1 | #*------------------------------------------------------------------- |
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2 | * EMSO Model Library (EML) Copyright (C) 2004 - 2007 ALSOC. |
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3 | * |
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4 | * This LIBRARY is free software; you can distribute it and/or modify |
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5 | * it under the therms of the ALSOC FREE LICENSE as available at |
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6 | * http://www.enq.ufrgs.br/alsoc. |
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7 | * |
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8 | * EMSO Copyright (C) 2004 - 2007 ALSOC, original code |
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9 | * from http://www.rps.eng.br Copyright (C) 2002-2004. |
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10 | * All rights reserved. |
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11 | * |
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12 | * EMSO is distributed under the therms of the ALSOC LICENSE as |
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13 | * available at http://www.enq.ufrgs.br/alsoc. |
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14 | * |
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15 | *-------------------------------------------------------------------- |
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16 | * Sample file for column model |
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17 | *-------------------------------------------------------------------- |
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18 | * |
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19 | * This sample file needs VRTherm DEMO(www.vrtech.com.br) to run |
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20 | * SectionColumn_Test and needs VRTherm full to run the distillation |
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21 | * column flowsheet. |
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22 | * |
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23 | *---------------------------------------------------------------------- |
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24 | * Author: Paula B. Staudt |
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25 | * $Id: sample_column.mso 208 2007-03-15 05:18:39Z arge $ |
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26 | *--------------------------------------------------------------------*# |
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27 | |
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28 | using "stage_separators/column"; |
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29 | using "controllers/PIDIncr"; |
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30 | |
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31 | # column section with 2 trays |
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32 | FlowSheet SectionColumn_Test_with2tray |
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33 | PARAMETERS |
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34 | PP as Plugin(Brief="Physical Properties",File="vrpp"); |
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35 | NComp as Integer; |
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36 | |
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37 | SET |
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38 | PP.Components = [ "isobutane", "benzene"]; |
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39 | PP.LiquidModel = "PR"; |
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40 | PP.VapourModel = "PR"; |
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41 | NComp = PP.NumberOfComponents; |
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42 | |
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43 | DEVICES |
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44 | sec as Section_Column; |
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45 | feed as liquid_stream; |
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46 | reb as vapour_stream; |
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47 | cond as liquid_stream; |
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48 | zero as stream; |
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49 | |
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50 | CONNECTIONS |
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51 | feed to sec.trays(2).Inlet; |
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52 | zero to sec.trays(1).Inlet; |
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53 | reb to sec.trays(2).InletV; |
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54 | cond to sec.trays(1).InletL; |
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55 | |
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56 | SPECIFY |
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57 | feed.F = 113.4 * 'kmol/h'; |
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58 | feed.T = 291 * 'K'; |
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59 | feed.P = 168.3 * 'kPa'; |
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60 | feed.z = [0.5, 0.5]; |
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61 | |
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62 | zero.F = 0 * 'kmol/h'; |
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63 | zero.T = 300 * 'K'; |
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64 | zero.P = 1 * 'atm'; |
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65 | zero.z = [0.5, 0.5]; |
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66 | zero.v = 0; |
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67 | zero.h = 0 * 'J/mol'; |
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68 | |
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69 | cond.F = 68 * 'kmol/h'; |
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70 | cond.P = 150 * 'kPa'; |
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71 | cond.T = 281.75 * 'K'; |
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72 | cond.z = [0.6664, 0.3336]; |
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73 | |
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74 | reb.F = 153 * 'kmol/h'; |
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75 | reb.P = 185 * 'kPa'; |
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76 | reb.T = 328.12 * 'K'; |
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77 | reb.z = [0.001848, 0.9982]; |
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78 | |
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79 | sec.trays.Emv = 1; |
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80 | |
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81 | SET |
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82 | sec.NTrays = 2; |
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83 | #COLUMN |
