Table A2 Boiling points for acetone 1 butanol and ethanol 102 Specific heat for | Course Hero
Table A2 Boiling points for acetone 1 butanol and ethanol 102 Specific heat for

Table a2 boiling points for acetone 1 butanol and

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Table A2: Boiling points for acetone, 1-butanol and ethanol [102] , Specific heat for acetone, butanol and ethanol [103] Pressure (atm) Boiling point, acetone (°C) Boiling point, 1-butanol (°C) Boiling point, ethanol (°C) Cp, acetone (kJ/kg*K) Cp, 1-butanol (kJ/kg*K) Cp, ethanol (kJ/kg*K) 1 56.5 117.7 78.4 2295 3223 3087 0.9 53 115 76 2282 3183 3050 0.8 50 111 73 2270 3119 3007 0.7 47 108 69 2259 3071 2954 0.6 42 103 65 2241 3000 2896 0.5 38 98 61 2227 2944 2837 0.4 32 93 56 2209 2880 2774 0.3 25 85 49 2187 2784 2689 0.2 16 76 40 2161 2693 2588 0.1 1 60 26 2121 2557 2450
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ii Appendix B Simulations in Aspen Plus Aspen Plus was used to simulate the processes at steady-state, from these simulations, the energy demands and the dimensions for the distillation stages were obtained. Distillation in Aspen Plus In the report from 2008 [1] donut trays was recommended (because of solid substance in the feed). Since donut trays not were available in Aspen Plus, so called bubble caps were instead used in the calculations. The efficiency was set to 100%. The model used to describe to equilibrium between steam-liquid-liquid was an activity factor model (NRTL) [33] . The idea is to get as pure butanol as possible, and at the same time not lose too much. The composition of each stream is shown in tables E1-E7 (Appendix E) and the dimension of each distillation column is shown in tables D15-D18 (Appendix D).
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iii Appendix C Process Calculations Heat Exchangers All heat exchangers are counter-current and have an estimated heat transfer coefficient to 1,0 kW/(m 2 K). The calculation of heat transfer area was made with equations C1 and C2. [Eq. C1] [Eq. C2] Decanters The design of the decanters is based on a retention time of 12 minutes. In the report from 2008 [2] a length to diameter ratio of 3:1 was used, since there is no reason to change it, it is kept the same. Equations C3-C5 were used. [Eq. C3] [Eq. C4] [Eq. C5] Fermenters/Reactors Perstraction Mesitylene as solvent Se Perstraction Oleyl Alcohol/Decane as solvent above for calculations. The extra fermenter volume will be 39 m 3 . Perstraction Oleyl Alcohol/Decane as solvent The extra volume needed in the fermenter is based on a retention time of 10 minutes for the solvent. Equations C3 to C5 are used. The extra fermenter volume will be 62 m 3 .
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iv Feed Composition Perstraction Oleyl Alcohol/Decan as solvent From the 2008 report [1] data presented in table C1 was taken. Table C1: Table with data for calculations of Oleyl/Decan Perstraction ABE ratio [wt%] 21.3:74.5:4.2 Production rate [kg/(m 3 h)] 0.320 Inhibition concentration [kg/m 3 ] 20.0 The perstraction was modeled as a continuous stirred tank reactor (the fermenter) with a smaller tank placed inside it. The two tanks are communicating through a membrane. Through this membrane acetone, butanol, ethanol and water diffuse. The group has made the assumption that mass transfer through the membrane not is the rate limiting step (it is probably the production rate).
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