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

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Black Liquor Used Modified Steam Demand Modified MP Steam Demand tonnes kg MJ 1 day 950 * 1000 * 12. 1 * = 133. 04MW day tonne kg 86400 seconds Steam tables show the specific enthalpy of MP steam at 11 bar and 200 degrees Celsius to be 2.822 GJ/tonne. Modified LP Steam Demand GJ ADt 1 day 1 tonneMPsteam tonne 4 . 3 * 2000 * * = 119. 3 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 Na2SO4 required GJ ADt 1 day 1 tonneMPsteam tonne 5 . 68 * 2000 * * = 150. 4 ADt day 24 hr 2. 732 GJ hr tonne tonne 150 . 4 + 119. 3 = 269. 7 hr hr tonne hr 1 tonneNa2SO4 tonneNa2SO 144130 * = 17534 day . 822 tonneNaOH day tonneNaOH 4 78
Appendix B: Composite Fuel Blend to Texaco Gasifier Solids requirement: 55 wt. % solids Black liquor solids content: 0.17 kg solid/kg weak black liquor Assuming 100 kg of black liquor feed: 83 kg water 17 kg black liquor solids To achieve 55 wt% solids: ( 17 + x) 17 + 83 + x ( ) = 0.55 Coal requirement = x = 84.4 kg Based on the solids distribution 84.4 kg coal/17 kg black liquor and the composition of coal and black liquor, the composite fuel blend composition was calculated using Excel. From BL (kg) From Coal (kg) Total (kg) Wt. Percent Carbon 6.1 62.7 68.7 67.8% Hydrogen 0.6 4.3 4.9 4.9% Nitrogen 0.0 1.1 1.2 1.1% Sulfur 0.7 3.3 4.0 4.0% Oxygen 6.1 5.1 11.2 11.0% Sodium 3.2 0 3.2 3.2% Potassium 0.2 0 0.2 0.2% Chlorine 0.1 0 0.1 0.05% SiO2 0 2.9 2.894 2.9% Al2O3 0 1.4 1.403 1.4% TiO2 0 0.1 0.061 0.1% Fe2O3 0 2.9 2.926 2.9% MgO 0 0.0 0.048 0.0% CaO 0 0.2 0.242 0.2% Na2O 0 0.0 0.026 0.0% K2O 0 0.1 0.112 0.1% P2O5 0 0.0 0.005 0.0% SO3 0 0.1 0.136 0.1% Total (kg) 17.0 84.3 101.3 79
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
Page 11 and 12:
2.1.2.2 Chemical Pulping The most c
Page 13 and 14:
sodium sulfide and sodium carbonate
Page 15 and 16:
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 and 76: PerformanceSimulation. 2006, Prince
Page 77: Appendix Appendix A MP Steam Demand
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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