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

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Chemrec Gasification Process Table B.4: Fuel input and syngas component mass flow rates. Temp 975 C Pressure 32 bar Oxygen 1172 ton/day Gasifier Feed 140 ton/hr Black Liquor 3420 dry tons/day DME yield 824 tons/day Table B.5: Fuel input and syngas component mass flow rates[94]. Syngas mole% H2 30.55 CO 29.70 CO2 14.93 CH4 1.05 N2 0.19 H20 22.09 H2S 1.44 COS 0.05 H2/CO 1.03 82
Air Separation Unit Requirements Based on the design by D. Cocco for an IGCC power plant for DME synthesis, the oxygen pressure should be compressed to 1.2 times the gasifier pressure. Assuming gasifier pressure of 50 bar Oxygen pressure = (1.2)*(50) = 60 bar The mass flow rate of oxygen from the ASU to the gasifier was determined by the oxygen-fuel requirement the gasifier. Oxygen-to-fuel requirement = 0.9 kg oxygen/kg fuel Oxygen mass flow rate = (0.9)*(65.9) = 60.3 kg/s The air flow rate required to the ASU was determined by calculating the air to oxygen mass flow rate ratios for the D. Cocco IGCC design and relating them to our design. Similarly, the energy contained in the oxygen from the ASU to the gasifier was calculated using the ratio approach. D. Cocco Our Design Oxygen (kg/s) 68.1 60.3 Air (kg/s) 278.6 X Oxygen (MW) 68.1 X Oxygen mass flow rate = X = [(60.3)*(278.6)]/68.1 = 242.6 kg/s Oxygen energy content = X = [(60.3)*(113)]/68.1 = 98.4 MW 83
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Novel Design of an Integrated Pulp
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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
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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
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 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: DME Density = 0.67 kg/L (at 20 °C)
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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