H2 H2 (Ruggeri (Ruggeri et et al., al., 2010) 2010) 1.2 1.2 Energy Energy Consumption Consumption Energy Energy consumption consumption has has been been described described under under sub-categories sub-categories as follows: 1.2.1 1.2.1 Energy Energy required required for for shredding shredding (ES) (ES) The The assumption assumption here here is is that that about about 100 100 kg kg of of waste waste is is shredded by the use of 0.5 L gasoline. 131 131 Biogas
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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
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(i.e. 5.2 and 3.04 respectively, pl
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getting affected with the presence
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feedstock 2 is considered as a sudd
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8.0) at most of the above said time
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Table 4.2 Surplus Energy of ITDAR D
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VFA 100 X (mg/L) VFA/Alk ratio 200
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the VFA concentration increased to
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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 and 124: Figure A-5 Sand drying bed for dewa
Page 125 and 126: Assumptions Size of the community:
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: Table D-3 Characteristics of Feed a
Page 143 and 144: Q = Heat transfer rate or heat loss
Page 145: Calculation of GHG Emission Potenti
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