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84 | sec.trays.V = 4 * 'ft^3'; |
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85 | sec.trays.Ah = 0.394 * 'ft^2'; |
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86 | sec.trays.lw = 20.94 * 'in'; |
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87 | sec.trays.hw = 0.125 * 'ft'; |
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88 | sec.trays.Q = 0 * 'kW'; |
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89 | sec.trays.beta = 0.6; |
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90 | sec.trays.alfa = 4; |
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91 | sec.trays.Ap = 3.94 * 'ft^2'; |
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92 | |
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93 | INITIAL |
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94 | sec.trays.OutletL.T = 290 *'K'; |
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95 | sec.trays.Level = 0.9 * sec.trays.hw; |
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96 | sec.trays.OutletL.z(1) = 0.5; |
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97 | |
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98 | OPTIONS |
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99 | #RelativeAccuracy = 1e-3; |
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100 | NLASolver = "sundials"; |
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101 | TimeStep = 10; |
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102 | TimeEnd = 1000; |
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103 | |
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104 | # After running few seconds of transient the steady-state |
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105 | # can be obtained by using the results from that transient: |
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106 | |
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107 | #GuessFile="SectionColumn_Test_with2tray.rlt"; |
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108 | #Dynamic = false; |
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109 | end |
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110 | |
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111 | # column section with 8 trays |
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112 | FlowSheet SectionColumn_Test_with8tray |
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113 | PARAMETERS |
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114 | PP as Plugin(Brief="Physical Properties",File="vrpp"); |
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115 | NComp as Integer; |
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116 | |
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117 | SET |
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118 | PP.Components = [ "isobutane", "benzene"]; |
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119 | PP.LiquidModel = "PR"; |
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120 | PP.VapourModel = "PR"; |
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121 | PP.Derivatives = 0; |
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122 | NComp = PP.NumberOfComponents; |
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123 | |
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124 | DEVICES |
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125 | sec as Section_Column; |
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126 | feed as liquid_stream; |
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127 | reb as vapour_stream; |
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128 | cond as liquid_stream; |
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129 | zero as stream; |
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130 | |
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131 | CONNECTIONS |
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132 | feed to sec.trays(5).Inlet; |
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133 | |
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134 | zero to sec.trays([1:4]).Inlet; |
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135 | zero to sec.trays([6:8]).Inlet; |
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136 | |
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137 | reb to sec.trays(8).InletV; |
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138 | cond to sec.trays(1).InletL; |
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139 | |
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140 | SPECIFY |
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141 | feed.F = 113.4 * 'kmol/h'; |
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142 | feed.T = 291 * 'K'; |
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143 | feed.P = 168.3 * 'kPa'; |
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144 | feed.z = [0.5, 0.5]; |
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145 | |
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146 | zero.F = 0 * 'kmol/h'; |
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147 | zero.T = 300 * 'K'; |
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148 | zero.P = 1 * 'atm'; |
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149 | zero.z = [0.5, 0.5]; |
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150 | zero.v = 0; |
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151 | zero.h = 0 * 'J/mol'; |
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152 | |
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153 | cond.F = 68 * 'kmol/h'; |
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154 | cond.P = 150 * 'kPa'; |
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155 | cond.T = 281.75 * 'K'; |
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156 | cond.z = [0.6664, 0.3336]; |
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157 | |
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158 | reb.F = 153 * 'kmol/h'; |
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159 | reb.P = 185 * 'kPa'; |
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160 | reb.T = 328.12 * 'K'; |
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161 | reb.z = [0.001848, 0.9982]; |
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162 | |
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163 | sec.trays.Emv = 1; |
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164 | |
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165 | SET |
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166 | sec.NTrays = 8; |
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167 | #COLUMN |
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168 | sec.trays.V = 4 * 'ft^3'; |
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169 | sec.trays.Ah = 0.394 * 'ft^2'; |
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170 | sec.trays.lw = 20.94 * 'in'; |
