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

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Figure D.4: Energy and mass balance of Larson et al. case study The Larson et al. case study is based on 47.1 kg/s of clean syngas, which is a low flow rate than that of this project’s FTD design. Larson et al. gave no information on product selectivity of its FT-products. An assumption can be made that a LTFT reactor will target high wax production to achieve the largest amount of FTD possible. An α to target FTD production will be no less than 0.9. Thus, an α of 0.94 was assumed as in the previous case. The Larson et al. case study did not provide a composition of the syngas used, however it did give a H2/CO ratio of 1.11. This mean that the syngas used in the Larson et al. case study is more energetic than the syngas produced and used in this project design. Table D.4 and Figure D.5 give the mass and energy balance of the Larson et al. and the FTD design used for this project. The final design is scaled up from Larson et al. at a factor 2.1. Table D.4 and Figure D.5 were scaled and developed using the same method and assumptions used to create Figure D.3 and table D.4 92
Table D.3 Mass and energy balance of the Larson et al. case study FTD design both with estimated final produce from upgrading. Larson et al. FTD design Coal feed mass flow [kg/s] 54.8 Coal feed energy [MW] 1908.1 Black liquor mass flow [kg/s] 11.0 Black liquor energy [MW] 132.5 Total fuel feed mass flow [kg/s] 65.9 Total fuel feed energy [MW] 2040.5 Clean syngas [kg/s] 47.1 123.0 Clean syngas LHV [MJ/kg] 14.7 11.7 Clean syngas [MW] Hydrocarbon condensate [kg/s] Wax [kg/s] 692.8 1437.8 Total products [kg/s] 8.2 17.0 scale 2.1 2.1 FT-product C20+ [kg/s] 5.7 11.9 FT-product C12-C20 [kg/s] 1.4 2.9 FT-product C5-C11 [kg/s] 0.9 1.9 Tailgas flow [kg/s] 29.1 60.4 Tailgas LHV [MJ/kg] 8.2 8.2 Tailgas [MW] 237.5 492.9 C1-C4 in tail gas [kg/s] 0.2 0.3 C1-C4 LHV approximant [MJ/kg] 46.0 46.0 C1-C4 Energy [MW] 7.6 15.7 waste gas in tailgas [kg/s] 28.9 60.1 waste gas in tailgas [MW] 229.9 477.2 Wax cracking product - diesel [kg/s] 4.6 9.5 Wax cracking product - naphtha [kg/s] 0.9 1.8 Wax cracking product - C1-C4 [kg/s] 0.3 0.6 Diesel [kg/s] 6.0 12.4 Diesel [bbl/day] 4176.5 8667.9 Diesel LHV [MJ/kg] 43.1 43.1 Diesel energy [MW] 258.3 536.1 Naphtha [kg/s] 1.8 3.7 Naphtha [bbl/day] 1230.1 2552.9 Naptha LHV [MJ/kg] 44 44 Naphtha energy [MW] 77.7 161.2 C1-C4 [kg/s] 0.9 0.6 C1-C4 LHV approximant [MJ/kg] 46.0 46.0 C 1-C 4 Energy [MW] 45.2 29.8 Energy sum MW 336.0 697.3 Syngas to FT-product efficiency [%] 48.5 48.5 Feed to FT-product efficiency [%] 0.34 93
Page 1 and 2:
Novel Design of an Integrated Pulp
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Table of Contents List of Figures .
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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
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 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: Figure D.3 Mass and energy balance
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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