1. Introduction - Firenze University Press

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[3] Greer, W.L., SO2/NOx Control Compliance with Environmental Regulations. IEE Transactions on Industry Applications 1989; 25:475-485. [4] McQueen, A.T., Bortz, S.J., Hatch, M.S., Leonard, R.L., Cement Kiln NOx Control. IEE Transactions on Industry Applications 1995; 31:36-44. [5] Mokrzycki, E., Uliasz-Bochénczyk, A., Alternative Fuels for the Cement Industry. Applied Energy 2003; 74:95-100. [6] Souza F.A., Utilização de Pneus Pós-Consumo como Combustível em Fornos de Cimento. In: CETESB, Seminário Nacional Sobre Reuso/Reciclagem de Resíduos Sólidos Industriais; 2000; São Paulo. [7] Giménez-Molina, S., Blanco-Varela, M.T., Solid state phases relationship in the CaO-SiO, Al2O, CaF2-CaSO4 system. Cement and Concrete Research 1995; 25:870-882. [8] Raina, K., Janakiraman, L.K., Use of Mineralizer in Black Meal Process for Improved Clinkerization and Conservation of Energy. Cement and Concrete Research 1998; 28:1093- 1099. [9] Lawrence, L.B., Joseph, R.H., Chemical Analyses of Middle and Upper Pennsylvanian Coals form south eastern Kansas – Available at: [accessed 3.16.2006]. [10] Salomon V.G., Evaluation of the Effects of the Presence of Heavy Metals in Waste Coprocessed when Used as Alternative Fuels and Raw Materials in Cement Industry [dissertation]. Itajubá, Brazil: Universidade Federal de Itajubá; 2002. [11] Kaplan E., Nedder N., Petroleum Coke Utilization for Cement Kiln Firing. In: Cement Industry Technical Conference, IEEE-IAS/PCA; 2001 29 Abr – 03 Mai; Vancouver, Canada. Academic Press: 251-263. [12] Jha, M.K., Abdullah, J., A Markovian approach for optimization highway life-cycle with genetic algorithms by considering maintenance of roadside appurtenances. Journal of the Franklin Institute 2006; 343:404-419. [13] Nash S.G., Sofer, A., A Linear and Nonlinear programming. McGraw-Hill, NY: 1996. [14] MatLab 7.0, MathWorks, USA – Available at: [accessed 6.22.2004]. [15] Carpio R.C., Optimization in Co-processing Waste in Cement Industry involving Costs, Quality and Environmental Impact [Thesis]. Itajubá, Brazil: Universidade Federal de Itajubá; 2005. 269
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 Abstract: Comparison of options for debottlenecking the recovery boiler at kraft pulp mills – Economic performance and CO2 emissions Johanna Jönsson a , Karin Pettersson b , Simon Harvey c and Thore Berntsson d a Div. of Heat and Power Technology, Dept. of Energy and Environment, Chalmers University of Technology, Göteborg, Sweden, johanna.jonsson@chalmers.se b Div. of Heat and Power Technology, Dept. of Energy and Environment, Chalmers University of Technology, Göteborg, Sweden, karin.pettersson@chalmers.se, c Div. of Heat and Power Technology, Dept. of Energy and Environment, Chalmers University of Technology, Göteborg, Sweden, simon.harvey@chalmers.se d Div. of Heat and Power Technology, Dept. of Energy and Environment, Chalmers University of Technology, Göteborg, Sweden, thore.berntsson@chalmers.se The trend in the European pulp and paper industry is toward fewer mills with larger capacity. As a result, a number of existing mills will increase their production capacity. For increased production capacity in kraft pulp mills, the recovery boiler is often a bottleneck.This paper compares three different options for debottlenecking the recovery boiler and utilizing a potential mill steam surplus at a typical Scandinavian kraft pulp mill, when increasing the production capacity by 25%:1) Upgrading the recovery boiler, 2) Lignin extraction and 3) Black liquor gasification (as a booster). For black liquor gasification (BLG) two options for using the product gas are considered: production of electricity or DME motor fuel. Furthermore, both BLG and upgrading of the recovery boiler are assumed to be possible to combine with carbon capture and storage (CCS). The extracted lignin is assumed to either be valued as wood fuel or as oil. The different options are evaluated and compared with respect to annual net profit and global CO2 emissions for four different future energy market scenarios.The results show that, generally, BLG with motor fuels production and lignin extraction with lignin valued as oil achieve the best economic performance. Upgrading the recovery boiler and capture and store CO2 from the boiler flue gases gives the highest CO2 emissions reduction but is only an economically attractive option in scenarios with a high CO2 emissions charge. Keywords: Kraft pulp mill, Biorefinery, Black liquor gasification, Lignin extraction, Carbon capture and storage, Energy market scenarios. 1. Introduction With increased concern for climate change and increasing energy prices, the need for energy efficiency measures is high on the agenda for both industrial and political decision makers. The industry sector, which stands for almost 30% of the energy use in Europe [1], is a key player in the transition towards a more sustainable European energy system. The pulp and paper industry is the sixth largest industrial energy user in Europe, using approximately 121 TWh of electricity and 365 TWh of thermal energy during 2007 [2]. Due to its high use of biomass and possibility to achieve an energy surplus, the kraft pulp industry has the potential to become a major contributor in reducing global CO2 emissions through increased delivery of energy products[3-10]. The potential for reduced process steam demand in the kraft pulp industry through improved process integration and by installing new efficient equipment has in previous research shown to be up to approximately 30-35%[11-14]. For most market kraft pulp mills implementation of such measures would lead to a significant steam surplus that can be utilized in different 270
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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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Page 253 and 254: Table 6. Experimental conversions o
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Page 275 and 276: Table A2. Extraction equations and
Page 277 and 278: [13] Teir S, Kuusik R, Fogelholm CJ
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Page 281 and 282: Tabel 1. Characteristics quantities
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Page 291 and 292: 2. Numerical model The purpose of t
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Page 337 and 338: In the presented paper a framework
Page 339 and 340: [5] Erdil E, Ilkan M, Egelioglu F.
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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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