1. Introduction - Firenze University Press

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emission” scope of the cycle. Micro-turbine is very sensible to the impurities. Then syngas scrubbing unit is fitted upstream the micro-turbine. Therefore, the scrubber is able to treat 400 Nm3/h in three stages: a Venturi scrubber, a spray tower wet scrubber, and a packed tower wet scrubber. The outlet particle diameter is lower than 1 m. The flare stack has been designed to the correct combustion of syngas from carbonator reactor or gasifier. Steam generator: The steam generator have 200kWt power output, and it is provided with an accumulator which permits a high flexibility mass flow production as a function of the configuration tests. It is possible to obtain three different mass flows at different pressure for every equipment: 30 kg/h at 1 atm for the coal gasification, 90 kg/h at 1 atm to the carbonatator, and 60 kg/h at 6 bar to the micro-turbine. Syngas compressor: The syngas compressor has three intercool centrifugal stages in order to maintain hydrogen under 130°C and water is drained. Then hydrogen stream is pre-heated and mixed with steam to the turbine conditions. Heaters: Three heaters are installed in the platform. An oxygen heater has been fitted in order to prevent condensation of water in the oxygen/steam mix. A nitrogen heater is needed to control the temperature in the heating/cooling processes in carbonation reactor between carbonation/calcination reactions. A heater of the syngas entering the carbonator is installed. Such a component is needed when synthetic gas is produced in the mixing station and send to the carbonator. In this case the syngas has to be heated from environmental temperature up to the carbonation temperature (600 °C). The platform is being commissioning. Several tests has been carried out in order to prove DCS system, steam generator, hydrogen compressor, pre-heater and flare. The main objectives which have been accomplished are mainly related to coal gasification, high temperature CO2 capture by means of solid sorbents, fluidynamics of bubbling bed, combustion of hydrogen. 4. Future activities in the framework of the ZECOMIX project In order to supply the experimental platform with a number of solid fuels (e.g. biomass and a blend of coal) a feeding system as flexible as possible is envisaged. Such a technological option will permit us to study the performances of the hydrogen production from solid fuels by varying the ratio of the different blends. Particularly the co-gasification of coal and biomass could be experienced and the main parameters affecting such a process will be studied. Such an experimental investigation will give information on how to mix coal and biomass and how the quality of the feedstock affects the production of electricity from hydrogen. Implementation of new sensors and probes (thermocouples and flux-meters) are envisaged. This improvement will permit us to increase the potential of the acquisition system and then the remote control of the process at hand with online monitoring and dynamic measurement. Particularly during the warm up of decarbonisation reactor the control of the refractory temperature is needed in order to know the evolution of the temperature profile into the refractory wall of the reactor and the characteristic time for heating up the reactor. In order to manage the energetic system at hand in an economically viable way, optimization of hydrogen and electricity production should be taken into account. These outputs of the experimental platform strongly depend on the correct blend of both feedstock and energy inputs (e.g quality and quantity of the solid fuel to be gasified and heat demand of calciner for sorbent regeneration as well). There is a lack of dependable economic and operative parameters, due to the intrinsic novelty of the proposed process. A valuable tool for addressing such a problem could be modeling each single main component (gasifier, carbonator, micro-turbine) to simulate and optimize ZECOMIX system. When thermo-economic constraints are included the optimization problem will increase significantly. Moreover if the number of variables governing the hydrogen and power production is relatively low an adequate and accurate DoE (design of experiment) is suggested as a valuable tool to determine how the main parameters affect the electricity production. Finally, the activities scheduled for the power unit at hand have been proposed in order to test the 173
hydrogen combustion technology at different scale levels and grades of integration with the whole experimental platform. In particular a dynamic model of the micro-turbine has been developed and integrated in a commercial power plant simulator. Such a model is a valuable tool for the simulation of a the micro-turbine in a number of operative conditions. Numerical simulation are needed to estimate the dynamic behavior of the power unit when the fuel supply switches from natural gas to hydrogen during full and half load as well. The experimental programmed activities have been enthusiastically welcomed by a number of European projects and research alliances to promote the co-operation between researchers. ZECOMIX project is involved in the ECCSEL initiative in the framework of CCS research facilities to share knowledge through network of researchers with the common interest to improve the assessment methodology for decarbonised energy production. Moreover the platform is involved in the EERA sub-programme for developing a methodology and comparing process performances in the field of CO2 capture.A complete schedule of activities has been planned are: 1. hot tests on carbonator in order to study heat transfer in the gas-particle-wall system and start-up procedure. Modeling activities are planned to predict the thermal behavior of the carbonator reactor. Start-up of H2 micro-turbine will be performed as well. 2. tests of SE-SMR reactor fed with synthetic syngas from cylinders. Performance of CO2 capture sorbents and catalyst. Study of instabilities in the process between calcination and carbonation phase. Integration with micro-turbine. Optimizing of operational conditions. 3. carbonation/calcination cycling with gasification integration. Studies of influence of gasification on flue gas composition. Effect of gasification on hydrogen production. Optimization of the process. Study of loss efficiency due to clean-up of gases. Acknowledgment The authors are grateful to Prof. Pier Ugo Foscolo and Prof. Antonino Germanà, of University of L’Aquila, for carbonator and gasifier design, and SO.IM.I. company for constructing the experimental platform. References [1] Stendardo S., Calabrò A., Experiments on CaO–CaCO3 loop for high temperature CO2 capture. ENEA Technical Report 2008 No.: EHE08039 TER-ENEIMP. [2] Stendardo S., Foscolo P.U., Carbon dioxide capture with dolomite: A model for gas–solid reaction within the grains of a particulate sorbent. Chem Eng Science 2009;64:2343-2352. [3] Stendardo S., Di Felice L., Gallucci K., Foscolo P.U., CO2 capture with calcined dolomite: the effect of sorbent particle size. Biomass Conv and Biorefinery 2011;1(3):149-161. [4] Galeno G., Spazzafumo G., ZECOMIX: Performance of alternative layouts. International Journal of Hydrogen Energy 2010;35:9845-9850. [5] Romano MC, Lozza G. 2010. Long-term coal gasification-based power plants with near-zero emissions. Part A: Zecomix cycle. Int Journal of Greenhouse Gas Control 2010;4:459-468. [6] Calabrò A., Deiana P., Fiorini P., Girardi G., Stendardo S., Possible optimal configurations for the ZECOMIX high efficiency zero emission hydrogen and power plant. Energy 2008;33:952- 962. 174
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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
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 and 196: [19] Yantovski E., Shokotov M., Sho
Page 197 and 198: investigation and the developing of
Page 199: University of L’Aquila and German
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Page 219 and 220: Concerning the absorption reaction,
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Page 223 and 224: [25] Aspen Plus 2004.1. Cambridge,
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Page 229 and 230: Fig. 2. Lower heating value of fuel
Page 231 and 232: Acknowledgements The results presen
Page 233 and 234: large amount of CO2 [1,5-7]. APCr a
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
Page 241 and 242: CaO HCl CaCl H O 193kJ / mol (
Page 243 and 244: [1] M. Fernández Bertos, S.J.R. Si
Page 245 and 246: Abstract: PROCEEDINGS OF ECOS 2012
Page 247 and 248: 2. Process development 2.1. Backgro
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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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