Preface |
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xvii | |
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1 | (14) |
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2 | (1) |
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Basics of Reactive Distillation |
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3 | (4) |
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Neat Operation Versus Excess Reactant |
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7 | (1) |
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8 | (1) |
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8 | (1) |
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9 | (1) |
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9 | (1) |
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9 | (1) |
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9 | (1) |
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10 | (1) |
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Matlab Programs for Steady-State Design |
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10 | (1) |
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10 | (1) |
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11 | (4) |
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PART I STEADY-STATE DESIGN OF IDEAL QUATENARY SYSTEM |
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15 | (72) |
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17 | (20) |
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Effect of Holdup on Reactive Trays |
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20 | (2) |
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Effect of Number of Reactive Trays |
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22 | (2) |
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24 | (3) |
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Effect of Chemical Equilibrium Constant |
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27 | (2) |
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Effect of Relative Volatilities |
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29 | (3) |
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Constant Relative Volatilities |
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30 | (1) |
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Temperature-Dependent Relative Volatilities |
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30 | (2) |
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Effect of Number of Stripping and Rectifying Trays |
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32 | (1) |
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Effect of Reactant Feed Location |
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33 | (3) |
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Reactant A Feed Location (NFA) |
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33 | (2) |
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Reactant B Feed Location (NFB) |
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35 | (1) |
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36 | (1) |
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Economic Comparison of Reactive Distillation with a Conventional Process |
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37 | (34) |
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Conventional Multiunit Process |
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38 | (5) |
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Assumptions and Specifications |
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38 | (2) |
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Steady-state Design Procedure |
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40 | (2) |
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Sizing and Economic Equations |
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42 | (1) |
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Reactive Distillation Design |
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43 | (4) |
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Assumptions and Specifications |
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44 | (1) |
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Steady-State Design Procedure |
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45 | (2) |
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Results for Different Chemical Equilibrium Constants |
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47 | (14) |
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47 | (7) |
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Reactive Distillation Process |
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54 | (7) |
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61 | (1) |
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Results for Temperature-Dependent Relative Volatilities |
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61 | (9) |
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62 | (2) |
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Optimum Steady-State Designs |
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64 | (5) |
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69 | (1) |
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70 | (1) |
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Neat Operation Versus Using Excess Reactant |
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71 | (16) |
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72 | (1) |
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72 | (3) |
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Two-Column System with Excess B |
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75 | (6) |
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76 | (2) |
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78 | (3) |
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Two-Column System with 20% Excess of A |
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81 | (4) |
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85 | (1) |
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86 | (1) |
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PART II STEADY-STATE DESIGN OF OTHER IDEAL SYSTEMS |
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87 | (58) |
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Ternary Reactive Distillation Systems |
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89 | (30) |
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Ternary System Without Inerts |
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90 | (9) |
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90 | (1) |
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Chemistry and Phase Equilibrium Parameters |
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90 | (2) |
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Design Parameters and Procedure |
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92 | (2) |
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94 | (1) |
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94 | (1) |
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94 | (1) |
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Number of Stripping Trays |
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94 | (5) |
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Ternary System With Inerts |
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99 | (17) |
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99 | (1) |
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Chemistry and Phase Equilibrium Parameters |
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99 | (1) |
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Design Parameters and Procedure |
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100 | (2) |
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102 | (1) |
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103 | (2) |
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105 | (2) |
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107 | (2) |
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Chemical Equilibrium Constant |
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109 | (1) |
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109 | (4) |
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113 | (1) |
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Number of Rectifying and Stripping Trays |
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113 | (3) |
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116 | (3) |
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Ternary Decomposition Reaction |
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119 | (26) |
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Termary Decomposition Reaction: Intermediate-Boiling Reactant |
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120 | (7) |
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120 | (1) |
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Chemistry and Phase Equilibrium Parameters |
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120 | (1) |
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Design Parameters and Procedure |
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121 | (2) |
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123 | (1) |
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124 | (2) |
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Number of Rectifying and Stripping Trays |
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126 | (1) |
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126 | (1) |
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Ternary Decomposition Reaction: Heavy Reactant with Two-Column Configurations |
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127 | (7) |
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127 | (1) |
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Chemistry and Phase Equilibrium Parameters |
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128 | (1) |
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Design Parameters and Procedure |
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128 | (1) |
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129 | (2) |
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131 | (1) |
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Number of Rectifying Trays |
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132 | (2) |
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Ternary Decomposition Reaction: Heavy Reactant with One-Column Configurations |
