1. Introduction - Firenze University Press

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[7] Romeo L. M., Bolea I., Lara Y., Escosa J. M., Optimization of intercooling compression in CO2 capture systems, Applied Thermal Engineering 29 (2009) 1744–1751 [8] Posch S., Haider M., Optimization of CO2 compression and purification units (CO2CPU) for CCS power plants, Fuel paper in press [9] Colin A. Scholes, Kathryn H. Smith, Sandra E. Kentish, Geoff W. Stevens, CO2 capture from pre-combustion processes - Strategies for membrane gas separation, International Journal of Greenhouse Gas Control 2010;4:739–755. [10] John J. Marano, Jared P. Ciferino, Integration of Gas Separation Membranes with IGCC - Identifying the right membrane for the right job, Energy Procedia 1 (2009) 361–368 [11] Mendes D., Chibante V., Zheng J.M., Tosti S., Borgognoni F., Mendes A., Madeira L. M., Enhancing the production of hydrogen via water gas shift reaction using Pd-based membrane reactors, J Membrane Sci 35 (2010) 12596- 12608 [12] Dijkstra J.W., Jansen D., Novel concepts for CO2 capture, Energy 29 (2004) 1249–1257 (In: 6th International Conference on Greenhouse Gas Control Technologies). [13] Atsonios K., Panopoulos K., Doukelis A., Kakaras E., Exergy Analysis of a Hydrogen fired combined cycle with natural gas reforming and membrane assisted shift reactors for CO2 capture, presented in ECOS 2011 in Novi Sad, Serbia, July 4-7 201<strong>1.</strong> [14] Jan Wilco Dijkstra, Johannis A.Z. Pieterse, Hui Li, Jurriaan Boon, Yvonne C. van Delft, Gunabalan Raju, Gerard Peppink, Ruud W. van den Brink, Daniel Jansen. Development of membrane reactor technology for power production with pre-combustion CO2 capture. Energy Procedia 2001;4:715–722 [15] Criscuoli A., Basile A., Drioli E., Loiacono O., An economic feasibility study for water gas shift membrane reactor. Journal of Membrane Science 181 (2001) 21–27 157
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 Design and Optimization of ITM Oxy-Combustion Power Plants Surekha Gunasekaran a , Nicholas D. Mancini a and Alexander Mitsos a a Massachusetts Institute of Technology, Cambridge, United States surekhag@mit.edu, mancini@mit.edu, amitsos@alum.mit.edu (CA) Oxy-fuel combustion using an oxygen ion-transport membrane (ITM) is a promising alternative to the existing cryogenic air separation method, which incurs heavy thermodynamic and economic penalties. The performance of ITM-based power plant systems depends on the operating conditions, geometric structure of the reactor and the integration approach of ITM to the existing power plant system. A detailed study of these factors is required to perform an optimization analysis. In this paper, an intermediate-fidelity ITM model is used to study the performance of ITM reactors under different operating conditions and flow configurations. Using this model, ITM-based oxy-combustion power cycles are investigated. This article focuses on the results of an optimization analysis of the AZEP 100 cycle, which consists of a Brayton-like topping cycle and a triple pressure heat recovery steam generation bottoming cycle. The effects of power plant operating parameters are analyzed, namely the outlet pressure of pumps, turbines, valves and de-aerator, the split fractions of splitters, flow rates, and the outlet temperatures of heat exchangers. The optimization study has resulted in an increase of 2.92 percentage points which is important with respect to the feasibility of ITMbased oxy-combustion power plants compared to alternatives. Keywords: Oxy-fuel combustion, Ion-transport membrane, Zero-emission power cycle, Power cycle efficiency. <strong>1.</strong> CCS and ITM Technology Global warming and anthropogenic emissions of CO2 have motivated the search for more efficient and economically feasible environment-friendly technologies for power generation, which contributes to about 65% of total anthropogenic CO2 emissions [1]. Carbon-dioxide capture and sequestration (CCS) allows for the use of fossil fuels for power generation without the detrimental effects of associated CO2 emissions. The most conventional CCS technique is post-combustion capture, which is energy-intensive and expensive [2]. In the oxy-combustion method, O2 is separated from air prior to the combustion of the fuel-air mixture and fuel oxidation occurs in a nitrogen free environment, typically with large recirculation of exhaust gases to control the temperature. The flue gas consists only of CO2 and H2O, from which CO2 can be separated simply by condensation. Thus, the penalty associated with separation of CO2 from the flue gas is greatly reduced [3]. At present, large scale separation of O2 from air is done using cryogenic air separation methods. The major disadvantages of this method are that it is energy intensive, and has low second law efficiency [4]. A promising alternative is the use of ion-transport membranes (ITM), which operate based on chemical potential differences, and use a high temperature mixed-conducting (ionic and electronic) ceramic membrane [5]. This technology is motivated by the fact that the penalties incurred are much lower than the additional power requirement for cryogenic air separation [6]. 158
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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
Page 134: (raw) materials pre-heating and AS
Page 137 and 138: Fig 3- Aspen Plus® model 110
Page 139 and 140: Table 4. Elemental and XRD analysis
Page 141 and 142: the ÅA CSM route. The content of M
Page 143 and 144: Abstract: PROCEEDINGS OF ECOS 2012
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: However, more energy duty is requir
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 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
Page 207 and 208: (see Fig 5). Carbon dioxide uptake
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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
Page 233 and 234: 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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