1. Introduction - Firenze University Press

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3.2.4 Effect of the ATR operational temperature (TATR) The ATR operating temperature is of high importance as it plays significant role on the syngas quality: according to the chemical equilibrium, the higher the temperature, the higher the methane conversion rate. On the other hand, in order to secure the autothermal conditions in the reactor, more oxidant agent is required in the case that the temperature is high. Furthermore, materials stability limits the maximum operating temperature to around 1100°C. Figure 9a. Impact of TATR on PCU Figure 9b. Effect of TATR on the power plant performance for the two purification methods for the two purification methods (CCR=90%). (CCE=90%). The ATR operating temperature is of high importance as it plays significant role on the syngas quality: according to the chemical equilibrium, the higher the temperature, the higher the methane conversion rate. On the other hand, in order to secure the autothermal conditions in the reactor, more oxidant agent is required in the case that the temperature is high. Furthermore, materials stability limits the maximum operating temperature to around 1100°C. As is shown in Figure 9a, at low ATR temperatures, cryogenic systems consume more energy for CO2 purification due to the increased presence of methane in the retentate stream. Recovery and exergy efficiencies for separation with a distillation column are greater than those of the corresponding flash separation method. This feature has a positive effect on the total system when the combustion of the recovered fuel satisfies the required CO2 capture rate. In this case, for TATR = 950°C, part of the methane is selected not to be recovered in order to meet the goal of CCR=90%. Consequently, the net efficiency drops considerably, (Figure 9b). At high temperatures, the oxy combustion option is more efficient than the cryogenic options by ca. 1%. 4. Conclusions This study investigates the cryogenic method as an alternative choice for the rich-CO2 stream purification after membrane separation, instead of simply combusting the retained combustibles. Two proposed cryogenic systems are investigated: flash separation with internal cooling and separation with distillation column. In the first case, electrical power is produced while the separation efficiency is quite high, as 62.6% of the combustibles heat input is recovered. On the other hand, separation by a distillation column may result in the complete separation of combustibles, providing high purity in the final CO2 stream (>99%). 155
However, more energy duty is required due to the external cooling system. The sensitivity analysis showed that the cryogenic methods can overbalance any ‘weak’ operating mode of the hydrogen block, such us low methane conversion rates at the ATR and low hydrogen recovery rates at the membranes. Nevertheless, as far as the total system efficiency is concerned, the oxy combustion option is preferable as it can combine both high capture rates and performance. Future work that correlates membrane area and investment cost of the whole plant would finally determine under which conditions a cryogenic recovery system is required. Acknowledgments The authors would like to gratefully acknowledge the support of the European Commission (CACHET II, FP7 Project No. 241342). Abbreviations ASU Air Separation Unit ATR Autothermal Reformer reactor COP Coefficient of performance GT Gas Turbine HRSG Heat Recovery Steam Generator HRF Hydrogen Recovery Factor HT-WGS High Temperature Water Gas Shift reactor LHV Lower Heating Value NG Natural Gas PCU Purification & Compression Unit ST Steam Turbine(s) S/CATR Steam-to-Carbon Ratio in ATR WGS-MR Water Gas Shift Membrane Reactor References [1] Olajire A. CO2 capture and separation technologies for end-of-pipe applications - A review. Energy 2010;35: 2610-2628. [2] Kanniche M., Gros-Bonnivard R., Jaud P., Valle-Marcos J., Amann J.M., Bouallou H. Precombustion, post-combustion and oxy-combustion in thermal power plant for CO2 capture. Applied Thermal Engineering 2010;30:53–62. [3] Romeo L.M., Lara Y., González A, Reducing energy penalties in carbon capture with Organic Rankine Cycles, Applied Thermal Engineering 31 (2011) 2928-2935 [4] Zanganeh K.E., Shafeen A., Salvador C., Beigzadeh A. Abbassi M., CO2 processing and multipollutant control for oxy-fuel combustion systems using an advanced CO2 capture and compression unit (CO2CCU), Energy Procedia 4 (2011) 1018–1025 [5] Kakaras E., Koumanakos A., Doukelis A., Giannakopoulos D., Vorrias I., Oxyfuel boiler design in a lignite-fired power plant, Fuel 86 (2007) 2144–2150 [6] Huang Y., Wang M., Stephenson P., Rezvania S., McIlveen-Wright D., Minchener A., Hewitt N., Dave A., Fleche A., Hybrid coal-fired power plants with CO2 capture: A technical and economic evaluation based on computational simulations, Fuel paper in press 156
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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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Page 132 and 133: HEAT Fig. 1. Scheme and main reacti
Page 134: (raw) materials pre-heating and AS
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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
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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.
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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
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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: Figure 7a. Impact of S/CATR on PCU
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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
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Page 201 and 202: hydrogen combustion technology at d
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Page 205 and 206: Fig. 1. TG curves collected for spe
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Page 217 and 218: 4. Pilot plant tests In order to de
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 231 and 232: 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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1. Introduction - Firenze University Press

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