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

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Figure 12: Equilibrium conversion of synthesis gas. Figure 13: The effect of the H2/CO ratio on DME productivity and materials utilization. Air Products and Chemicals also drew the same conclusion[103]. A very strong dependence of the DME productivity on the H2/CO ratio in the fresh feed gas is observed. The maximum productivity occurs at a H2/CO ratio of 1.0. The productivity drops by about 65% and 44% when the ratio changes to 0.5 and 1.5. Since our syngas H2/CO ratio is about 0.8 which is close to 1, we will directly use the cleaned syngas. 3.3.2.2 Catalyst system for the single-stage DME synthesis The single-step DME synthesis catalysts are powdered catalysts contains between about 75 and about 90 wt % copper-containing methanol synthesis catalyst and the remainder of said powdered catalyst consists essentially of methanol dehydration catalyst[104]. The methanol synthesis catalyst is Cu/ZnO/Al2O3 and methanol dehydration catalyst is alumina. To main the catalyst activity, stability and reaction activity, 270 o C and 50 bar are chosen as the operation conditions. 54
3.3.2.3 Reactors A single-step gas phase process would generally require less equipment than multi-step gas processes. However, a single-step gas-phase process would still suffer from a large reactor exotherm due to the high net heat of reaction. Hence, it is necessary to remove reaction heat and perform reaction temperature control properly in order to prevent a reduction of equilibrium conversion and catalyst deactivation due to temperature rise. A slurry phase reactor is going to be used in which the reaction is promoted by placing the synthesis gas in contact with the catalyst in slurry in which the catalyst is suspended in a reaction medium. Because the heat capacity and thermal conductivity of the reaction medium are both large, the reaction heat is absorbed by the reaction medium and leveling of the temperature in the reactor is easy. Figure 14: Concept of slurry phase rector (JFE Holdings, Inc). . Figure 15: Conversion and selectivity as a function of H2/CO. 55
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: Nitrogen compounds Nitrogen from th
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 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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