1. Introduction - Firenze University Press

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Heat production (GWh) 1,854.60 1,857.30 Tallinn CHPP 438.00 438.00 Incineration plant CHP 278.40 Mustamäe boiler house 71<strong>1.</strong>00 667.10 Kadaka boiler house 394.40 354.70 Iru Plant 31<strong>1.</strong>20 119.10 Electricity production (GWh) 219.00 313.60 Tallinn CHPP 219.00 219.00 Incineration plant CHP 94.66 Fuel consumption (GWh) 2,314.00 2,467.40 Natural gas 1,438.00 1,144.80 Wood 876.00 876.00 Waste 446.60 Working hours Tallinn CHPP 8760 8760 Incineration plant CHP 5568 Mustamäe boiler house 5616 5616 Kadaka boiler house 5064 4008 Iru Plant 5136 2544 The year-round operation of the system is shown graphically in Fig. 6. Fig. 6 shows that Tallinn CHPP operates all year round. The Mustamäe boiler house operates during all the heating period, but Kadaka boiler house and Iru Plant are used for peak loads. Fig. 6. Heat load of Tallinn District Heating Network. Simulation of the current situation. 323
Fig.7 shows the operation forecast for the second scenario when the incineration plant is added. The Tallinn CHPP operates all year round. The incineration plant works during all the heating period at full load. The Mustamäe boiler house operates during all the heating period, but at partial load. The Kadaka boiler house and Iru Plant work less than in the first scenario. Fig.7. Heat load of Tallinn District Heating Network. Simulation of the scenario with an additional waste incineration plant. Conclusion The reliability and cost-efficiency of district heating depends on the efficiency of its operation. In this paper a methodology for the assessment and efficiency increasing of heat production and distribution was offered. As a case study, the Tallinn district heating system was analysed. The Tallinn district heating system includes 4 heat plants, which cover the heat demand in 3 districts. For the evaluation of district heating network, a model was created using the TERMIS software. For the heat loss analysis and hydraulic analysis, four different scenarios were simulated: the current situation, decreased maximum flow temperature by 15°C, decreased consumption by 20% and decreased temperature by 20°C with the decreased consumption by 20%. As a result, the decreasing of relative heat loss by 23.2GWh during the heating season compared to the current situation was gained. For the evaluation of energy production, a model was created using the EnergyPro software. The system was split into three sites. This model was used for the simulation of two scenarios: the current situation and the case where anew incineration cogeneration plant will be installed. The actual data for the last years were used for the simulation. The results of simulation showed that according to the current situation, the cogeneration plant should work all year round, the boiler houses should operate during the heating period and the Iru Plant boiler should be used only for the peak heat load. In case when the incineration plant is added, it can operate at full load during more than 5500 hours per year. Heat generation in this plant will decrease the consumption of natural gas 324
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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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Table 4 - Results of the optimizati
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Page 337 and 338: In the presented paper a framework
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Page 341 and 342: PROCEEDINGS OF ECOS 2012 - THE 25 T
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Page 345 and 346: were decreased by 10°C.All scenari
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Page 353 and 354: [13] TERMIS Operation User Guide, 7
Page 355 and 356: Polygeneration is a term used to de
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Page 361 and 362: 6. Extensions to core methodology 6
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Page 367 and 368: Abstract: PROCEEDINGS OF ECOS 2012
Page 369 and 370: gasification [15], hybrid biomass g
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1. Introduction - Firenze University Press

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