1. Introduction - Firenze University Press

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The net amount of the flue gas leaving the boiler island is of high CO2 concentration (ca 82,5 %vol), however further inert gas separation (mainly O2 and N2) is necessary. Inert gas separation line is of cryogenic type. The inert gas separation line has not been physically modelled within the current paper as it is not related to the analysed waste heat recovery systems. After [3], it has been just assumed that there is some required flue gas pressure before the cryogenic separation unit. The flue gas pressure drop within the separation installation, as well as, separation effectiveness have also been assumed as constant values. The auxiliary power consumption related to inert gas separation is determined as power of flue gas compressors. Finally, the CO2 content in flue gas leaving the oxy-fuel system is nearly 96% and is the same as reported in [3]. The steam cycle is of single reheat supercritical design. Its structure and parameters represent the best available technology for today plants – the parameters of live / reheated steam are: 600OC, 28,5MPa / 620OC, 5MPa. 2.2 Heat recovery from the flue gas to combustion oxygen (Case 2) The idea of case 2 has been shown in Fig. 1, where the oxygen heater has been added between ASU and boiler. The oxygen taken from ASU exhaust is preheated up to 260 0 C by the flue gas flowing within the main recirculation loop. The detailed flow sheet of Case 2 has been presented in Fig. A2 in appendix A. The steam cycle is the same as for the reference case, so the Fig. A1b in appendix A refers also to case 2. Figure <strong>1.</strong> Idea for heat recovery from the flue gas to combustion oxygen (case 2) 2.3 Heat recovery from the flue gas compression train to steam cycle (Case 3) The idea for heat recovery from the flue gas compression train to steam cycle which is the essence of case 3 is presented in Fig. 2. Recovered heat replaces the LP heat regeneration within the steam cycle in ca 70%. The detailed flow sheet of Case 3 has been presented in Fig. A3a and A3b in appendix A. 47
Figure 2. Idea for heat recovery from the flue gas compression train to steam cycle (case 3) Comparing to the reference case, the additional flue gas coolers located behind appropriate compression stages have been added. The cooling media within these new coolers is steam cycle condensate. The flue gas is finally cooled to the required, possible lowest temperature before following compression stage by cooling water as for the reference case. 2.4 Lignite drying by ASU-waste nitrogen (Case 4) The idea for lignite drying by ASU-waste nitrogen (case 4) is presented in Fig. 3. The plant structure includes fluidized-bed lignite dryer fed by dry nitrogen taken from ASU exhaust. Additionally, the heat exchanger is located inside the bed to enhance the heat transfer to the fuel being dried. Such a technology has been tuned for utilization of low-temperature waste heat and follows the commercially proved idea presented in [6]. The coal dryer applied within power system presented in [6] uses however air as drying agent and assumes integration with conventional air-firing boiler. It has been assumed, that the dry nitrogen and water for the in-bed heat exchanger are preheated by the compressed air from the ASU air compression line. The detailed flow sheet of Case 4 has been presented in Fig. A4 in appendix A. The steam cycle is the same as for the reference case, so the Fig. A1b in appendix A refers also to Case 4. Detailed information about streams entering fuel drier has been shown in Table 2. Table 2. Detailed information about streams entering fuel dryer Stream (No at Fig.3) Temperature, 0 C Mass flow, kg/s Nitrogen entering preheater (158) 30 566,9 Nitrogen entering fuel dryer (161) 70 566,9 Nitrogen leaving fuel dryer (155) 35 575,3 Lignite entering fuel dryer (159) 25 219,2 Lignite leaving fuel dryer (2) 30 204,5 48
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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
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 34 and 35: [ P EXmth EX SNG] ESR F where EXm
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 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
Page 84 and 85: Figure A3a. Thermoflex flow sheet o
Page 86 and 87: Figure A4. Thermoflex flow sheet of
Page 90 and 91: 2.1. Life Cycle Assessment 2.1.1. G
Page 92 and 93: these factors. A sensitivity analys
Page 94 and 95: methane slip contributes to 13% of
Page 96 and 97: As can be seen in Fig. 5 the impact
Page 98 and 99: References [1] Eurobserv’er, The
Page 102 and 103: in which CO2 is separated from H2,
Page 104 and 105: dimensions of water droplets and wa
Page 106 and 107: Temperature (°C) 8 7 6 5 4 3 2 1 0
Page 108 and 109: 4. Conclusions In the present paper
Page 112 and 113: penalty, but without separate captu
Page 114 and 115: 0.5 - 0.7 kg/kg, resulting typicall
Page 116 and 117: 3.3 - Utilising waste heat All exis
Page 118 and 119: 4.5 - Suomusjärvi olivine deposits
Page 120 and 121: material will change from a few % t
Page 122 and 123: 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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Abstract: PROCEEDINGS OF ECOS 2012
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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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PROCEEDINGS OF ECOS 2012 - THE 25 T
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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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PROCEEDINGS OF ECOS 2012 - THE 25 T
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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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