1. Introduction - Firenze University Press

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Engineering Technical Conferences & Computers and Information in Engineering Conference IDETC/CIE 2007 September 4-7, 2007, Las Vegas, Nevada, USA. [16] H.G Jin, W. Han, L. Gao, 2007. A NOVEL MULTI-FUNCTIONAL ENERGY SYSTEM (MES) FOR CO2 REMOVAL WITH ZERO ENERGY PENALTY, Proceedings of GT2007 ASME Turbo Expo 2007: Power for Land, Sea, and Air May 14-17, 2007, Montreal, Canada GT-2007-27680. [17] Möllersten K., Yan J., 2001. Economic evaluation of biomass-based energy systems with CO2 capture and sequestration—The influence of the price of CO2 emission quota, World Resour Rev, 13(4), pp. 509-525. [18] Möllersten K., Yan J., Moreira JR., 2003. Potential market niches for biomass energy with CO2 capture and storage—opportunities for energy supply with negative CO2 emissions. Biomass and Bioenergy, 25(3), pp. 273-285. [19] Obersteiner M., Azar Ch., Kauppi P., Möllersten K., Moreira J., Nilsson S., Read P., Riahi K., Schlamadinger B., Yamagata Y., Yan J., Van Ypersele J.-P., 2001. Managing Climate Risk, Science, 294(2001), pp. 786-787. [20] IEA (International Energy Agency), 2001Key World Energy Statistics from the IEA, 2001 Edition. [21] H.G. Jin., Ishida M., 1997. A New Advanced IGCC Power Plant with Chemical-Looping Combustion, Proc. of TAIES’97, pp. 548-553, Beijing, 1997. [22] W. D. Ni, H.S. Zhen, Z. Li, N. Jiang, 2003. Polygeneration A Very Important Way to Overcome Five Challenges in Energy Field of China, POW ER ENGINEERING, (3)2003, pp. 2245-2251. 17
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 Analysis and Optimization of CO2 Capture in a China’s Existing Coal-fired Power Plant Gang Xu a , Yongping Yang b , Shoucheng Li c , Wenyi Liu d and Ying Wu e a North China Electric Power University, Beijing, China, xg2008@ncepu.edu.cn b North China Electric Power University, Beijing, China, yyp@ncepu.edu.cn c North China Electric Power University, Beijing, China, lishoucheng6363@126.com d North China Electric Power University, Beijing, China, lwy@ncepu.edu.cn e North China Electric Power University, Beijing, China, 837469236@qq.com Abstract: In China, pulverized coal-fired power plants provide over 70% of the total electricity, on the other side, make up nearly half of the total CO2 emission volume of the whole country. Thus, CO2 capture in these coal fired power plants will be extremely important to the effort of CO2 reduction made worldwide. However, to retrofit existing power plant for CO2 capture may encounter many constrains from the layout of original process and the structure of existing equipments, causing a lot of special problems in process design and bringing deep influence on system performance, which in turn requiring special considerations in system integration. In view of these factors, this paper carried out the process simulation, characteristics analysis and system integration of CO2 capture based on a typical China’s existing coal-fired power plant with supercritical parameters. The paper analyzes main constrains encountered in retrofitting existing power plant with CO2 capture using monoethanolamine (MEA) solution and puts forward several special system integration schemes for CO2 capture in an existing 600MW unit of China. The results revealed that, due to the constrains of the layout of original process and the structure of existing equipments, efficiency penalty of CO2 capture in a existing power plant will be even higher than a re-design new power plant by 3-5%-points. However, through the special system integrations, the efficiency of such retrofitting existing power plant can increase by 2-4%-points. The research of this paper may provide a feasible technology solution for decarburization retrofits of existing power plants, and promote CCS technologies into application. Keywords: CO2 Capture, Existing Coal-fired Power Plant, Retrofit, Thermal Energy Integration. 1. Introduction Increasing concentration of CO2 and other greenhouse gases (GHG) is the main reason behind alarming environmental phenomena, such as global warming and sea level rising [1-2]. China, one of the world’s largest producers of CO2 emissions, is responsible for approximately one fifth of global CO2 emissions [3]. Different from many industrialized countries, China’s main primary energy is coal, which is a kind of cheap but carbon-intensive energy resources. And in China, pulverized coal fired power plants, whose total installed capacity is over 700GW, provide nearly 80% of the total electricity, however, make up almost half of the total CO2 emission volume of the whole country [4]. Thus, the reduction of CO2 emissions in the electricity supply sector of China, especially in these pulverized coal fired power plants, will make a significant contribution to the country and even to the whole world. Though suffering of high energy and cost penalty, CO2 capture and storage (CCS) is commonly considered as a technically feasible method of making deep reductions in carbon dioxide emissions from sources such as energy utilization systems, and attracted great attentions worldwide [5-11]. At present, there are three basic technologies for capturing CO2 from energy systems: post-combustion capture, oxy-fuel combustion capture, and pre-combustion capture. As for CO2 separation process, 18
