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 112 2007-01-15 01:01:46Z 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 CalcObject(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 stream_therm; |
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46 | reb as stream_therm; |
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47 | cond as stream_therm; |
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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 | feed.v = 0; |
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62 | |
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63 | zero.F = 0 * "kmol/h"; |
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64 | zero.T = 300 * "K"; |
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65 | zero.P = 1 * "atm"; |
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66 | zero.z = [0.5, 0.5]; |
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67 | zero.v = 0; |
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68 | zero.h = 0 * "J/mol"; |
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69 | |
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70 | cond.F = 68 * "kmol/h"; |
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71 | cond.P = 150 * "kPa"; |
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72 | cond.T = 281.75 * "K"; |
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73 | cond.v = 0.0; |
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74 | cond.z = [0.6664, 0.3336]; |
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75 | |
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76 | reb.F = 153 * "kmol/h"; |
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77 | reb.P = 185 * "kPa"; |
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78 | reb.T = 328.12 * "K"; |
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79 | reb.z = [0.001848, 0.9982]; |
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80 | reb.v = 1.0; |
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81 | |
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82 | sec.trays.Emv = 1; |
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83 | |
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84 | SET |
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85 | sec.NTrays = 2; |
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86 | #COLUMN |
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87 | sec.trays.V = 4 * "ft^3"; |
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88 | sec.trays.Ah = 0.394 * "ft^2"; |
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89 | sec.trays.lw = 20.94 * "in"; |
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90 | sec.trays.hw = 0.125 * "ft"; |
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91 | sec.trays.Q = 0 * "kW"; |
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92 | sec.trays.beta = 0.6; |
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93 | sec.trays.alfa = 4; |
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94 | sec.trays.Ap = 3.94 * "ft^2"; |
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95 | |
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96 | INITIAL |
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97 | sec.trays.OutletL.T = 290 *"K"; |
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98 | sec.trays.Level = 0.9 * sec.trays.hw; |
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99 | sec.trays.OutletL.z(1) = 0.5; |
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100 | |
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101 | OPTIONS |
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102 | #relativeAccuracy = 1e-3; |
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103 | NLASolver = "sundials"; |
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104 | time = [0:10:1000]; |
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105 | |
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106 | # After running few seconds of transient the steady-state |
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107 | # can be obtained by using the results from that transient: |
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108 | |
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109 | #guessFile="SectionColumn_Test_with2tray.rlt"; |
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110 | #mode = "steady"; |
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111 | end |
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112 | |
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113 | # column section with 8 trays |
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114 | FlowSheet SectionColumn_Test_with8tray |
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115 | PARAMETERS |
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116 | PP as CalcObject(Brief="Physical Properties",File="vrpp"); |
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117 | NComp as Integer; |
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118 | |
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119 | SET |
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120 | PP.Components = [ "isobutane", "benzene"]; |
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121 | PP.LiquidModel = "PR"; |
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122 | PP.VapourModel = "PR"; |
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123 | PP.Derivatives = 0; |
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124 | NComp = PP.NumberOfComponents; |
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125 | |
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126 | DEVICES |
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127 | sec as Section_Column; |
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128 | feed as stream_therm; |
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129 | reb as stream_therm; |
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130 | cond as stream_therm; |
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131 | zero as stream; |
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132 | |
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133 | CONNECTIONS |
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134 | feed to sec.trays(5).Inlet; |
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135 | |
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136 | zero to sec.trays([1:4]).Inlet; |
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137 | zero to sec.trays([6:8]).Inlet; |
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138 | |
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139 | reb to sec.trays(8).InletV; |
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140 | cond to sec.trays(1).InletL; |
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141 | |
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142 | SPECIFY |
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143 | feed.F = 113.4 * "kmol/h"; |
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144 | feed.T = 291 * "K"; |
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145 | feed.P = 168.3 * "kPa"; |