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134 | (9) |
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134 | (5) |
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139 | (1) |
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Design Parameters and Procedure |
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139 | (1) |
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139 | (1) |
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139 | (1) |
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Number of Rectifying Trays |
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140 | (3) |
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143 | (1) |
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Comparison Between These Two Flowsheets |
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143 | (1) |
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143 | (2) |
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PART III STEADY-STATE DESIGN OF REAL CHEMICAL SYSTEMS |
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145 | (94) |
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Steady-State Design for Acetic Acid Esterification |
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147 | (32) |
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Reaction Kinetics and Phase Equilibria |
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147 | (6) |
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147 | (2) |
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149 | (4) |
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153 | (5) |
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153 | (3) |
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Type II Flowsheet: EtAc and IPAc |
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156 | (1) |
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Type III Flowsheet: BuAc and AmAc |
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157 | (1) |
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158 | (10) |
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158 | (2) |
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160 | (8) |
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168 | (7) |
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168 | (1) |
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168 | (2) |
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170 | (5) |
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175 | (2) |
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177 | (2) |
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Design of Tame Reactive Distillation Systems |
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179 | (34) |
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Chemical Kinetics and Phase Equilibrium |
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180 | (14) |
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180 | (1) |
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Phase Equilibrium Using Aspen Plus |
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181 | (5) |
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186 | (8) |
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194 | (1) |
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Prereactor and Reactive Column |
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195 | (13) |
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Base Case Design of Reactive Column |
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195 | (4) |
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Effect of Design Parameters on Reactive Column |
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199 | (9) |
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Pressure-Swing Methanol Separation Section |
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208 | (1) |
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Extractive Distillation Methanol Separation Section |
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209 | (1) |
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210 | (2) |
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212 | (1) |
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Design of MTBE and ETBE Reactive Distillation Columns |
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213 | (26) |
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213 | (18) |
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214 | (1) |
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214 | (1) |
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Aspen Plus Simulation Issues |
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214 | (1) |
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Setting up the Aspen Plus Simulation |
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215 | (6) |
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Effect of Design parameters |
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221 | (8) |
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Chemical Equilibrium Model |
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229 | (2) |
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231 | (6) |
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231 | (1) |
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232 | (1) |
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232 | (2) |
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Chemical Equilibrium Model |
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234 | (2) |
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Effects of Design parameters |
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236 | (1) |
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237 | (2) |
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PART IV CONTROL OF IDEAL SYSTEMS |
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239 | (114) |
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Control of Quaternary Reactive Distillation Columns |
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241 | (20) |
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242 | (1) |
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243 | (2) |
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245 | (1) |
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Selection of Control Tray Location |
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246 | (1) |
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247 | (2) |
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247 | (1) |
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248 | (1) |
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Using More Reactive Trays |
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249 | (5) |
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249 | (1) |
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250 | (3) |
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Dynamic Performance of CS7-RR |
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253 | (1) |
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Increasing Holdup on Ractive Trays |
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254 | (2) |
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256 | (3) |
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259 | (2) |
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Control of Excess Reactant Systems |
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261 | (32) |
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Control Degrees of Freedom |
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261 | (2) |
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Sigle Reactive Column Control Structures |
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263 | (15) |
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Two-Temperature Control Structure |
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265 | (7) |
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Internal Composition control Structure |
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272 | (6) |
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Control of Two-Column System |
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278 | (14) |
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279 | (6) |
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Temperature/Composition Cascade Control |
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285 | (7) |
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292 | (1) |
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Control of Ternary Reactive Distillation Columns |
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293 | (60) |
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Ternary System Without Inerts |
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293 | (17) |
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293 | (3) |
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296 | (4) |
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300 | (3) |
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303 | (7) |
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Ternary System With Inerts |
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310 | (14) |
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310 | (1) |
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310 | (4) |
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314 | (6) |
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320 | (2) |
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Conclusion for Ternary A+B⇔ C System |
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322 | (2) |
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Ternary A⇔B+c System: Intermediate-Boiling Reactant |
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324 | (10) |
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324 | (2) |
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326 | (3) |
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329 | (5) |
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334 | (1) |
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Ternary A ⇔ B+C System: Heavy Reactant With Two-Column Confiuration |
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334 | (8) |
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334 | (1) |
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334 | (1) |
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335 | (7) |
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Ternary A ⇔ B+C System: Heavy Reactant With One-Column Configuration |