Page 1: Proceedings e report 90
Page 4 and 5: ECOS 2012 : the 25 th International
Page 7 and 8: Advisory Committee (Track Organizer
Page 10 and 11: The 25 th ECOS Conference 1987-2012
Page 12 and 13: VOLUME VI CONTENT VI. 1 CARBON CAPT
Page 14 and 15: -----------------------------------
Page 16 and 17: » Personal transportation energy c
Page 18 and 19: » Excess enthalpies of second gene
Page 20 and 21: VOLUME IV IV . 1 - FLUID DYNAMICS A
Page 22 and 23: » Exergy analysis and genetic algo
Page 24 and 25: » Optimal lighting control strateg
Page 26 and 27: » Stability and limit cycles in an
Page 28 and 29: PROCEEDINGS OF ECOS 2012 - THE 25 T
Page 30 and 31: Fig. 2. The exergy destruction of M
Page 32 and 33: ineffectiveness of the catalyst, in
Page 34 and 35: [ P EXmth EX SNG] ESR F where EXm
Page 36 and 37: Fuel inputkW 728221 203771 237719 3
Page 38 and 39: Not only at desined Rc (the ratio o
Page 40 and 41: 4. DISCUSSION The graphic exergy an
Page 42 and 43: Figure 9(a) illustrates the energy
Page 46 and 47: generally there are four kinds of m
Page 48 and 49: However, even under the off-design
Page 50 and 51: Fig. 3. 600MW supercritical coal-fi
Page 52 and 53: CO2 rich loading(molCO2/molMEA) 0.4
Page 54 and 55: Net efficiency (%) 40.28 30.29 26.4
Page 56 and 57: Fig. 11. Schematic diagram of heat
Page 58 and 59: 28.67%. In addition, through heat i
Page 60 and 61: Applied Thermal Engineering 2010;30
Page 62 and 63: Abstract: PROCEEDINGS OF ECOS 2012
Page 64 and 65: Fig. 1. Solution diagram of „four
Page 66 and 67: K ~ K 1 eK 1a p K 1a iK mK
Page 68 and 69: Oxygen recovery rate, % 105 95 85 7
Page 70 and 71: Calculated optimal compressor press
Page 72 and 73: PROCEEDINGS OF ECOS 2012 - THE 25 T
Page 74 and 75: The net amount of the flue gas leav
Page 76 and 77: Figure 3. Idea for lignite drying b
Page 78 and 79: Energy efficiency, % 34,00 33,00 32
Page 80 and 81: points efficiency increase related
Page 82 and 83: Figure A1b. Thermoflex flow sheet o
Page 84 and 85: Figure A3a. Thermoflex flow sheet o
Page 86 and 87: 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
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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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PROCEEDINGS OF ECOS 2012 - THE 25 T
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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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Abstract: PROCEEDINGS OF ECOS 2012
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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
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The CO2 emission factor which indic
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The CO2 emission factor calculated
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Appendix A Fig A.1. Simulation mode
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(b) Fig. A.2. Simulation model of C
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Table A.1. Calculated parameters at
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References [1] Pfaff I., Oexmann J.
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with a CC installation could be avo
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2.3. Basic CHP plant indices. The b
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3. Off-design calculations The main
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Fig. 6. CHP plant efficiency Fig. 7
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amount of steam delivered to the he
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[5] Lukowicz H., Mroncz M.: Analysi
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water removal is feasible by coolin
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Figure 2. Sketch of the suggested P
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a b Figure 5. a) Exergy balance of
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The basis of comparison of each met
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Figure 7a. Impact of S/CATR on PCU
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However, more energy duty is requir
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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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