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146 | feed.z = [0.5, 0.5]; |
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147 | feed.v = 0; |
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148 | |
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149 | zero.F = 0 * "kmol/h"; |
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150 | zero.T = 300 * "K"; |
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151 | zero.P = 1 * "atm"; |
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152 | zero.z = [0.5, 0.5]; |
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153 | zero.v = 0; |
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154 | zero.h = 0 * "J/mol"; |
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155 | |
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156 | cond.F = 68 * "kmol/h"; |
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157 | cond.P = 150 * "kPa"; |
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158 | cond.T = 281.75 * "K"; |
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159 | cond.v = 0.0; |
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160 | cond.z = [0.6664, 0.3336]; |
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161 | |
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162 | reb.F = 153 * "kmol/h"; |
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163 | reb.P = 185 * "kPa"; |
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164 | reb.T = 328.12 * "K"; |
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165 | reb.z = [0.001848, 0.9982]; |
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166 | reb.v = 1.0; |
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167 | |
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168 | sec.trays.Emv = 1; |
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169 | |
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170 | SET |
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171 | sec.NTrays = 8; |
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172 | #COLUMN |
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173 | sec.trays.V = 4 * "ft^3"; |
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174 | sec.trays.Ah = 0.394 * "ft^2"; |
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175 | sec.trays.lw = 20.94 * "in"; |
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176 | sec.trays.hw = 0.125 * "ft"; |
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177 | sec.trays.Q = 0 * "kW"; |
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178 | sec.trays.beta = 0.6; |
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179 | sec.trays.alfa = 4; |
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180 | sec.trays.Ap = 3.94 * "ft^2"; |
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181 | |
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182 | INITIAL |
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183 | sec.trays.OutletL.T = [290:(330-290)/(sec.NTrays-1):330] *"K"; |
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184 | sec.trays.Level = 0.3 * sec.trays.hw; |
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185 | sec.trays.OutletL.z(1) = 0.5; |
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186 | |
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187 | OPTIONS |
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188 | relativeAccuracy = 1e-5; |
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189 | time = [0:1:100]; |
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190 | #guessFile="SectionColumn_Test_with8tray.rlt"; |
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191 | #mode = "steady"; |
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192 | end |
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193 | |
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194 | |
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195 | FlowSheet Distillation_kettle_cond_Test |
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196 | PARAMETERS |
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197 | PP as CalcObject(Brief="Physical Properties",File="vrpp"); |
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198 | NComp as Integer; |
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199 | |
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200 | VARIABLES |
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201 | Qc as heat_rate (Brief="Heat rate removed from condenser"); |
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202 | Qr as heat_rate (Brief="Heat rate supplied to reboiler"); |
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203 | |
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204 | SET |
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205 | PP.Components = [ "isobutane", "n-pentane", "propylene", |
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206 | "benzene", "isobutene" ]; |
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207 | PP.LiquidModel = "PR"; |
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208 | PP.VapourModel = "PR"; |
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209 | PP.Derivatives = 1; |
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210 | NComp = PP.NumberOfComponents; |
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211 | |
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212 | DEVICES |
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213 | col as Distillation_kettle_cond; |
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214 | feed as streamTP; |
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215 | zero as stream; |
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216 | |
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217 | CONNECTIONS |
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218 | feed to col.trays(5).Inlet; |
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219 | zero to col.reb.Inlet; |
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220 | zero to col.trays([1:4]).Inlet; |
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221 | zero to col.trays([6:col.NTrays]).Inlet; |
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222 | Qc to col.cond.Q; |
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223 | Qr to col.reb.Q; |
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224 | |
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225 | SPECIFY |
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226 | feed.F = 113.4 * "kmol/h"; |
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227 | feed.T = 291 * "K"; |
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228 | feed.P = 168.3 * "kPa"; |
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229 | feed.z = 1/NComp; |
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230 | |
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231 | zero.F = 0 * "kmol/h"; |
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232 | zero.T = 300 * "K"; |
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233 | zero.P = 1 * "atm"; |
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234 | zero.z = 1/NComp; |
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235 | zero.v = 0; |
