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

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Clean syngas 123.0 kg/s 1437.8 MW 145 o C 50 bar Clean syngas 123.0 kg/s 1437.8 MW Tail gas 91.5 kg/s 118 o C 29.4 bar Tail Gas 60.4 kg/s 492.9 MW 260 o C 30.3 bar Slurry-phase bubbling-bed reactor Steam 96.3 kg/s 86 o C 10 bar Water 96.3 kg/s 15 o C 10bar Steam 128.8 kg/s 2.846 MW 260 o C 38 bar Water 15 o C 38 bar Tail gas 91.5 kg/s 38 o C 29.4 bar FT Liquid 6.2 kg/s Condenser FT Liquid 10.8 kg/s Unconverted syngas 60.4 kg/s 492.9 MW 38 o C 26.6bar Water 20.3 kg/s Wax Hydrocracking Wax C20+ 11.9 kg/s FT Separator FT Product C1-C4 0.6 kg/s 46.0 MW Distillate C12–C20 2.9 kg/s Naphtha C5–C11 1.9 kg/s Diesel 9.5 kg/s Naphtha 1.8 kg/s Diesel 12.4 kg/s 8667.9 bbl/d 536.1 MW Naphtha 3.7 kg/s 2552.9 bbl/d 161.2 MW Figure D.5: Mass and energy balance of the Larson et al case study FTD design both with estimated final produce from upgrading. The syngas to FT-product efficiency of the FTD project design based on Larson et al. is 48.5 %, where the design based on the Steynberg et al. case study is 52.6 %. The FTD design based on the Larson et al. case study was used for this project, because its scale is closer to that of the case study it was based on, thus providing a more likely efficiency. Diesel conversion: bbl kg 1 = 0. 001435 day s ton kg 1 = 0. 277778 hour s Well to tank report LHV Diesel 43.1 MJ/kg Naptha 44 MJ/kg Methane 50 MJ/kg kg bbl 4 . 3 = 2996. 516 s day kg ton 1 = 3. 599997 s hour 94
Appendix E: Heat and Power Generation 1. Heat Recovery Calculation Property of raw syngas: Temperature °C 1400 Pressure bar 50 Flow Rate kg/s 123 Energy MWt 1437.8 CO:H2 0.8096 H2 mole percent % 37 H2 mass percent % 3.66 H2 cp a kJ/kgK 16.39 CO mole percent % 45.7 CO mass percent % 62.68 CO cp b kJ/kgK 1.273 a. http://www.engineeringtoolbox.com/hydrogen-d_976.html b. http://www.engineeringtoolbox.com/carbon-monoxide-d_975.html Property of cooled syngas: Temperature °C 400 Pressure bar 50 Flow Rate kg/s 123 H2 cp kJ/kgK 14.58 CO cp kJ/kgK 1.106 Energy supplied from cooler MW 179.81 Energy to generate steam for ST MW 173.05 Heat Exchange: Saturated Water Temperature °C 120.6 Pressure bar 1.01 cp a kJ/kgK 1.901 a. http://www.engineeringtoolbox.com/water-vapor-d_979.html MP Steam Heat Exchanger MP Steam Temperature °C 195 Pressure bar 13 Flow Rate kg/s 31.5 cp kJ/kgK 2.733 95
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
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1 Introduction The global transport
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2 Background 2.1 Pulp Mill Backgrou
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2.1.2.2 Chemical Pulping The most c
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sodium sulfide and sodium carbonate
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process described in the section on
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2.2.1 Low-Temperature Black Liquor
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Figure 2: Chemrec gasification proc
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Table 3: Average syngas composition
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DME than that could be obtained fro
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U.S. Patent[58] and European Patent
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Figure 4: Topsøe gas phase technol
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DME Workshop, Japan (Sept. 7, 2000)
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2.4.1. Fischer-Tropsch Reactors The
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kpH 2 pCO Cobalt rate = 2 (2.4.1) (
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invention of Fischer-Tropsch in the
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Table 7: hydrocarbons and associate
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3 Process Design 3.1 Pulp Mill 3.1.
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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 and 76: PerformanceSimulation. 2006, Prince
Page 77 and 78: Appendix Appendix A MP Steam Demand
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: Table D.3 Mass and energy balance o
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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