1. Introduction - Firenze University Press

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[8] Confidential Report on Lime Production, Nordkalk, May 2011 [9] Nduagu, E. Mineral carbonation: preparation of magnesium hydroxide [Mg(OH)2] from serpentinite rock. M.Sc. (Eng.) Thesis, Åbo Akademi University, Finland, 2008 [10] Nduagu, E., Björklöf, T., Fagerlund, J., Wärnå, J., Geerlings, H., Zevenhoven, R. Production of reactive magnesium from magnesium silicate for the purpose of CO2 mineralization. Part 1. Application to Finnish serpentinite. Minerals Engineering, 2012; 30:75-86 [11] Nduagu, E., Björklöf, T., Fagerlund, J., Mäkelä, E., Salonen, J., Geerlings, H., Zevenhoven, R. Production of reactive magnesium from magnesium silicate for the purpose of CO2 mineralization. Part 2. Mg extraction modeling and application to different Mg silicate rocks. Minerals Engineering, 2012; 30:87-94 [12] Fagerlund, J., Zevenhoven, R. An experimental study of Mg(OH)2 carbonation. Int. J. of Greenhouse Gas Control 2011; 5:1406-1412 [13] Fagerlund, J., Carbonation of Mg(OH)2 in a pressurised fluidised bed for CO2 sequestration PhD thesis, Åbo Akademi University, Turku Finland (2012) Available at: [14] Fagerlund, J., Zevenhoven, R. The effect of SO2 on CO2 mineral sequestration applied directly to a flue gas. Submitted to ECOS2012, Perugia, Italy, June 2012; paper under review [15] Romão, I., Nduagu, E., Fagerlund, J., M. Gando-Ferreira, L., Zevenhoven, R. CO2 Fixation Using Magnesium Silicate Minerals. Part 2: Energy Efficiency and Integration with Iron-and Steelmaking. Energy, 2012; 41:203-211 [16] Romão, I., Fagerlund, J., Gando-Ferreira, L. M., Zevenhoven, R. CO2 Sequestration with Portuguese serpentine. Proceedings of 3rd International Conference on Accelerated Carbonation for Environmental and Materials Engineering – ACEME10, 29 Nov - 1 Dec, 2010, Turku, Finland; 77-87; Ed. Ron Zevenhoven [17] Romão, I., Gando-Ferreira, L. M, Morais, I., Silva, M.V.G., Fagerlund, J., Zevenhoven, R., CO2 sequestration with Portuguese serpentinite and metaperidotite. 11th International Conference on Energy for a clean environment – CLEAN AIR 2011, 5-8th July [18] Bond, F:C:, The third Theory Communition, Trans AIME, 1952; 193: 484-494 115
Abstract: PROCEEDINGS OF ECOS 2012 - THE 25 TH INTERNATIONAL CONFERENCE ON EFFICIENCY, COST, OPTIMIZATION, SIMULATION AND ENVIRONMENTAL IMPACT OF ENERGY SYSTEMS JUNE 26-29, 2012, PERUGIA, ITALY Comparison of IGCC and CFB cogeneration plants equipped with CO2 removal Marcin Liszka a , Tomasz Malik b , Micha Budnik c , Andrzej Zibik d a Institute of Thermal Technology, Silesian University of Technology, 44-100 Gliwice, Konarskiego 22, Poland, marcin.liszka@polsl.pl, b Institute of Thermal Technology, Silesian University of Technology, 44-100 Gliwice, Konarskiego 22, Poland, tomasz.malik@polsl.pl, CA c Institute of Thermal Technology, Silesian University of Technology, 44-100 Gliwice, Konarskiego 22, Poland, michal.budnik@polsl.pl, d Institute of Thermal Technology, Silesian University of Technology, 44-100 Gliwice, Konarskiego 22, Poland, andrzej.ziebik@polsl.pl The introduction of CO2 removal processes into coal-fired power units causes usually generation of waste heat which is not possible to utilize within steam cycle. Normally, the waste heat is rejected to cooling water and then to the environment. As the temperature of waste heat carriers is usually moderately high (ca. 80 - 100C), there is a potential possibility for using them in district heating systems. The main goal of the present paper is thus the energy and CO2 emission analysis of large-scale CHP plants equipped with CO2 removal and utilizing waste heat generated within the plant. Two case studies have been formulated. First of them is dealing with the CFB plant equipped with a tap-backpressure steam turbine and post-combustion chemical CO2 absorption. The steam necessary