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236 | zero.h = 0 * "J/mol"; |
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237 | |
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238 | col.sptop.Outlet2.F = 85 * "kmol/h"; |
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239 | col.reb.OutletL.F = 28.4 * "kmol/h"; |
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240 | col.sptop.frac = 0.444445; |
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241 | col.cond.OutletV.F = 0 * "kmol/h"; |
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242 | Qr = 3.7743e6 * "kJ/h"; |
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243 | Qc = -3.71e6 * "kJ/h"; |
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244 | col.pump1.dP = 16 * "kPa"; |
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245 | col.trays.Emv = 1; |
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246 | |
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247 | SET |
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248 | col.NTrays = 8; |
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249 | col.cond.V = 2 * "m^3"; |
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250 | col.cond.Across = 1 * "m^2"; |
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251 | col.trays.V = 4 * "ft^3"; |
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252 | col.trays.Ah = 0.394 * "ft^2"; |
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253 | col.trays.lw = 20.94 * "in"; |
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254 | col.trays.hw = 0.125 * "ft"; |
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255 | col.trays.Q = 0 * "kW"; |
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256 | col.trays.beta = 0.6; |
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257 | col.trays.alfa = 4; |
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258 | col.trays.Ap = 3.94 * "ft^2"; |
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259 | col.reb.V = 2 * "m^3"; |
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260 | col.reb.Across = 1 * "m^2"; |
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261 | |
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262 | INITIAL |
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263 | # condenser |
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264 | col.cond.OutletL.T = 260 *"K"; |
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265 | col.cond.Level = 1 * "m"; |
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266 | col.cond.OutletL.z([1:4]) = [0.65, 0.05, 0.01, 0.01]; |
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267 | |
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268 | # reboiler |
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269 | col.reb.OutletL.T = 330 *"K"; |
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270 | col.reb.Level = 1 * "m"; |
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271 | col.reb.OutletL.z([1:4]) = [0.1, 0.7, 0.01, 0.01]; |
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272 | |
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273 | # column trays |
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274 | col.trays.OutletL.T = [290:(330-290)/(col.NTrays-1):330] * "K"; |
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275 | col.trays.Level = 1.2 * col.trays.hw; |
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276 | col.trays.OutletL.z([1:4]) = [0.5, 0.05, 0.01, 0.01]; |
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277 | |
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278 | OPTIONS |
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279 | relativeAccuracy = 1e-3; |
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280 | time = [0:0.01:1, 2:50]; |
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281 | #guessFile="Distillation_kettle_cond_Test.rlt"; |
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282 | #mode = "steady"; |
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283 | end |
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284 | |
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285 | FlowSheet Column_ctrl |
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286 | PARAMETERS |
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287 | PP as CalcObject(Brief="Physical Properties",File="vrpp"); |
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288 | NComp as Integer; |
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289 | |
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290 | Qcmin as heat_rate (Brief="Minimum Condenser Heat supplied"); |
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291 | Qcmax as heat_rate (Brief="Maximum Condenser Heat supplied"); |
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292 | Qrmin as heat_rate (Brief="Minimum Reboiler Heat supplied"); |
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293 | Qrmax as heat_rate (Brief="Maximum Reboiler Heat supplied"); |
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294 | Frmin as flow_mol (Brief="Minimum bottom flow rate"); |
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295 | Frmax as flow_mol (Brief="Maximum bottom flow rate"); |
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296 | Fcmin as flow_mol (Brief="Minimum reflux flow rate"); |
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297 | Fcmax as flow_mol (Brief="Maximum reflux flow rate"); |
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298 | Hmint as length (Brief="Minimum liquid level in top tank"); |
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299 | Hmaxt as length (Brief="Maximum liquid level in top tank"); |
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300 | Hminb as length (Brief="Minimum liquid level in reboiler"); |
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301 | Hmaxb as length (Brief="Maximum liquid level in reboiler"); |
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302 | Pmax as pressure (Brief="Maximum column pressure"); |
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303 | Pmin as pressure (Brief="Minimum column pressure"); |
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304 | Tmax as temperature (Brief="Maximum column temperature"); |
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305 | Tmin as temperature (Brief="Minimum column temperature"); |
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306 | |
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307 | VARIABLES |
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308 | Qc as heat_rate (Brief="Heat rate removed from condenser"); |
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309 | Qr as heat_rate (Brief="Heat rate supplied to reboiler"); |
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310 | Had_top as Real (Brief="Dimensionless condenser level"); |
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311 | Had_bot as Real (Brief="Dimensionless reboiler level"); |
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312 | Pad as Real (Brief="Dimensionless pressure"); |
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313 | Tad as Real (Brief="Dimensionless temperature"); |
