1. Introduction - Firenze University Press

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Abstract: PROCEEDINGS OF ECOS 2012 - THE 25 TH INTERNATIONAL CONFERENCE ON EFFICIENCY, COST, OPTIMIZATION, SIMULATION AND ENVIRONMENTAL IMPACT OF ENERGY SYSTEMS JUNE 26-29, 2012, PERUGIA, ITALY Thermodynamic analysis of a supercritical power plant with oxy type pulverized fuel boiler, carbon dioxide capture system (cc) and four-end high temperature membrane air separator Janusz Kotowicz a , Sebastian Michalski b a Silesian University of Technology, Poland, janusz.kotowicz@polsl.pl, b Silesian University of Technology, Poland, sebastian.michalski@polsl.pl, In this paper the analysis of a supercritical power plant was made. Power of the power plant is 460 MW. The parameters of life steam are at 29 MPa/600 oC and of the reheated steam 4.8 MPa/600 oC. Power plant is equipped with the following units: oxy type pulverized fuel boiler, "four-end" high temperature membrane (HTM) air separator and carbon dioxide capture system (CC). With the assumption of a constant gross power of the analyzed power plant the thermal efficiency of the boiler and power consumption of all mentioned above units were calculated. These parameters were designated as a function of the recovery rate of oxygen in the HTM. This allowed to make the characteristic of efficiency as a function of recovery rate. The net efficiency increased from 34.8% to 36.7% with a change of oxygen recovery rate from 0.45 to 0.9. The effect of membrane working temperature on the efficiency characteristics was also analyzed. Integration of CC, HTM air separator and steam cycle was proposed for the increase of the efficiency of a power plant. The theoretical analysis was carried out and appropriate calculations were made for this integration. Keywords: OXY type pulverized fuel boiler, air separation, four-end HTM (High Temperature Membrane) 1. Introduction Currently observed in the world trend in efforts to reduce emissions, especially of greenhouse gases, contributes to significant changes in the direction of the development of energy technologies [1]. This is very important for the development of coal technologies, due to importance of these fuels in the energy balances of many countries, including Poland, as well as due to significant emission of CO2 per electricity production unit. In the area of coal technology there are two main research directions aiming to bring down the reduction of CO2 unit emission, thus, in consequences, to the reduction of global emission: search of low-energy consuming carbon capture technologies (including searching for new technologies, optimization of known technologies, also in the area of integration of the CCS unit with a power plant), increasing the efficiency of electricity generation, including optimization of a power plant, both in the area of its structure, as well as in area of operation parameters [2]. Among carbon capture technologies three directions are developed: pre-combustion technology, post-combustion technology, oxy-combustion technology. 251
In the area of coal technologies all of these solutions can be used. However, the first solution is predisposed for IGCC systems [3], in which there is the possibility of generating carbon dioxide before combustion of synthesis gas. The fuel before entering the combustion chamber is subjected to a carbon sequestration. Due to the lower gas stream from which the carbon dioxide is removed such a separation process is connected with less energy consumption. The next technology is based on removing carbon dioxide from flue gases leaving the power system. The post-combustion technology is predisposed for the conventional coal-fired power plants. In the area of postcombustion technology, as in the case of pre-combustion, the research on absorption and adsorption techniques, as well as membrane and cryogenic separation are realized [4÷5]. Among of clean coal technology large hopes are associated with oxy-combustion technology, of which the principal purpose is combustion of coal in the oxygen-rich atmosphere in order to eliminate from the exhaust gases the inert gas (nitrogen). In this case the exhaust gases leaving the steam boiler consists mainly of carbon dioxide and steam, so the carbon capture process is much less energy intensive. Currently in the research area of oxy-combustion technology, the solutions aiming for decreasing the energy consumption connected with oxygen production in the air separation unit are searched for [6÷10]. The results presented in the paper were realized within the framework of the Strategic Project ”Advanced Technologies for Energy Generation: Oxy-combustion technology for PC and FBC boilers with CO2 capture”. In the paper the results of the analysis of the steam cycles of energy generation units are shown. These steam cycles will be the basis for creation of the models of the whole oxy-combustion power plants. In the paper the results of analysis including the influence of different solutions of steam cycles, and thus their assumed parameters, on the energy effectiveness evaluation indicators are shown. 2. Model of the air separation unit integrated with the oxy type pulverized boiler and assumptions for calculations Air separation unit structure consists of: a counter-current air heater (APH), an air compressor (C), an expander (EX), a generator (G) and a "four end" type membrane (M). The expander drives the air compressor. Depending on the assumed quantities the expander and compressor can give or take electricity from the grid. The structure of the air separation unit is shown in Figure 1. Fig. 1. Scheme of the air separation unit (ASU) 252
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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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Page 231 and 232: Acknowledgements The results presen
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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
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Page 243 and 244: [1] M. Fernández Bertos, S.J.R. Si
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Page 275 and 276: Table A2. Extraction equations and
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Page 281 and 282: Tabel 1. Characteristics quantities
Page 283 and 284: N m eT 4a ~ T cp T4a 1 ( K
Page 285 and 286: Auxiliary power rate of ASU, % 40 4
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Page 305 and 306: Table 5. Key data for the four ener
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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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