for CO2 solvent (MEA) regeneration is taken from the steam turbine exhaust, while district heat is produced mainly in CO2 dehumidifier and CO2 compression train. The second case is dealing with an IGCC equipped with the pre-combustion CO2 removal by physical absorption. The district heat is then produced using classical final flue gas cooler located in HRSG, syngas cooler, as well as, compression trains of ASU air, nitrogen and CO2 product. For both analyzed cases, the peak-load district heat production using steam turbine extraction is also possible. Both CFB and IGCC plants have been modelled on the Thermoflex software. The reference, CFB-based CHP plant without CO2 removal has also been modelled. The district heat production and district water parameters have been fixed for all analyzed cases to the same values. The energy utilization factor, exergy efficiency and electricity-to-heat ratio have been calculated for both plants as main assessment factors. The methodology of alternative electricity production (equivalent power unit) has been involved for calculation of CO2 emissions. The obtained results indicates, that IGCC plant has better thermodynamic indicators than CFB-based unit. Moreover, the CO2 emission considering system interconnections within the electricity production network is negative for both the CFB and IGCC plants equipped with CCS. When comparing exergy efficiency, the highest value is achieved for the reference CFB plant (without CO2 capture). The decrease of exergy efficiency caused by CO2 capture and compression is ca. 8 percentage points, but in case of IGCC CHP plant the exergy efficiency plant is only 3 points lower than for the reference system. Keywords: IGCC, CFB, CHP, CCS, waste heat 1. Introduction The CO2 removal processes integrated with coal-fired power units cause significant drop of energy efficiency and economic profitability of the overall power generation process. The decrease of power generation efficiency is externalized usually by increased amount of waste heat rejected to the environment. The waste heat coming from the CO2 removal and compression installations is often of moderate temperature (ca. 80-100C), and therefore its utilization within the power cycle or for external purposes could be possible. On the other hand, the decrease of CO2 emission without its removal is also possible. The combined heat and power production (CHP) is a good example 116
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Proceedings e report 90
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ECOS 2012 : the 25 th International
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Advisory Committee (Track Organizer
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The 25 th ECOS Conference 1987-2012
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VOLUME VI CONTENT VI. 1 CARBON CAPT
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-----------------------------------
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» Personal transportation energy c
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» Excess enthalpies of second gene
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VOLUME IV IV . 1 - FLUID DYNAMICS A
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» Exergy analysis and genetic algo
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» Optimal lighting control strateg
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» Stability and limit cycles in an
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PROCEEDINGS OF ECOS 2012 - THE 25 T
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Fig. 2. The exergy destruction of M
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ineffectiveness of the catalyst, in
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[ P EXmth EX SNG] ESR F where EXm
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Fuel inputkW 728221 203771 237719 3