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314 | RR as positive (Brief="Reflux ratio"); |
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315 | |
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316 | SET |
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317 | PP.Components = [ "isobutane", "n-pentane", "propylene", |
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318 | "benzene", "isobutene" ]; |
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319 | PP.LiquidModel = "PR"; |
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320 | PP.VapourModel = "PR"; |
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321 | PP.Derivatives = 1; |
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322 | NComp = PP.NumberOfComponents; |
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323 | |
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324 | DEVICES |
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325 | col as Distillation_kettle_cond; |
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326 | feed as streamTP; |
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327 | zero as stream; |
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328 | TCcond as PIDIncr_Ideal_AW; |
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329 | LCtop as PIDIncr_Ideal_AW; |
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330 | LCbot as PIDIncr_Ideal_AW; |
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331 | PC as PIDIncr_Ideal_AW; |
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332 | |
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333 | CONNECTIONS |
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334 | feed to col.trays(5).Inlet; |
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335 | zero to col.reb.Inlet; |
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336 | zero to col.trays([1:4]).Inlet; |
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337 | zero to col.trays([6:col.NTrays]).Inlet; |
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338 | Qc to col.cond.Q; |
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339 | Qr to col.reb.Q; |
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340 | |
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341 | EQUATIONS |
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342 | "Temperature Controller" |
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343 | TCcond.Parameters.tau = 0*"s"; |
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344 | TCcond.Parameters.tauSet = 0*"s"; |
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345 | TCcond.Parameters.alpha = 0.3; |
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346 | TCcond.Parameters.bias = 0.5; |
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347 | TCcond.Parameters.gamma = 1; |
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348 | TCcond.Parameters.beta = 1; |
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349 | TCcond.Options.action = 1; |
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350 | TCcond.Options.clip = 1; |
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351 | TCcond.Options.autoMan = 0; |
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352 | TCcond.Parameters.intTime = 60*"s"; |
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353 | TCcond.Parameters.gain = 0.6; |
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354 | TCcond.Parameters.derivTime = 1*"s"; |
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355 | TCcond.Ports.setPoint = ((15+273.15) * "K" - Tmin)/(Tmax-Tmin); |
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356 | TCcond.Ports.input = Tad; |
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357 | Tad = (col.cond.OutletL.T-Tmin)/(Tmax-Tmin); |
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358 | Qc = Qcmin+(Qcmax-Qcmin)*TCcond.Ports.output; |
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359 | |
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360 | "Pressure Controller" |
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361 | PC.Parameters.tau = 0*"s"; |
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362 | PC.Parameters.tauSet = 0*"s"; |
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363 | PC.Parameters.alpha = 0.3; |
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364 | PC.Parameters.bias = 0; |
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365 | PC.Parameters.gamma = 1; |
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366 | PC.Parameters.beta = 1; |
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367 | PC.Options.action = -1; |
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368 | PC.Options.clip = 1; |
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369 | PC.Options.autoMan = 0; |
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370 | PC.Parameters.intTime = 50*"s"; |
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371 | PC.Parameters.gain = 0.5; |
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372 | PC.Parameters.derivTime = 1*"s"; |
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373 | PC.Ports.setPoint = (2.0*"bar"-Pmin)/(Pmax-Pmin); |
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374 | PC.Ports.input = Pad; |
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375 | Pad = (col.cond.OutletV.P-Pmin)/(Pmax-Pmin); |
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376 | col.cond.OutletV.F = (Fcmin+(Fcmax-Fcmin)*PC.Ports.output); |
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377 | |
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378 | "Ttop Level Controller" |
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379 | LCtop.Parameters.tau = 0*"s"; |
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380 | LCtop.Parameters.tauSet = 0*"s"; |
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381 | LCtop.Parameters.alpha = 0.3; |
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382 | LCtop.Parameters.bias = 0.5; |
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383 | LCtop.Parameters.gamma = 1; |
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384 | LCtop.Parameters.beta = 1; |
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385 | LCtop.Options.action = -1; |
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386 | LCtop.Options.clip = 1; |
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387 | LCtop.Options.autoMan = 0; |
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388 | LCtop.Parameters.intTime = 10*"s"; |
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389 | LCtop.Parameters.gain = 1; |
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390 | LCtop.Parameters.derivTime = 1*"s"; |
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391 | LCtop.Ports.setPoint = (1.0 * "m" - Hmint)/(Hmaxt-Hmint); |
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392 | LCtop.Ports.input = Had_top; |
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393 | Had_top = (col.cond.Level-Hmint)/(Hmaxt-Hmint); |
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394 | col.sptop.Outlet1.F = Fcmin + (Fcmax-Fcmin) * LCtop.Ports.output; |
