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 Implementation of a CCS technology: the ZECOMIX experimental platform Calabrò Antonio a , Cassani Stefano a , Pagliari Leandro a Stendardo Stefano a a ENEA, Italian National Agency for New Technologies, Energy, and the Sustainable Economic Development Via Anguillarese, 301, S. Maria di Galeria, 00123, Rome, Italy One of the key challenges for the implementation of CO2 Capture and Storage (CCS) is the reduction of the CO2 capture costs derived by their applications in actual power plants. The research of new technologies based on more efficient materials and more efficient design for integration of CO2 capture technologies in power cycles, is a promising way to ensure, in the medium term, costs and energy performances comparable to the actual power plant without CCS. ZECOMIX experimental platform represents the ENEA proposal for this challenge and it can be count among the Research Infrastructures more innovative in Europe. The aim of this work is to present the first results of commissioning plant tests. Therefore this work is focused on the planning of future experimental activities in order to demonstrate the feasibility of the high temperature solid sorbent CO2 sorption process, applied to a syngas derived from coal gasification. Keywords: Keywords: Ca-based sorbent, carbon capture, solid chemical looping, gasification. 1. Introduction In July 2005 the activities of the project ZECOMIX (Zero Emission Coal Mixed Technology) started officially, within the framework of a program funded by the Italian University and Research Minister. The main aim of the project is to demonstrate, through a series of modelling and experimental activities, the feasibility of a new innovative process for production of electricity and hydrogen "zero emission" by coal. In the ZECOMIX project different processes (e.g. coal gasification, clean-up of syngas, capture and sequestration of CO2, combustion of hydrogen in gas turbine) have been coupled. The integration of these processes is the key factor to achieve higher cycle performance and optimization (fig.1) of the platform at hand. Preliminary studies on high temperature decarbonization syngas [1-3] and thermodynamic H2/O2 cycle [4,5] as led us to propose ZECOMIX cycle with a net electrical efficiency close to 50% [6]. The analysis was subsequently refined with the cooperation of major Italian Universities and Research Institutes, and the results have fully confirmed the encouraging prospects that the cycle had announced: at least ten-point performance higher than a current post-combustion capture technology coal plant [4,5]. The design and realization of a complex experimental platform to test new process for CO2 capture and hydrogen production was certainly the more challenging tasks from a technical and financial point of view. A large numbers of advanced research issues is related to the proposed platform (coal hydro-gasification, simultaneous high temperature CO2 and H2S capture with solid sorbents, hydrogen/steam fuelled micro-turbine). Preliminary studies have permitted us the commencement of several research lines in the fields of advanced system modelling [2,6] for testing coal gasification, and the study of materials for CO2 capturing [1-2]. On the other hand the great knowhow gained with years allows us to enter with a leading role in the most important European scientific organizations, in order to coordinate the research on CCS technologies considered the most promising option for sustainable use of fossil fuels in the near future. The experimental ZECOMIX pilot plant has been designed and constructed to test each single unit integrated in the platform. It is an advanced and flexible facility particularly oriented to the experimental 169
investigation and the developing of process and component modeling. The plant has been presented in an international framework (e.g. CSLF, ZEP, ECCSEL, EERA) and consistent with advanced technological initiatives of the European and worldwide scientific community. Moreover ZECOMIX plant has been evaluated and inserted in the first Italian Roadmap towards the Large research Facilities conceived by the Ministry of Research. 2. Conceptual description of the ZECOMIX platform Details of the ZECOMIX concept are presented in [6] whereas alternative configurations are proposed in [4,5] . In Fig 1(a) we have reported the main areas of the platform and how they are connected each other; in Fig 1(b) the layout of the platform constructed is showed. This work highlights our efforts in the realisation of the plant layout showed in Fig 1(b). The plant (see Fig 2(a)) can be broken into : Unit based on a 50 kg/h coal fluidised bed; Syngas decarbonising reactor. It has been conceived as a fluidised bed and designed in order to decarbonise 100 Nm3/h of coal syngas leaving the gasifier or a gaseous mixture produced by means adequate cylinders; 100 kWe micro-turbine modified to accommodate a mixture of H2 and H2O. Fig. 1. (a) Simplified schematic of the ZECOMIX concept; (b) Layout of the ZECOMIX platform. A number of devices are installed to further treat the syngas (e.g. scrubbing, drying and compression) to make it suitable as fuel for the micro-turbine. Moreover a steam generator has been 170 a b
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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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Page 145 and 146: moisture - 0,2237 ash - 0,0876 LHV
Page 147 and 148: 2.2 CFB plant For the current momen
Page 149 and 150: The CO2 emission factor which indic
Page 151 and 152: The CO2 emission factor calculated
Page 153 and 154: Appendix A Fig A.1. Simulation mode
Page 155 and 156: (b) Fig. A.2. Simulation model of C
Page 157 and 158: Table A.1. Calculated parameters at
Page 159 and 160: References [1] Pfaff I., Oexmann J.
Page 161 and 162: with a CC installation could be avo
Page 163 and 164: 2.3. Basic CHP plant indices. The b
Page 165 and 166: 3. Off-design calculations The main
Page 167 and 168: Fig. 6. CHP plant efficiency Fig. 7
Page 169 and 170: amount of steam delivered to the he
Page 171 and 172: [5] Lukowicz H., Mroncz M.: Analysi
Page 173 and 174: water removal is feasible by coolin
Page 175 and 176: Figure 2. Sketch of the suggested P
Page 177 and 178: a b Figure 5. a) Exergy balance of
Page 179 and 180: The basis of comparison of each met
Page 181 and 182: Figure 7a. Impact of S/CATR on PCU
Page 183 and 184: However, more energy duty is requir
Page 185 and 186: Abstract: PROCEEDINGS OF ECOS 2012
Page 187 and 188: 3.1. JACOBIAN-ASPEN Interface ASPEN
Page 189 and 190: Fig. 3. Triple Pressure Bottoming S
Page 191 and 192: As seen from Table 1, the mass flow
Page 193 and 194: 4. Conclusion Fig. 5. Partial Emiss
Page 195: [19] Yantovski E., Shokotov M., Sho
Page 199 and 200: University of L’Aquila and German
Page 201 and 202: hydrogen combustion technology at d
Page 203 and 204: eversibility of a pre-treated synth
Page 205 and 206: Fig. 1. TG curves collected for spe
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Page 211 and 212: CO2 capture capacity up to 150 th c
Page 213 and 214: the way for biogas utilisation is t
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Page 217 and 218: 4. Pilot plant tests In order to de
Page 219 and 220: Concerning the absorption reaction,
Page 221 and 222: with Regeneration (AwR), consists i
Page 223 and 224: [25] Aspen Plus 2004.1. Cambridge,
Page 225 and 226: systems for fuel drying waste strea
Page 227 and 228: heated in a heat exchanger placed i
Page 229 and 230: Fig. 2. Lower heating value of fuel
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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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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