1. Introduction - Firenze University Press

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[ P EXmth EX SNG] ESR F where EXmth and EXSNG represents the exergy output of methanol and SNG respectively, kW. The performance of the new polygeneration system and the reference systems is simulated by Aspen Plus software. The thermodynamic properties of syngas and chemicals are calculated by the Peng-Robinson and Redlich-Kwong equations respectively. The key parameters in the polygeneration system are selected to agree with the reference systems. For example, the inlet temperature of gas turbine is 1200, the pressure ratio is 16.5, and the isentropic efficiency for gas turbine, high-pressure, middle-pressure and low-pressure steam turbines are selected to be 0.9, 0.88, 0.89 and 0.86 respectively. Datong coal was assumed as the basis for this study, whose LHV is 26,710 kJ/kg. The coal analysis data along with some other basic conditions for simulation are listed in table 1. Table 1. Basic condition for simulation C f H f 7 (3) Coal component analysis (weight %) 68.54 3.97 6.85 0.74 1.08 Ash f W f 9.98 8.84 O f Condition for gas turbine parameter value Inlet temperature () N f S f 1200 Pressure ratio 16.5 Isentropic efficiency 0.9 Inlet temperature () Inlet pressure High/Middle/Low (bar) Isentropic efficiency High/Middle/Low pressure Pinch temperature difference of HRSG () Condition for steam cycle 535 120/39/3.75 0.88/0.89/0.86 17
The stream data corresponding to the points indicated in Figure 4 is listed in Table 2. The simulation results of the polygeneration system and its reference systems are summarized in Table 3. Table 2. Stream data for the flow sheet in Figure 4 1 2 3 4 5 6 7 8 9 10 13 14 15 Pressure(bar) 68.0 27.4 74.5 74.5 74.5 80.0 77.7 77.7 4.9 16.4 1.1 77.7 30.0 Temperature() 1346 51 40 40 40 423 25 25 92 1200 66 25 40 Flow rate (mol/s) Mole fraction,% 2763 2088 169 523 1045 5301 279 6 2.8 4967 163 273 957 CO 44.0 27.0 0.3 24.3 24.3 4.3 0.1 1.5 0.1 CO2 11.7 0.9 0.7 1.6 1.6 2.9 5.4 2.2 34.1 3.0 5.5 99.9 H2 30.5 71.6 0.3 73.4 73.4 14.1 0.2 0.7 0.2 CH4 38.7 91.4 4.3 93.2 COS 0.6 H2S 0.3 H2O 12.6 0.4 1.7 38.7 0.1 6.0 0.2 8.2 0.1 N2 0.3 0.2 74.5 0.2 O2 14.3 CH4O 97 0.6 0.6 1.1 2.4 87.3 58.7 99.8 0.7 C2H6O 0.1 0.1 0.2 4.7 0.1 Others 0.1 Table 3. The performance of the polygeneration (PG) system Items PG with 8 Reference systems CO2 capture IGCC Single methanol Single SNG process process
Page 1: Proceedings e report 90
Page 4 and 5: ECOS 2012 : the 25 th International
Page 7 and 8: Advisory Committee (Track Organizer
Page 10 and 11: The 25 th ECOS Conference 1987-2012
Page 12 and 13: VOLUME VI CONTENT VI. 1 CARBON CAPT
Page 14 and 15: -----------------------------------
Page 16 and 17: » Personal transportation energy c
Page 18 and 19: » Excess enthalpies of second gene
Page 20 and 21: VOLUME IV IV . 1 - FLUID DYNAMICS A
Page 22 and 23: » Exergy analysis and genetic algo
Page 24 and 25: » Optimal lighting control strateg
Page 26 and 27: » Stability and limit cycles in an
Page 28 and 29: PROCEEDINGS OF ECOS 2012 - THE 25 T
Page 30 and 31: Fig. 2. The exergy destruction of M
Page 32 and 33: ineffectiveness of the catalyst, in
Page 36 and 37: Fuel inputkW 728221 203771 237719 3
Page 38 and 39: Not only at desined Rc (the ratio o
Page 40 and 41: 4. DISCUSSION The graphic exergy an
Page 42 and 43: Figure 9(a) illustrates the energy
Page 44 and 45: Engineering Technical Conferences &
Page 46 and 47: generally there are four kinds of m
Page 48 and 49: However, even under the off-design
Page 50 and 51: Fig. 3. 600MW supercritical coal-fi
Page 52 and 53: CO2 rich loading(molCO2/molMEA) 0.4
Page 54 and 55: Net efficiency (%) 40.28 30.29 26.4
Page 56 and 57: Fig. 11. Schematic diagram of heat
Page 58 and 59: 28.67%. In addition, through heat i
Page 60 and 61: Applied Thermal Engineering 2010;30
Page 62 and 63: Abstract: PROCEEDINGS OF ECOS 2012
Page 64 and 65: Fig. 1. Solution diagram of „four
Page 66 and 67: K ~ K 1 eK 1a p K 1a iK mK
Page 68 and 69: Oxygen recovery rate, % 105 95 85 7
Page 70 and 71: Calculated optimal compressor press
Page 72 and 73: PROCEEDINGS OF ECOS 2012 - THE 25 T
Page 74 and 75: The net amount of the flue gas leav
Page 76 and 77: Figure 3. Idea for lignite drying b
Page 78 and 79: Energy efficiency, % 34,00 33,00 32
Page 80 and 81: points efficiency increase related
Page 82 and 83: 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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Abstract: PROCEEDINGS OF ECOS 2012
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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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PROCEEDINGS OF ECOS 2012 - THE 25 T
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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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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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