Novel Design of an Integrated Pulp Mill Biorefinery for the ...

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99. J.P. Jansen, R.H.B., B. Breman, Large-scale production of biofuels through biomass (co- )gasification and Fischer-Tropsch synthesis. TNO Environment, Energy and Process Innovation Report. TNO-MEP - R 2002/406, 2002. 100. T. Chmielniak, M.S., Co-Gasification of Biomass and Coal for Methanol Synthesis. Applied Energy, 2003. 74: p. 393-403. 101. Kapfenberger, J., et al. Acid Gas Removal by Customized Sorbents for Integrated Gasification Fuel Cell Systems. [cited; Available from: http://www.osti.gov/energycitations/purl.cover.jsp?purl=/836749-RiYSFI/native/. 102. Higman, C. and M.v.d. Burgt, GASIFICATION. 2003: elsevier. 391. 103. Peng, X.D., et al., Single-step syngas-to-dimethyl ether processes for optimal productivity, minimal emissions, and natural gas-derived syngas. Industrial & Engineering Chemistry Research, 1999. 38(11): p. 4381-4388. 104. Hsiung, T.H.L., et al., Di:methyl ether and methanol synthesis - by one-step liq. phase process using synthesis gas and solid catalyst in inert liq, Air Prod & Chem Inc (Airp). 105. Peng, X., et al., Production of dimethyl ether involves using, as scrubbing solvent, solvent comprising mixture of dimethyl ether and methanol, Air Prod & Chem Inc (Airp). 106. Rytter, E., et al., QA and optimization issues during development of the Statoil FTcatalyst, in Fischer-Tropsch Synthesis, Catalysts and Catalysis, B.H. Davis and M.L. Occelli, Editors. 2007, Elsevier: Amsterdam. 107. Larson, E.D., T.G. Kreutz, and S. Consonni, Combined Biomass and Black Liquor Gasifier/Gas Turbine Cogeneration at Pulp and Paper Mills. Journal of Engineering for Gas Turbines and Power, 1999. 121: p. 394-400. 108. Stigsson, L. and N. Berglin. Black Liquor Gasification – Toweards Improved Pulp and Energy Yields. in the 6th International Conference on New Available Technologies at SPCI ’99. 1999. Stockholm, Sweden. 109. Larson, E.D., S. Consonni, and K.R. E., A cost-benefit assessment of Gasification-Based Biorefining in the Kraft Pulp and Paper Industry. 2006. 110. Quaak, P., H. Knoef, and H. Stassen, eds. Energy from Biomass: A Review of Combustion and Gasification Technologies. 1999, Washington, D.C.: Washington D.C. 76
Appendix Appendix A MP Steam Demand Steam tables show the specific enthalpy of MP steam at 11 bar and 200 degrees Celsius to be 2.822 GJ/tonne. LP Steam Demand GJ ADt 1 day 1 tonneMPsteam tonne 4 . 3 * 2000 * * = 126. 98 ADt day 24 hr 2. 822 GJ hr Steam tables show the specific enthalpy of LP steam at 3.5 bar to be 2.732 GJ/tonne. Total Steam Demand Power required to run mill Energy into System Bark Energy Flow GJ ADt 1 day 1 tonneMPsteam tonne 5 . 68 * 2000 * * = 173. 26 ADt day 24 hr 2. 732 GJ hr tonne tonne 173 . 26 + 126. 98 = 300. 24 hr hr tonne hr kWh ADt 1 day 1 MWe 701 * 2000 * * = 58. 42MWe ADt day 24 hr 1000 kW tonnewood kg 1 day MJ 4148 * 1000 * * 16 = 768. 15MW day tonne 86400 s kg tonnewood kg 1 day MJ 4148 * 1000 * * 20 = 960. 19MW day tonne 86400 s kg tonnebark kg 1 day MJ 362 . 5 * 1000 * * 16. 0 = 67. 13MW day tonne 86400 s kg 77
Page 1 and 2:
Novel Design of an Integrated Pulp
Page 3 and 4:
Table of Contents List of Figures .
Page 5 and 6:
List of Figures Figure 1: Price of
Page 7 and 8:
1 Introduction The global transport
Page 9 and 10:
2 Background 2.1 Pulp Mill Backgrou
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2.1.2.2 Chemical Pulping The most c
Page 13 and 14:
sodium sulfide and sodium carbonate
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process described in the section on
Page 17 and 18:
2.2.1 Low-Temperature Black Liquor
Page 19 and 20:
Figure 2: Chemrec gasification proc
Page 21 and 22:
Table 3: Average syngas composition
Page 23 and 24:
DME than that could be obtained fro
Page 25 and 26: U.S. Patent[58] and European Patent
Page 27 and 28: Figure 4: Topsøe gas phase technol
Page 29 and 30: DME Workshop, Japan (Sept. 7, 2000)
Page 31 and 32: 2.4.1. Fischer-Tropsch Reactors The
Page 33 and 34: kpH 2 pCO Cobalt rate = 2 (2.4.1) (
Page 35 and 36: invention of Fischer-Tropsch in the
Page 37 and 38: Table 7: hydrocarbons and associate
Page 39 and 40: 3 Process Design 3.1 Pulp Mill 3.1.
Page 41 and 42: carbonate is fired in a lime kiln t
Page 43 and 44: lost and the pulp that provides tha
Page 45 and 46: Table 16: General operating paramet
Page 47 and 48: Table 19: Ash analysis of Pittsburg
Page 49 and 50: Table 22: Experimental syngas compo
Page 51 and 52: 3.2.5 Process Options and Flexibili
Page 53 and 54: Nitrogen compounds Nitrogen from th
Page 55 and 56: 3.3.2.3 Reactors A single-step gas
Page 57 and 58: Table 27: FT-diesel fuel synthesis
Page 59 and 60: 3.5.2 Power Generation Process Desi
Page 61 and 62: Figure 21: Schematic of biorefinery
Page 63 and 64: ar) reacts with the fuel in the com
Page 65 and 66: Figure 25showed the detailed energy
Page 67 and 68: 4. Design Summary The DME design an
Page 69 and 70: Figure 27: Mass and energy flow of
Page 71 and 72: References 1. Åhman, M., G. Modig,
Page 73 and 74: 42. R.A. Peascoe, J.R.K., C.R. Hubb
Page 75: PerformanceSimulation. 2006, Prince
Page 79 and 80: Appendix B: Composite Fuel Blend to
Page 81 and 82: DME Density = 0.67 kg/L (at 20 °C)
Page 83 and 84: Air Separation Unit Requirements Ba
Page 85 and 86: Purge gas: CO conversion is 60%, 40
Page 87 and 88: Appendix D: FTD Synthesis Two diffe
Page 89 and 90: Table D.3: The hydrocarbon product
Page 91 and 92: Figure D.3 Mass and energy balance
Page 93 and 94: Table D.3 Mass and energy balance o
Page 95 and 96: Appendix E: Heat and Power Generati
Page 97 and 98: Energy H2O absorbed MW 46.71 Using
Page 99 and 100: Combustion 2CO+O2→ 2CO2 + 566 kJ/
Page 101 and 102: Specific Heat (cp) b kJ/kgK 1.072 E
Page 103 and 104: Specific Heat of Steam (cp) kJ/kgK
Page 105: Appendix F: Concept Map 105
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