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171 | sec.trays.hw = 0.125 * 'ft'; |
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172 | sec.trays.Q = 0 * 'kW'; |
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173 | sec.trays.beta = 0.6; |
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174 | sec.trays.alfa = 4; |
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175 | sec.trays.Ap = 3.94 * 'ft^2'; |
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176 | |
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177 | INITIAL |
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178 | sec.trays.OutletL.T = [290:(330-290)/(sec.NTrays-1):330] *'K'; |
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179 | sec.trays.Level = 0.3 * sec.trays.hw; |
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180 | sec.trays.OutletL.z(1) = 0.5; |
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181 | |
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182 | OPTIONS |
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183 | RelativeAccuracy = 1e-5; |
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184 | TimeStep = 1; |
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185 | TimeEnd = 100; |
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186 | #GuessFile="SectionColumn_Test_with8tray.rlt"; |
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187 | #Dynamic = false; |
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188 | end |
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189 | |
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190 | |
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191 | FlowSheet Distillation_kettle_cond_Test |
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192 | PARAMETERS |
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193 | PP as Plugin(Brief="Physical Properties",File="vrpp"); |
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194 | NComp as Integer; |
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195 | |
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196 | VARIABLES |
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197 | Qc as heat_rate (Brief="Heat rate removed from condenser"); |
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198 | Qr as heat_rate (Brief="Heat rate supplied to reboiler"); |
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199 | |
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200 | SET |
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201 | PP.Components = [ "isobutane", "n-pentane", "propylene", |
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202 | "benzene", "isobutene" ]; |
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203 | PP.LiquidModel = "PR"; |
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204 | PP.VapourModel = "PR"; |
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205 | PP.Derivatives = 1; |
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206 | NComp = PP.NumberOfComponents; |
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207 | |
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208 | DEVICES |
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209 | col as Distillation_kettle_cond; |
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210 | feed as source; |
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211 | zero as stream; |
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212 | |
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213 | CONNECTIONS |
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214 | feed.Outlet to col.trays(5).Inlet; |
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215 | zero to col.reb.Inlet; |
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216 | zero to col.trays([1:4]).Inlet; |
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217 | zero to col.trays([6:col.NTrays]).Inlet; |
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218 | Qc to col.cond.Q; |
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219 | Qr to col.reb.Q; |
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220 | |
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221 | SPECIFY |
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222 | feed.Outlet.F = 113.4 * 'kmol/h'; |
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223 | feed.Outlet.T = 291 * 'K'; |
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224 | feed.Outlet.P = 168.3 * 'kPa'; |
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225 | feed.Outlet.z = 1/NComp; |
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226 | |
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227 | zero.F = 0 * 'kmol/h'; |
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228 | zero.T = 300 * 'K'; |
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229 | zero.P = 1 * 'atm'; |
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230 | zero.z = 1/NComp; |
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231 | zero.v = 0; |
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232 | zero.h = 0 * 'J/mol'; |
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233 | |
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234 | col.sptop.Outlet2.F = 85 * 'kmol/h'; |
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235 | col.reb.OutletL.F = 28.4 * 'kmol/h'; |
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236 | col.sptop.frac = 0.444445; |
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237 | col.cond.OutletV.F = 0 * 'kmol/h'; |
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238 | Qr = 3.7743e6 * 'kJ/h'; |
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239 | Qc = -3.71e6 * 'kJ/h'; |
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240 | col.pump1.dP = 16 * 'kPa'; |
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241 | col.trays.Emv = 1; |
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242 | |
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243 | SET |
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244 | col.NTrays = 8; |
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245 | col.cond.V = 2 * 'm^3'; |
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246 | col.cond.Across = 1 * 'm^2'; |
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247 | col.trays.V = 4 * 'ft^3'; |
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248 | col.trays.Ah = 0.394 * 'ft^2'; |
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249 | col.trays.lw = 20.94 * 'in'; |
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250 | col.trays.hw = 0.125 * 'ft'; |
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251 | col.trays.Q = 0 * 'kW'; |
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252 | col.trays.beta = 0.6; |
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253 | col.trays.alfa = 4; |
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254 | col.trays.Ap = 3.94 * 'ft^2'; |
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255 | col.reb.V = 2 * 'm^3'; |
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256 | col.reb.Across = 1 * 'm^2'; |