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Not only at desined Rc (the ratio o
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4. DISCUSSION The graphic exergy an
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Figure 9(a) illustrates the energy
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Engineering Technical Conferences &
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generally there are four kinds of m
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However, even under the off-design
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Fig. 3. 600MW supercritical coal-fi
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CO2 rich loading(molCO2/molMEA) 0.4
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Net efficiency (%) 40.28 30.29 26.4
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Fig. 11. Schematic diagram of heat
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28.67%. In addition, through heat i
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Applied Thermal Engineering 2010;30
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Abstract: PROCEEDINGS OF ECOS 2012
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Fig. 1. Solution diagram of „four
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K ~ K 1 eK 1a p K 1a iK mK
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Oxygen recovery rate, % 105 95 85 7
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Calculated optimal compressor press
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The net amount of the flue gas leav
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Figure 3. Idea for lignite drying b
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Energy efficiency, % 34,00 33,00 32
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points efficiency increase related
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Figure A1b. Thermoflex flow sheet o
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Figure A3a. Thermoflex flow sheet o
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Figure A4. Thermoflex flow sheet of
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2.1. Life Cycle Assessment 2.1.1. G
Page 92 and 93: these factors. A sensitivity analys
Page 94 and 95: methane slip contributes to 13% of
Page 96 and 97: As can be seen in Fig. 5 the impact
Page 98 and 99: References [1] Eurobserv’er, The
Page 100 and 101: PROCEEDINGS OF ECOS 2012 - THE 25 T
Page 102 and 103: in which CO2 is separated from H2,
Page 104 and 105: dimensions of water droplets and wa
Page 106 and 107: Temperature (°C) 8 7 6 5 4 3 2 1 0
Page 108 and 109: 4. Conclusions In the present paper
Page 110 and 111: Abstract: PROCEEDINGS OF ECOS 2012
Page 112 and 113: penalty, but without separate captu
Page 114 and 115: 0.5 - 0.7 kg/kg, resulting typicall
Page 116 and 117: 3.3 - Utilising waste heat All exis
Page 118 and 119: 4.5 - Suomusjärvi olivine deposits
Page 120 and 121: material will change from a few % t
Page 122 and 123: Fig. 5 Schematic diagram of the PFB
Page 124 and 125: 8. Combined SO2 capture and CO2 min
Page 126 and 127: Fig. 10 Carbonate- (left) and sulph
Page 128 and 129: [13] Ekdahl, E., Idman, H. Statemen
Page 132 and 133: HEAT Fig. 1. Scheme and main reacti
Page 134: (raw) materials pre-heating and AS
Page 137 and 138: Fig 3- Aspen Plus® model 110
Page 139 and 140: Table 4. Elemental and XRD analysis
Page 141: the ÅA CSM route. The content of M
Page 145 and 146: moisture - 0,2237 ash - 0,0876 LHV
Page 147 and 148: 2.2 CFB plant For the current momen
Page 149 and 150: The CO2 emission factor which indic
Page 151 and 152: The CO2 emission factor calculated
Page 153 and 154: Appendix A Fig A.1. Simulation mode
Page 155 and 156: (b) Fig. A.2. Simulation model of C
Page 157 and 158: Table A.1. Calculated parameters at
Page 159 and 160: References [1] Pfaff I., Oexmann J.