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342 | (11) |
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342 | (1) |
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342 | (2) |
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344 | (1) |
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345 | (7) |
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Conclusion for Ternary A ⇔ B+C System |
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352 | (1) |
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PART V CONTROL OF REAL SYSTEMS |
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353 | (76) |
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Control of Reactive Distillations for Acetic Acid Esterification |
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355 | (34) |
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355 | (7) |
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355 | (1) |
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356 | (6) |
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362 | (18) |
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Selection of Temperature Control Trays |
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363 | (3) |
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Control Struture and Controller Design |
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366 | (2) |
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368 | (8) |
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Alternative Temperature Control Structures |
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376 | (4) |
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Extension to Composition Control |
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380 | (8) |
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388 | (1) |
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Plantwide Control Of Tame Reactive Distillation System |
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389 | (18) |
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389 | (8) |
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389 | (1) |
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390 | (1) |
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391 | (6) |
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Methanol Recovery Column C3 |
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397 | (1) |
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397 | (6) |
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397 | (2) |
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Reactive Distillation Column C1 |
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399 | (1) |
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Extractive Distillation Column C2 |
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399 | (2) |
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Methanol Recovery Column C3 |
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401 | (2) |
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403 | (3) |
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406 | (1) |
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Control Of MTBE And ETBE Reactive Distillation Columns |
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407 | (22) |
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407 | (11) |
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407 | (1) |
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Control Struture with C4 Feedflow Controlled |
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408 | (8) |
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Control Structure With Methanol Feedflow Controlled |
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416 | (2) |
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418 | (11) |
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Control Structure with Flow Control of C4 Feed |
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419 | (5) |
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Control Structure With Flow control of Ethanol Feed |
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424 | (5) |
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PART VI HYDRID AND NONCONVENTIONAL SYSTEMS |
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429 | (116) |
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Design and Control of Column/Side Reactor Systems |
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431 | (56) |
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431 | (2) |
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Design for Quaternary Ideal System |
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433 | (13) |
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Assumptions and Specifications |
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434 | (1) |
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Reactor and Column Equations |
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435 | (1) |
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Design Optimization Procedure |
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436 | (1) |
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437 | (8) |
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Reactive Column with Optimum Feed Tray Locations |
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445 | (1) |
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Control of Quaternary Ideal System |
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446 | (12) |
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Dynamic Tubular Reactor Model |
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446 | (1) |
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447 | (11) |
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Design of Column/Side Reactor process for Ethyl Acetate System |
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458 | (16) |
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458 | (1) |
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459 | (15) |
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Control of Column/Side Reactor Process for Ethyl Acetate System |
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474 | (11) |
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Determining Manipulated Variables |
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475 | (4) |
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Selection of Temperature Control Trays |
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479 | (2) |
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481 | (1) |
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481 | (4) |
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Extension to Composition Control |
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485 | (1) |
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Comparison with Reactive Distillation Temperature Control |
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485 | (1) |
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485 | (2) |
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Effects of Boiling Point Rankings on the Design of Reactive Distilation |
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487 | (32) |
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Process and Classification |
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487 | (5) |
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487 | (3) |
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490 | (2) |
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Relaxation and Convergence |
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492 | (3) |
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495 | (16) |
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496 | (5) |
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501 | (6) |
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507 | (4) |
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511 | (7) |
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511 | (3) |
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514 | (4) |
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518 | (1) |
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Effects of Feed Tray Locations on Design and Control of Reactive Distillation |
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519 | (26) |
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519 | (10) |
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521 | (1) |
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522 | (1) |
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522 | (1) |
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Feed Locations Versus Reactants Distribution |
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523 | (4) |
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527 | (2) |
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Effects of Relative Volatilities |
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529 | (4) |
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Changing Relative Volatilities of Reactants |
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529 | (1) |
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Changing Relative Volatilities of Products |
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530 | (2) |
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532 | (1) |
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Effects of Reaction Kinetics |
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533 | (5) |
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Reducing Activation Energies |
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533 | (3) |
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Effects of Preexponential Factor |
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536 | (2) |
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538 | (6) |
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Optimal Feed Location for Production Rate Variation |
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538 | (1) |
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539 | (2) |
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541 | (3) |
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544 | (1) |
Appendix Catalog of Types of Real Reactive Distillation Systems |
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545 | (18) |
References |
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563 | (10) |
Index |
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573 | |