1. Introduction - Firenze University Press

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It should be mentioned that the total water flow and pressure difference in the network will grow. It means that more powerful pumps should be used. Electricity consumption will grow, but the heat savings will be bigger than the increase of pumping cost. Besides, in case of Tallinn, most of the pipes are oversized and the growth of pressure difference is not so rapid. 3.2. Heat production 3.2.<strong>1.</strong> Model description The model of current situation was built using the EnergyPro software. The components included in this model are shown in the Table 3. The model consists of three sites. Site 1includes 2 boiler houses operated during the heating season and a heat consumer. Site 2 includes a heat consumer, which is supplied by the heat produced in Site 1 and Site 3. Site 3 includes 2 energy units: the Tallinn CHPP where heat and electricity are cogenerated and Iru Plant where only two boilers are operated with no electricity generation. Besides, a heat consumer is included in Site 3. During the summer period only the Tallinn CHPP is operated supplying heat for hot water production to the whole district heating system. During the winter period all energy units are operated while the heat produced in Sites 1 and 3 is used to cover the heat demand of these sites and supplied to Site 2 also. The description of the model components is presented in Table 3. Table 3. Components of the Tallinn DH model Site 1 Heat sources Heat load Site 2 Heat sources Mustamäe boiler house Natural gas, heat capacity 100 MW, fuel input 106, working time, 15/09-15/05 Kadaka boiler house Natural gas, heat capacity 129 MW, fuel input 138, working time, 15/09-15/05 Site 2 When the boiler houses in Site 1 are shut down, heat is supplied via Site 2 Demand in Mustamäe District Annual heat demand is 693 GWh, 11% of the demand is hot water heating load, 89% of the demand depends linearly on ambient temperature during the heating period. The data on the ambient temperature in Tallinn for 2010 were used for simulation Site 2 During the heating period the heat produced in Mustamäe and Kadaka boiler houses is supplied to Site 2 Site 1 Heat produced in Site 1 (by Mustamäe and Kadaka boiler houses) during the heating season is supplied to Site 2 Site 3 Heat produced in Site 3 (by the Tallinn CHPP and Iru Plant) during the heating season and in summer supplied to Site 2 Heat load Demand in Kesklinna District Annual heat demand is 380 GWh, 11% of the demand is hot water heating load and 89% of the demand has a linear dependence on the ambient temperature during the heating period. The data on the ambient temperature in Tallinn for 2010 were used for the simulation. 319
Site 3 Heat sources Heat load Site 1 During the summer period, the heat supplied from Site 3 is distributed in Site 1 Tallinn CHPP Wood, heat capacity 65 MW, electrical capacity 25 MW, fuel input 125, working time year-round supply Iru Plant Natural gas, 353 MW Demand in Lasnamäe District Annual heat demand is 561 GWh, 11% of the demand is hot water heating load and 89% of the demand has a linear dependence on the ambient temperature during the heating period. The data on the ambient temperature in Tallinn for 2010 were used for simulation. Site 2 During the heating period and in summer the heat produced in Tallinn CHPP and Iru Plant is supplied to Site 2, during the summer time when other heat generation units are shut down, the heat is supplied via Site 2 to Site 3 Transmissions Transmission 1 Heat from Site 1 can be supplied to Site 2 and from Site 2 to Site 1, the maximum capacity 200 MW, loss 10% Transmission 2 Heat from Site 3 can be supplied to Site 2 and from Site 2 to Site 3, the maximum capacity 173 MW, loss 10% The sites of the model are shown in Figs 2 to 4. Fig. 2. Model of Tallinn district heating system, Site <strong>1.</strong> 320
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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
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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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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
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Page 317 and 318: 2.2.2. Pinch analysis Pinch analysi
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Page 331 and 332: A) Time Slices for solar thermal en
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Page 335 and 336: cTSs demand TS solar TSs 0 2 4 6 8
Page 337 and 338: In the presented paper a framework
Page 339 and 340: [5] Erdil E, Ilkan M, Egelioglu F.
Page 341 and 342: PROCEEDINGS OF ECOS 2012 - THE 25 T
Page 343 and 344: district energy network simulation
Page 345: were decreased by 10°C.All scenari
Page 349 and 350: 3.2.2. Input data and assumptions A
Page 351 and 352: Fig.7 shows the operation forecast
Page 353 and 354: [13] TERMIS Operation User Guide, 7
Page 355 and 356: Polygeneration is a term used to de
Page 357 and 358: The increase in energy utilization
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Page 361 and 362: 6. Extensions to core methodology 6
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Page 365 and 366: laterites. Ore Geology Reviews, v.
Page 367 and 368: Abstract: PROCEEDINGS OF ECOS 2012
Page 369 and 370: gasification [15], hybrid biomass g
Page 371 and 372: the second reactor. In this unit, s
Page 373 and 374: The variables effect was evaluated
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Page 377 and 378: Fig. 4. Effect of operating tempera
Page 379 and 380: SDG has slight effect on the syngas
Page 381: [26.] Castle WF. Air separation and
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1. Introduction - Firenze University Press

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