1. Introduction - Firenze University Press

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GateCycle TM software. The built-in components were used to build the integrated model. It was assumed that through the membrane flows pure oxygen. The auxiliary power rate of steam cycle, the live steam thermodynamic parameters, reheated steam thermodynamic parameters, mass flow rates of live steam and reheated steam were assumed as for a 460 MW power plant. The gross power of steam turbine is constant, despite electricity generated in the air separation unit. Energy consumption of the carbon dioxide capture unit was calculated with use of the model of carbon dioxide capture unit. The structure of this model is shown in Figure 3. The energy consumption value is correct for the specific composition of the flue gas. Rys.3. Scheme of the carbon dioxide capture unit (CC) 3. The results of calculations of air separation unit integrated with the oxy type pulverized boiler The air mass flow rate depends on the separated in membrane oxygen mass flow rate ( m O2 ), oxygen recovery rate (R) and mass content of oxygen in the air ( g O2air ). The relationship between these quantities is as follows: m O2 m 1a (1) R g O2air Next the air is flowing to the compressor. Effective power required to drive the compressor depends on the air mass flow rate ( 1a m ), the air temperature ( ~c 1a ), the 255 T ), the average specific heat ( p K 1 compressor pressure ratio ( K ), the heat capacity ratio contained in the factor ( K ), K the compressor isentropic efficiency ( iK ) and the compressor mechanical efficiency ( mK ). The equation showing the relationship between these quantities is as follows: N m eK 1a K ~ K 1 c T p K 1a iK mK (2) The mass flow rate of gas flowing through the expander is lower than the mass flow rate of gas flowing through the compressor. This mass flow rate depends on the oxygen mass flow rate separated from the air in the membrane ( m O2 ) and the air flow rate ( m 1a ).The relationship between these quantities is as follows: m m m 4a 1a O2 (3) The expander effective power depends on the retentate mass flow rate ( a m 4 ), the retentate temperature ( T 4a ), the average specific heat (~c p ), the compressor pressure ratio ( K K ), the reduction factor of compressor pressure ratio ( ), the heat capacity ratio contained in the factor 1 ( T ), the expander isentropic efficiency ( iT ) and the expander mechanical efficiency T ). The equation showing the relationship between these quantities is as follows: ( mT
N m eT 4a ~ T cp T4a 1 ( K) iT mT T The gross electrical power of the air separation unit depends on the expander gross power ( N eT ), the compressor gross power ( N eK ) and the generator efficiency ( g ). The relationship between these quantities is as follows: N elTG N eT eK g N (5) Figure 4 shows a graph of boiler thermal efficiency as a function of oxygen recovery rate of the air separation unit. It should be noted that the boiler thermal efficiency increases from about 55% for low oxygen recovery rates to about 83% for high recovery rates. The boiler thermal efficiency depends on the live steam flow rate ( 6s m ), the reheated steam flow rate ( m 8s ), the enthalpy of live seam leaving the boiler ( 6s h ), the enthalpy of feed water at inlet to the boiler ( h 2s ), the enthalpy of reheated steam leaving the boiler ( h 8s ),the enthalpy of reheated steam at the inlet to the boiler ( h 7s ), the fuel mass flow rate ( 1c m ) and fuel lower heating value ( W dp ). The equation showing the relationship between these quantities can be written as: m 6s h6s h2 s m 8s h8s h7s k (6) m W Boiler thermal efficiency, % 85 80 75 70 65 60 1c dp 55 40 45 50 55 60 65 70 75 80 85 90 95 100 Oxygen recovery rate, % Fig.4. Thermal efficiency of the oxy type boiler as a function of the air separation unit oxygen recovery rate The thermal efficiency of steam cycle depends on the heat supplied to the steam cycle ( d Q ) and the heat discharged from the steam cycle ( w Q ).The relationship between these quantities is as follows: Q Q d w obp Q (7) d The gross efficiency of electricity generation is calculated in terms of the generator electrical power driven by the steam turbine. The electricity generated in other units is included in their auxiliary recovery rates. The gross efficiency of electricity generation depends on the steam turbine electrical power ( el 256 N ), the fuel flow rate ( 1c m ) and lower heating value ( W dp ).The equation showing the relationship between these quantities can be written as: (4)
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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
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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
Page 231 and 232: Acknowledgements The results presen
Page 233 and 234: large amount of CO2 [1,5-7]. APCr a
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
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Page 275 and 276: Table A2. Extraction equations and
Page 277 and 278: [13] Teir S, Kuusik R, Fogelholm CJ
Page 279 and 280: In the area of coal technologies al
Page 281: Tabel 1. Characteristics quantities
Page 285 and 286: Auxiliary power rate of ASU, % 40 4
Page 287 and 288: [8] Buhre B.J.P., Elliott L.K., She
Page 289 and 290: 1.1 - Cement Manufacturing The ceme
Page 291 and 292: 2. Numerical model The purpose of t
Page 293 and 294: -0.309x15.77x2 2.085x3 240x4 12.53x
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
Page 301 and 302: cycle) or a lignin extraction plant
Page 303 and 304: limiting factor for the maximum siz
Page 305 and 306: Table 5. Key data for the four ener
Page 307 and 308: Global CO 2 emissions [ktonnes/yr]
Page 309 and 310: for biofuels and the investment cos
Page 311 and 312: The possibility to capture CO2 from
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
Page 321 and 322: Te 1000 mp era 900 tur 800 e [°C 7
Page 323 and 324: Application of the approach led to
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Page 327 and 328: e equal at both time intervals and
Page 329 and 330: 2.5. Selecting the number of TSs Se
Page 331 and 332: 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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