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257 | |
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258 | INITIAL |
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259 | # condenser |
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260 | col.cond.OutletL.T = 260 *'K'; |
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261 | col.cond.Level = 1 * 'm'; |
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262 | col.cond.OutletL.z([1:4]) = [0.65, 0.05, 0.01, 0.01]; |
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263 | |
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264 | # reboiler |
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265 | col.reb.OutletL.T = 330 *'K'; |
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266 | col.reb.Level = 1 * 'm'; |
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267 | col.reb.OutletL.z([1:4]) = [0.1, 0.7, 0.01, 0.01]; |
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268 | |
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269 | # column trays |
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270 | col.trays.OutletL.T = [290:(330-290)/(col.NTrays-1):330] * 'K'; |
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271 | col.trays.Level = 1.2 * col.trays.hw; |
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272 | col.trays.OutletL.z([1:4]) = [0.5, 0.05, 0.01, 0.01]; |
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273 | |
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274 | OPTIONS |
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275 | RelativeAccuracy = 1e-3; |
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276 | TimeStep = 0.1; |
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277 | TimeEnd = 50; |
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278 | #time = [0:0.01:1, 2:50]; |
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279 | #GuessFile="Distillation_kettle_cond_Test.rlt"; |
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280 | #Dynamic = false; |
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281 | end |
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282 | |
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283 | FlowSheet Column_ctrl |
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284 | PARAMETERS |
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285 | PP as Plugin(Brief="Physical Properties",File="vrpp"); |
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286 | NComp as Integer; |
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287 | |
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288 | Qcmin as heat_rate (Brief="Minimum Condenser Heat supplied"); |
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289 | Qcmax as heat_rate (Brief="Maximum Condenser Heat supplied"); |
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290 | Qrmin as heat_rate (Brief="Minimum Reboiler Heat supplied"); |
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291 | Qrmax as heat_rate (Brief="Maximum Reboiler Heat supplied"); |
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292 | Frmin as flow_mol (Brief="Minimum bottom flow rate"); |
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293 | Frmax as flow_mol (Brief="Maximum bottom flow rate"); |
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294 | Fcmin as flow_mol (Brief="Minimum reflux flow rate"); |
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295 | Fcmax as flow_mol (Brief="Maximum reflux flow rate"); |
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296 | Hmint as length (Brief="Minimum liquid level in top tank"); |
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297 | Hmaxt as length (Brief="Maximum liquid level in top tank"); |
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298 | Hminb as length (Brief="Minimum liquid level in reboiler"); |
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299 | Hmaxb as length (Brief="Maximum liquid level in reboiler"); |
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300 | Pmax as pressure (Brief="Maximum column pressure"); |
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301 | Pmin as pressure (Brief="Minimum column pressure"); |
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302 | Tmax as temperature (Brief="Maximum column temperature"); |
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303 | Tmin as temperature (Brief="Minimum column temperature"); |
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304 | |
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305 | VARIABLES |
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306 | Qc as heat_rate (Brief="Heat rate removed from condenser"); |
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307 | Qr as heat_rate (Brief="Heat rate supplied to reboiler"); |
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308 | Had_top as Real (Brief="Dimensionless condenser level"); |
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309 | Had_bot as Real (Brief="Dimensionless reboiler level"); |
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310 | Pad as Real (Brief="Dimensionless pressure"); |
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311 | Tad as Real (Brief="Dimensionless temperature"); |
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312 | RR as positive (Brief="Reflux ratio"); |
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313 | |
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314 | SET |
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315 | PP.Components = [ "isobutane", "n-pentane", "propylene", |
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316 | "benzene", "isobutene" ]; |
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317 | PP.LiquidModel = "PR"; |
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318 | PP.VapourModel = "PR"; |
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319 | PP.Derivatives = 1; |
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320 | NComp = PP.NumberOfComponents; |
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321 | |
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322 | DEVICES |
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323 | col as Distillation_kettle_cond; |
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324 | feed as source; |
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325 | zero as stream; |
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326 | TCcond as PIDIncr_Ideal_AW; |
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327 | LCtop as PIDIncr_Ideal_AW; |
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328 | LCbot as PIDIncr_Ideal_AW; |
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329 | PC as PIDIncr_Ideal_AW; |
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330 | |
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331 | CONNECTIONS |
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332 | feed.Outlet to col.trays(5).Inlet; |
