1. Introduction - Firenze University Press

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appears to be due to thermal decomposition of ammonium sulfate leading to the formation of sulfur oxide(s), which could alter the thermodynamics of the extraction reactions. The application of pinch analysis and the heat exchanger network as implemented in an Aspen Plus model resulted in a ~ 0.5 Gt/t-CO2 (~ 10% points) reduction in the exergy requirement of producing Mg(OH)2. When the Mg(OH)2 production and carbonation units are integrated the process requirements of the process becomes 3.88 Gt/t-CO2. Carbonating Mg(OH)2 in the carbonation unit provides a ~17% points energy offset to the entire process. The overall energy requirement of the process reduces by another ~0.5 GJ/t-CO2 if the compound form of Fe in mineral is assumed to be FeO instead of the Fe2O3 used here. Acknowledgements This work was supported by the Academy of Finland program “Sustainable Energy” (2008-2011). Further support came from KH Renlund Foundation (2007-2009). Financial support from Åbo Akademi University’s Graduate School for Chemical Engineering (GSCE) is also acknowledged. Appendix Apendix A - Tables Table A1 . Composition of magnesium silicate minerals tested. Elemental composition (%-wt) Mg/Fe Rock type and locations Mg Fe Si Ca Al (kg/kg) Serpentinite rocks N.S. Wales serp. (Aus) 23.0 4.80 19.5 0.00 0.50 4.8 Donia serp. (Portugal) 22.0 5.01 19.4 0.18 0.88 4.4 7 Fontes serp. (Portugal) 23.3 5.77 19.5 0.09 1.02 4.0 Bragança serp. (Portugal) 21.6 5.70 19.6 0.00 0.60 3.8 Finnish serp. (Fin) 21.8 10.1 11.6 0.30 0.00 2.2 Lithuania serp. (Lit) 18.9 12.3 15.9 0.90 0.10 1.5 Olivine rocks Åheim olivine (Nor) 29.6 5.00 19.5 0.10 2.80 5.9 Suomusjärvi-2 (Fin) 12.60 8.32 20.71 5.93 3.71 1.5 Vammala-2 (Fin) 16.88 12.87 18.37 1.00 0.69 1.3 Vammala-1 (Fin) 11.58 10.77 21.03 6.43 1.85 1.1 Suomusjärvi-1(Fin) 8.14 7.62 23.46 5.57 5.72 1.1 Satakunta olivine (Fin) 3.30 10.7 21.9 6.30 8.50 0.3 Reactions (A1)-(A5) represent the thermodynamics of reactions involving Mg3Si2O5(OH)4, Fe- and Ca-based compounds; iron could be found as FeO/Fe2O3/Fe3O4 and calcium is present as CaSiO3[16, 17]. It can be seen from the thermodynamic compositions of possible products of the reactions (see also Fig.B1) that MgSO4 is the dominant solid product of the reaction. 247
Table A2. Extraction equations and thermodynamics # Extraction reactions (A1) (A2) (A3) (A4) (A5) Appendix B – Figures 248 T (K) ∆G
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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
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these factors. A sensitivity analys
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methane slip contributes to 13% of
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As can be seen in Fig. 5 the impact
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References [1] Eurobserv’er, The
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in which CO2 is separated from H2,
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dimensions of water droplets and wa
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Temperature (°C) 8 7 6 5 4 3 2 1 0
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4. Conclusions In the present paper
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penalty, but without separate captu
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0.5 - 0.7 kg/kg, resulting typicall
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3.3 - Utilising waste heat All exis
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4.5 - Suomusjärvi olivine deposits
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material will change from a few % t
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Fig. 5 Schematic diagram of the PFB
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8. Combined SO2 capture and CO2 min
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Fig. 10 Carbonate- (left) and sulph
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[13] Ekdahl, E., Idman, H. Statemen
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HEAT Fig. 1. Scheme and main reacti
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(raw) materials pre-heating and AS
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Fig 3- Aspen Plus® model 110
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Table 4. Elemental and XRD analysis
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the ÅA CSM route. The content of M
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moisture - 0,2237 ash - 0,0876 LHV
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2.2 CFB plant For the current momen
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The CO2 emission factor which indic
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The CO2 emission factor calculated
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Appendix A Fig A.1. Simulation mode
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(b) Fig. A.2. Simulation model of C
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Table A.1. Calculated parameters at
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References [1] Pfaff I., Oexmann J.
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with a CC installation could be avo
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2.3. Basic CHP plant indices. The b
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3. Off-design calculations The main
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Fig. 6. CHP plant efficiency Fig. 7
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amount of steam delivered to the he
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[5] Lukowicz H., Mroncz M.: Analysi
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water removal is feasible by coolin
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Figure 2. Sketch of the suggested P
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a b Figure 5. a) Exergy balance of
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The basis of comparison of each met
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Figure 7a. Impact of S/CATR on PCU
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However, more energy duty is requir
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3.1. JACOBIAN-ASPEN Interface ASPEN
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Fig. 3. Triple Pressure Bottoming S
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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
Page 223 and 224: [25] Aspen Plus 2004.1. Cambridge,
Page 225 and 226: systems for fuel drying waste strea
Page 227 and 228: heated in a heat exchanger placed i
Page 229 and 230: Fig. 2. Lower heating value of fuel
Page 231 and 232: Acknowledgements The results presen
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Page 235 and 236: N 1 i ( x x i n 1 m ) 2.3. Carbon
Page 237 and 238: DTA analysis of the untreated APCrs
Page 239 and 240: Table 4. Relative Error (%) of the
Page 241 and 242: CaO HCl CaCl H O 193kJ / mol (
Page 243 and 244: [1] M. Fernández Bertos, S.J.R. Si
Page 245 and 246: Abstract: PROCEEDINGS OF ECOS 2012
Page 247 and 248: 2. Process development 2.1. Backgro
Page 249 and 250: to dissolve the chloride salts prec
Page 251 and 252: The remaining 25% (5 ml/min) of the
Page 253 and 254: Table 6. Experimental conversions o
Page 255 and 256: p p 1 1. 5 p H 1 1. 5 2O p mi
Page 257 and 258: Calculating from the Aspen Plus mod
Page 259 and 260: [11] Mattila, H.-P., Experimental s
Page 261 and 262: Mg2SiO4(s) + 2CO2(g) →2MgCO3(s) +
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Page 265 and 266: Figure 2. Effect of Mg/Fe ratio of
Page 267 and 268: Figure 4 shows that an increase in
Page 269 and 270: Figure 5. Process flow diagram of M
Page 271 and 272: 2. Only cold utility is needed belo
Page 273: extraction process at 400 °C (~ 62
Page 277 and 278: [13] Teir S, Kuusik R, Fogelholm CJ
Page 279 and 280: In the area of coal technologies al
Page 281 and 282: Tabel 1. Characteristics quantities
Page 283 and 284: N m eT 4a ~ T cp T4a 1 ( K
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Page 291 and 292: 2. Numerical model The purpose of t
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Page 295 and 296: Table 4 - Results of the optimizati
Page 297 and 298: PROCEEDINGS OF ECOS 2012 - THE 25 T
Page 299 and 300: 1. Define the studied system (in th
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Page 305 and 306: Table 5. Key data for the four ener
Page 307 and 308: Global CO 2 emissions [ktonnes/yr]
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Page 313 and 314: [17] Berglin N, Andersson L. Proces
Page 315 and 316: Therefore NL Agency (an agency of t
Page 317 and 318: 2.2.2. Pinch analysis Pinch analysi
Page 319 and 320: 3. Case study 3.1. Plant and proces
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Page 323 and 324: 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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