1. Introduction - Firenze University Press

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Table 3. Summary of the process’ exergy. EQUIPMENT Energy Q (J/s) T (°C) Exergy as heat (MJ/hr) MJ/kgCO2 SS DECOMPOSITION 463146 450 1003 5.44 DISSOLUTION -52259 80 -35 -0.19 PPI -52455 30 -9 -0.05 PP2 -14218 30 -3 -0.01 TANK 1 -82000 40 -137 -0.74 EVAPORAT 630066 103 532 2.88 CARBONATOR -5500 500 -12 -0.07 HX-1 (S+AS+WT pre-heat) 434378 430 923 5.01 HX-2 (FG pre-heat) 65050 450 141 0.76 HX-3 (Mg(OH)2 pre-heat ) 27517 260 46 0.25 HX-4 (Gaseous Products ) -472663 440 -1014 -5.50 HX-5 (solid Products) -93161 440 -200 -1.08 HX-6 (wt from AS recovery) -612765 103 -517 -2.80 HX-7 (gas from turbine) -73507 187 -99 -0.54 Utilities Multistage Compressor (Water [15–90] °C) stage 1 -30105 90 -22 -0.12 Total Exergy Process 2 Exergy provided by the FG 3 Exergy Process + FG 4 stage 2 -23328 90 -17 -0.09 stage 3 -23512 90 -18 -0.09 stage 4 -23878 90 -18 -0.10 stage 5 -24599 90 -18 -0.10 111 Flue Gas (kg/hr) Flue Gas NTP (m 3 n/s) FG500 FG440 FG500 FG440 37442 4992 11235 13723 525 2.85 Total 42434 24958 9.42 6.65 2645 14.34 -2120 -11.49 2 Total exergy as heat (120~450⁰C) needed to run the process, without integration with flue gas. 3 Exergy that the flue gas provides to the endothermic blocks. 4 Total exergy of the process when flue gas provides heat to all the endothermic stages. This final value may lead to the erroneous conclusion that the heat content of the flue gas is enough to process more serpentine. This “surplus” of exergy comes from streams at T ≤ 400⁰C making its heat content unsuitable for the processing of rock material at ~440⁰C. On the other hand this heat is appropriate for district heating. 891 8.32 1.11 3.40 3.08 0.20
Table 4. Elemental and XRD analysis of the diopside sample. Elemental Analysis (%) Structural Analysis (XRD) CaO SiO2 TiO2 Al2O3 Fe2O3 MgO K2O Na2O Others 15.6 50.9 0.4 12.2 4.5 4.9 3.1 2.1 6.3 112 Hedenbergite, Orthoclase, Albite (Calcium), Muscovite, Clinochlore A total of twelve experiments were done in order to determine the reactivity of the rock. The diopside (D) was mixed with solid ammonium sulphate (D:AS=2g:3g) and placed in an oven at different temperatures, 250-500°C, for 30 minutes. The products of this extraction step were dissolved in water and the concentrations of magnesium, iron, aluminium, calcium, sodium, potassium and sulphur in the solution were measured by an ICP-OES analysis. In six of the experiments, the influence of water was studied by adding 3 ml of water to the diopside/AS mixture (D:AS:W=2g:3g:1ml). 3.2 Experimental results À priori, the composition of the diopside does not seem to be very suitable for direct application of the ÅA procedure mainly due to its dramatically low content of MgO, but also due to its high percentage of aluminium and other alkaline elements. In earlier experiments [16] the increase of aluminium content did not appear to favour the extraction reactions. Disappointingly, also the extraction results are very discouraging. Besides its low Mg content, the diopside’s reactivity is extremely low making the upgrading of this material doubtful. Water does not appear to play a key role on the materials reactivity. In fact, contrary to what occurs with the serpentine minerals [17], the evolution of the extraction rates with temperature is quite similar both in the presence and absence of water. Even if it was possible to extract all the X elements of the rock material, the applicability of the ÅA route presents several challenges. The extraction of all the magnesium is energy consuming due to the presence (in greater percentages) of other elements (mainly Al, Fe, Na, K, and Ca). In fact, a quick calculation allows for concluding that only 1/4 of the overall reactions’ heat is used for Mg extraction. A successful extraction of Ca would imply a second carbonation stage (probably in an aqueous solution). And finally, the presence of alkali metals (which are highly water soluble and do not precipitate) would make the AS recovery very difficult implying the application of extra separation stages to preclude the recirculation/accumulation of those unwanted elements. In Table 5 a brief comparison of the pros and cons of using serpentinite vs diopside for CO2 mineralisation is presented. As these results show that the diopside seems not to be a suitable material, no Aspen Plus simulations were made for that. Extraction % 12 10 8 6 4 2 DRY Extraction 0 200 250 300 350 400 450 500 550 Temperature ( C) Al Fe Mg Ca K Na 0 200 250 300 350 400 450 500 550 Temperature ( C) Fig.4 Experimental results concerning the extraction Fig.5 Experimental results concerning the Extraction % 12 10 8 6 4 2 WET Extraction Al Fe Mg Ca K Na
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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
Page 88 and 89: Abstract: PROCEEDINGS OF ECOS 2012
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 100 and 101: PROCEEDINGS OF ECOS 2012 - THE 25 T
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
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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
Page 124 and 125: 8. Combined SO2 capture and CO2 min
Page 126 and 127: Fig. 10 Carbonate- (left) and sulph
Page 128 and 129: [13] Ekdahl, E., Idman, H. Statemen
Page 132 and 133: HEAT Fig. 1. Scheme and main reacti
Page 134: (raw) materials pre-heating and AS
Page 137: Fig 3- Aspen Plus® model 110
Page 141 and 142: the ÅA CSM route. The content of M
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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 187 and 188: 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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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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