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333 | zero to col.reb.Inlet; |
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334 | zero to col.trays([1:4]).Inlet; |
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335 | zero to col.trays([6:col.NTrays]).Inlet; |
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336 | Qc to col.cond.Q; |
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337 | Qr to col.reb.Q; |
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338 | |
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339 | EQUATIONS |
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340 | "Temperature Controller" |
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341 | TCcond.Parameters.tau = 0*'s'; |
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342 | TCcond.Parameters.tauSet = 0*'s'; |
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343 | TCcond.Parameters.alpha = 0.3; |
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344 | TCcond.Parameters.bias = 0.5; |
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345 | TCcond.Parameters.gamma = 1; |
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346 | TCcond.Parameters.beta = 1; |
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347 | TCcond.Options.action = 1; |
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348 | TCcond.Options.clip = 1; |
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349 | TCcond.Options.autoMan = 0; |
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350 | TCcond.Parameters.intTime = 60*'s'; |
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351 | TCcond.Parameters.gain = 0.6; |
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352 | TCcond.Parameters.derivTime = 1*'s'; |
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353 | TCcond.Ports.setPoint = ((15+273.15) * 'K' - Tmin)/(Tmax-Tmin); |
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354 | TCcond.Ports.input = Tad; |
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355 | Tad = (col.cond.OutletL.T-Tmin)/(Tmax-Tmin); |
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356 | Qc = Qcmin+(Qcmax-Qcmin)*TCcond.Ports.output; |
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357 | |
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358 | "Pressure Controller" |
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359 | PC.Parameters.tau = 0*'s'; |
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360 | PC.Parameters.tauSet = 0*'s'; |
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361 | PC.Parameters.alpha = 0.3; |
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362 | PC.Parameters.bias = 0; |
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363 | PC.Parameters.gamma = 1; |
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364 | PC.Parameters.beta = 1; |
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365 | PC.Options.action = -1; |
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366 | PC.Options.clip = 1; |
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367 | PC.Options.autoMan = 0; |
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368 | PC.Parameters.intTime = 50*'s'; |
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369 | PC.Parameters.gain = 0.5; |
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370 | PC.Parameters.derivTime = 1*'s'; |
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371 | PC.Ports.setPoint = (2.0*'bar'-Pmin)/(Pmax-Pmin); |
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372 | PC.Ports.input = Pad; |
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373 | Pad = (col.cond.OutletV.P-Pmin)/(Pmax-Pmin); |
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374 | col.cond.OutletV.F = (Fcmin+(Fcmax-Fcmin)*PC.Ports.output); |
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375 | |
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376 | "Ttop Level Controller" |
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377 | LCtop.Parameters.tau = 0*'s'; |
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378 | LCtop.Parameters.tauSet = 0*'s'; |
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379 | LCtop.Parameters.alpha = 0.3; |
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380 | LCtop.Parameters.bias = 0.5; |
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381 | LCtop.Parameters.gamma = 1; |
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382 | LCtop.Parameters.beta = 1; |
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383 | LCtop.Options.action = -1; |
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384 | LCtop.Options.clip = 1; |
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385 | LCtop.Options.autoMan = 0; |
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386 | LCtop.Parameters.intTime = 10*'s'; |
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387 | LCtop.Parameters.gain = 1; |
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388 | LCtop.Parameters.derivTime = 1*'s'; |
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389 | LCtop.Ports.setPoint = (1.0 * 'm' - Hmint)/(Hmaxt-Hmint); |
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390 | LCtop.Ports.input = Had_top; |
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391 | Had_top = (col.cond.Level-Hmint)/(Hmaxt-Hmint); |
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392 | col.sptop.Outlet1.F = Fcmin + (Fcmax-Fcmin) * LCtop.Ports.output; |
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393 | |
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394 | "Tbottom Level Controller" |
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395 | LCbot.Parameters.tau = 0*'s'; |
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396 | LCbot.Parameters.tauSet = 0*'s'; |
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397 | LCbot.Parameters.alpha = 0.3; |
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398 | LCbot.Parameters.bias = 0.5; |
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399 | LCbot.Parameters.gamma = 1; |
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400 | LCbot.Parameters.beta = 1; |
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401 | LCbot.Options.action = -1; |
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402 | LCbot.Options.clip = 1; |
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403 | LCbot.Options.autoMan = 0; |
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404 | LCbot.Parameters.intTime = 100*'s'; |
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405 | LCbot.Parameters.gain = 1; |
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406 | LCbot.Parameters.derivTime = 1*'s'; |
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407 | LCbot.Ports.setPoint = (1.0 * 'm' - Hminb)/(Hmaxb-Hminb); |
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408 | LCbot.Ports.input = Had_bot; |
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409 | Had_bot = (col.reb.Level-Hminb)/(Hmaxb-Hminb); |