Page 161 and 162: with a CC installation could be avo
Page 163 and 164: 2.3. Basic CHP plant indices. The b
Page 165 and 166: 3. Off-design calculations The main
Page 167 and 168: Fig. 6. CHP plant efficiency Fig. 7
Page 169 and 170: amount of steam delivered to the he
Page 171 and 172: [5] Lukowicz H., Mroncz M.: Analysi
Page 173 and 174: water removal is feasible by coolin
Page 175 and 176: Figure 2. Sketch of the suggested P
Page 177 and 178: a b Figure 5. a) Exergy balance of
Page 179 and 180: The basis of comparison of each met
Page 181 and 182: Figure 7a. Impact of S/CATR on PCU
Page 183 and 184: However, more energy duty is requir
Page 187 and 188: 3.1. JACOBIAN-ASPEN Interface ASPEN
Page 189 and 190: Fig. 3. Triple Pressure Bottoming S
Page 191 and 192: As seen from Table 1, the mass flow
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4. Conclusion Fig. 5. Partial Emiss
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[19] Yantovski E., Shokotov M., Sho
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investigation and the developing of
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University of L’Aquila and German
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hydrogen combustion technology at d
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eversibility of a pre-treated synth
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Fig. 1. TG curves collected for spe
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(see Fig 5). Carbon dioxide uptake
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period is reduced to the first 15 c
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CO2 capture capacity up to 150 th c
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the way for biogas utilisation is t
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projectand is described in the foll
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4. Pilot plant tests In order to de
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Concerning the absorption reaction,
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with Regeneration (AwR), consists i
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[25] Aspen Plus 2004.1. Cambridge,
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systems for fuel drying waste strea
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heated in a heat exchanger placed i
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Fig. 2. Lower heating value of fuel
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Acknowledgements The results presen
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large amount of CO2 [1,5-7]. APCr a
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N 1 i ( x x i n 1 m ) 2.3. Carbon
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DTA analysis of the untreated APCrs
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Table 4. Relative Error (%) of the
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CaO HCl CaCl H O 193kJ / mol (
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[1] M. Fernández Bertos, S.J.R. Si
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2. Process development 2.1. Backgro
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to dissolve the chloride salts prec
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The remaining 25% (5 ml/min) of the
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Table 6. Experimental conversions o
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p p 1 1. 5 p H 1 1. 5 2O p mi
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Calculating from the Aspen Plus mod
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[11] Mattila, H.-P., Experimental s
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Mg2SiO4(s) + 2CO2(g) →2MgCO3(s) +
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(Mg/Fe) of the mineral rock, Mg-sil
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Figure 2. Effect of Mg/Fe ratio of
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Figure 4 shows that an increase in
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Figure 5. Process flow diagram of M
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2. Only cold utility is needed belo
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extraction process at 400 °C (~ 62
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Table A2. Extraction equations and
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[13] Teir S, Kuusik R, Fogelholm CJ
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In the area of coal technologies al
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Tabel 1. Characteristics quantities
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N m eT 4a ~ T cp T4a 1 ( K
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Auxiliary power rate of ASU, % 40 4
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[8] Buhre B.J.P., Elliott L.K., She
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1.1 - Cement Manufacturing The ceme
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2. Numerical model The purpose of t
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-0.309x15.77x2 2.085x3 240x4 12.53x
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Table 4 - Results of the optimizati
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1. Define the studied system (in th
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cycle) or a lignin extraction plant
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limiting factor for the maximum siz
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Table 5. Key data for the four ener
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Global CO 2 emissions [ktonnes/yr]
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for biofuels and the investment cos
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The possibility to capture CO2 from
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[17] Berglin N, Andersson L. Proces
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Therefore NL Agency (an agency of t
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2.2.2. Pinch analysis Pinch analysi
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3. Case study 3.1. Plant and proces
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Te 1000 mp era 900 tur 800 e [°C 7
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Application of the approach led to
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The advantage of dynamic models is
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e equal at both time intervals and
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2.5. Selecting the number of TSs Se
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A) Time Slices for solar thermal en
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The first step of procedure is to p
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cTSs demand TS solar TSs 0 2 4 6 8
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In the presented paper a framework
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[5] Erdil E, Ilkan M, Egelioglu F.
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district energy network simulation
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were decreased by 10°C.All scenari
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Site 3 Heat sources Heat load Site
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3.2.2. Input data and assumptions A
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Fig.7 shows the operation forecast
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[13] TERMIS Operation User Guide, 7
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Polygeneration is a term used to de
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The increase in energy utilization
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are available for an entire year, 8
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6. Extensions to core methodology 6
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thermal storage and possible suppor
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laterites. Ore Geology Reviews, v.
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gasification [15], hybrid biomass g
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the second reactor. In this unit, s
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The variables effect was evaluated
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atio, as well as the shift-syngas f
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Fig. 4. Effect of operating tempera
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SDG has slight effect on the syngas
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[26.] Castle WF. Air separation and
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1. Introduction - Firenze University Press

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