1. Introduction - Firenze University Press

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v. 37, p. 5330-5339, 2003. 44. DOE. International Energy Outlook 2011. U.S. Department of Energy - U.S. Energy Information Administration, 2011. See also: . Accessed on: 11 Jan 2012. 339
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 Simulation of Synthesis Gas Production from Steam Oxygen Gasification of Colombian Bituminous Coal using Aspen Plus ® John Ortiz a , Juan González b , Jorge Preciado c , Rocío Sierra d and Gerardo Gordillo e a Universidad de los Andes, Bogotá, Colombia: jj.ortiz24@uniandes.edu.co, b Universidad de los Andes, Bogotá, Colombia, jc.gonzalez141@uniandes.edu.co c Universidad de los Andes, Bogotá, Colombia, je.preciado40@uniandes.edu.co d Universidad de los Andes, Bogotá, Colombia, rsierra@uniandes.edu.co e Universidad de los Andes, Bogotá, Colombia, g.gordillo43@uniandes.edu.co The growing energy demand, sustained increase in fossil fuel prices, and need for environmental protection have forced to consider alternatives to the traditionally energy resources employed. Synthesis gas (syngas) produced by gasification of coal, biomass, petroleum coke, or solid waste has proven to be a useful clean fuel due to its lower emissions of sulfurs and nitrous oxides compared to other fuels. In this work, a simulation of syngas production from a Steam-Oxygen Gasification (SOG) process that uses the GE/Texaco technology was performed using Aspen Plus ® . For the simulation, the average proximate and ultimate compositions of bituminous coal obtained from the Colombian Andean region were employed. The obtained simulation was applied to conduct sensitivity analyses in key parameters. The information obtained allows the selection of critical operating conditions leading to improve system efficiency and environmental performance. The results of the parameter analysis indicate that the oxygen to carbon ratio is a key variable as it affects significantly both the LHV and thermal efficiency of the process. On the other hand, the process becomes almost insensitive to SDG values higher than 2. Finally, a thermal efficiency of 62.2% can be reached. This result corresponds to a slurry solid concentration of 0.65, a WGS process SDG of 0.59, and a LTS reactor operating temperature of 473 K. At these fixed variables, a syngas with H2 molar composition of 92.2% and LHV of 12 MJ N m -3 was attained. Keywords: Aspen Plus ® Simulation, Coal, Steam-Oxygen Gasification, Synthesis Gas. 1. Introduction Currently, in a world of high and growing energy demands and increasing oil prices, alternative and sustainable raw material resources are being sought. Ideally, these sources would be used for either energy generation or as valuable chemical feedstocks for variety of chemical processes and synthesis. Among different alternatives, syngas has shown to be a favorable option. Syngas is considered a clean fuel with environmental advantages compared to other fossil fuels because the sulfur oxides (SOX), nitrous oxides (NOX) and CO2 emissions are considerably lower [1, 2]. Syngas is an important building block in chemical, oil and energy industries due to its applications: 1) as a feedstock for the production of several chemicals such as hydrogen, ammonia, methanol, and Fischer-Tropsch products [3], 2) as a fuel in a gas turbine to produce electricity [4], 3) as a cell fuel for mobile sources [5], 4) as an electricity supplier through solid oxide fuel cells [3], and 5) as a primary fuel. Syngas, which is mainly a mixture of hydrogen (H2) and carbon monoxide (CO), is mainly used as a chemical substance rather than a fuel, representing 50 billion US$ market for 40 Tg (40 Mt) annual production nowadays [6]. Hydrogen could help to satisfy the world energy demand. Recent reports show that global energy consumption grew 5.6% in 2010, the largest yearly increase since 1973 [7]. 340
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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
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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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1. Introduction - Firenze University Press

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