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410 | col.reb.OutletL.F = Frmin + (Frmax-Frmin) * LCbot.Ports.output; |
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411 | |
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412 | RR * (col.cond.OutletV.F + col.sptop.Outlet1.F) = col.sptop.Outlet2.F; |
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413 | |
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414 | if time < 1 * 'h' then |
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415 | col.sptop.Outlet2.F = 70 * 'kmol/h'; # reflux |
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416 | else |
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417 | col.sptop.Outlet2.F = 85 * 'kmol/h'; # reflux |
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418 | end |
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419 | |
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420 | SPECIFY |
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421 | feed.Outlet.F = 113.4 * 'kmol/h'; |
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422 | feed.Outlet.T = 291 * 'K'; |
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423 | feed.Outlet.P = 168.3 * 'kPa'; |
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424 | feed.Outlet.z = 1/NComp; |
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425 | |
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426 | zero.F = 0 * 'kmol/h'; |
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427 | zero.T = 300 * 'K'; |
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428 | zero.P = 1 * 'atm'; |
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429 | zero.z = 1/NComp; |
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430 | zero.v = 0; |
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431 | zero.h = 0 * 'J/mol'; |
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432 | |
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433 | Qr = 3e6 * 'kJ/h'; |
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434 | col.pump1.dP = 16 * 'kPa'; |
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435 | col.trays.Emv = 1; |
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436 | |
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437 | SET |
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438 | col.NTrays = 8; |
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439 | col.cond.V = 2 * 'm^3'; |
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440 | col.cond.Across = 1 * 'm^2'; |
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441 | col.trays.V = 4 * 'ft^3'; |
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442 | col.trays.Ah = 0.394 * 'ft^2'; |
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443 | col.trays.lw = 20.94 * 'in'; |
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444 | col.trays.hw = 0.125 * 'ft'; |
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445 | col.trays.Q = 0 * 'kW'; |
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446 | col.trays.beta = 0.6; |
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447 | col.trays.alfa = 4; |
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448 | col.trays.Ap = 3.94 * 'ft^2'; |
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449 | col.reb.V = 2 * 'm^3'; |
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450 | col.reb.Across = 1 * 'm^2'; |
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451 | |
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452 | Qrmax = 5e6 * 'kJ/h'; |
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453 | Qrmin = 1e6 * 'kJ/h'; |
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454 | Frmin = 0 * 'kmol/h'; |
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455 | Frmax = 60 * 'kmol/h'; |
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456 | Fcmin = 0 * 'kmol/h'; |
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457 | Fcmax = 120 * 'kmol/h'; |
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458 | Hmint = 0 * 'm'; |
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459 | Hmaxt = 2 * 'm'; |
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460 | Hminb = 0 * 'm'; |
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461 | Hmaxb = 2 * 'm'; |
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462 | Pmin = 0.5 * 'bar'; |
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463 | Pmax = 4 * 'bar'; |
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464 | Qcmax = -5e5 * 'kJ/h'; |
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465 | Qcmin = -5e6 * 'kJ/h'; |
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466 | Tmax = (30+273.15) * 'K'; |
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467 | Tmin = (-20+273.15) * 'K'; |
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468 | |
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469 | INITIAL |
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470 | # condenser |
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471 | col.cond.OutletL.T = 260 *'K'; |
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472 | col.cond.Level = 1 * 'm'; |
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473 | col.cond.OutletL.z([1:4]) = [0.2, 0.2, 0.4, 0.05]; |
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474 | |
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475 | # reboiler |
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476 | col.reb.OutletL.T = 350 *'K'; |
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477 | col.reb.Level = 1 * 'm'; |
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478 | col.reb.OutletL.z([1:4]) = [0.1, 0.4, 0.1, 0.3]; |
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479 | |
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480 | # column trays |
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481 | col.trays.OutletL.T = [290:(330-290)/(col.NTrays-1):330] * 'K'; |
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482 | col.trays.Level = 1.2 * col.trays.hw; |
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483 | col.trays.OutletL.z([1:4]) = [0.15, 0.3, 0.25, 0.2]; |
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484 | |
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485 | OPTIONS |
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486 | RelativeAccuracy = 1e-3; |
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487 | TimeStep = 0.01; |
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488 | TimeEnd = 2; |
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489 | TimeUnit = 'h'; |
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490 | #InitialFile = "Column_ctrl.rlt"; |
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491 | #GuessFile = "Column_ctrl.rlt"; |
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492 | #Dynamic = false; |
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493 | end |
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494 | |
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