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395 | |
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396 | "Tbottom Level Controller" |
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397 | LCbot.Parameters.tau = 0*"s"; |
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398 | LCbot.Parameters.tauSet = 0*"s"; |
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399 | LCbot.Parameters.alpha = 0.3; |
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400 | LCbot.Parameters.bias = 0.5; |
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401 | LCbot.Parameters.gamma = 1; |
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402 | LCbot.Parameters.beta = 1; |
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403 | LCbot.Options.action = -1; |
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404 | LCbot.Options.clip = 1; |
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405 | LCbot.Options.autoMan = 0; |
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406 | LCbot.Parameters.intTime = 100*"s"; |
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407 | LCbot.Parameters.gain = 1; |
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408 | LCbot.Parameters.derivTime = 1*"s"; |
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409 | LCbot.Ports.setPoint = (1.0 * "m" - Hminb)/(Hmaxb-Hminb); |
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410 | LCbot.Ports.input = Had_bot; |
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411 | Had_bot = (col.reb.Level-Hminb)/(Hmaxb-Hminb); |
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412 | col.reb.OutletL.F = Frmin + (Frmax-Frmin) * LCbot.Ports.output; |
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413 | |
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414 | RR * (col.cond.OutletV.F + col.sptop.Outlet1.F) = col.sptop.Outlet2.F; |
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415 | |
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416 | if time < 1 * "h" then |
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417 | col.sptop.Outlet2.F = 70 * "kmol/h"; # reflux |
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418 | else |
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419 | col.sptop.Outlet2.F = 85 * "kmol/h"; # reflux |
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420 | end |
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421 | |
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422 | SPECIFY |
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423 | feed.F = 113.4 * "kmol/h"; |
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424 | feed.T = 291 * "K"; |
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425 | feed.P = 168.3 * "kPa"; |
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426 | feed.z = 1/NComp; |
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427 | |
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428 | zero.F = 0 * "kmol/h"; |
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429 | zero.T = 300 * "K"; |
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430 | zero.P = 1 * "atm"; |
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431 | zero.z = 1/NComp; |
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432 | zero.v = 0; |
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433 | zero.h = 0 * "J/mol"; |
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434 | |
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435 | Qr = 3e6 * "kJ/h"; |
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436 | col.pump1.dP = 16 * "kPa"; |
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437 | col.trays.Emv = 1; |
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438 | |
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439 | SET |
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440 | col.NTrays = 8; |
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441 | col.cond.V = 2 * "m^3"; |
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442 | col.cond.Across = 1 * "m^2"; |
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443 | col.trays.V = 4 * "ft^3"; |
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444 | col.trays.Ah = 0.394 * "ft^2"; |
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445 | col.trays.lw = 20.94 * "in"; |
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446 | col.trays.hw = 0.125 * "ft"; |
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447 | col.trays.Q = 0 * "kW"; |
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448 | col.trays.beta = 0.6; |
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449 | col.trays.alfa = 4; |
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450 | col.trays.Ap = 3.94 * "ft^2"; |
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451 | col.reb.V = 2 * "m^3"; |
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452 | col.reb.Across = 1 * "m^2"; |
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453 | |
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454 | Qrmax = 5e6 * "kJ/h"; |
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455 | Qrmin = 1e6 * "kJ/h"; |
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456 | Frmin = 0 * "kmol/h"; |
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457 | Frmax = 60 * "kmol/h"; |
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458 | Fcmin = 0 * "kmol/h"; |
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459 | Fcmax = 120 * "kmol/h"; |
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460 | Hmint = 0 * "m"; |
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461 | Hmaxt = 2 * "m"; |
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462 | Hminb = 0 * "m"; |
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463 | Hmaxb = 2 * "m"; |
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464 | Pmin = 0.5 * "bar"; |
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465 | Pmax = 4 * "bar"; |
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466 | Qcmax = -5e5 * "kJ/h"; |
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467 | Qcmin = -5e6 * "kJ/h"; |
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468 | Tmax = (30+273.15) * "K"; |
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469 | Tmin = (-20+273.15) * "K"; |
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470 | |
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471 | INITIAL |
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472 | # condenser |
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473 | col.cond.OutletL.T = 260 *"K"; |
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474 | col.cond.Level = 1 * "m"; |
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475 | col.cond.OutletL.z([1:4]) = [0.2, 0.2, 0.4, 0.05]; |
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476 | |
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477 | # reboiler |
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478 | col.reb.OutletL.T = 350 *"K"; |
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479 | col.reb.Level = 1 * "m"; |
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480 | col.reb.OutletL.z([1:4]) = [0.1, 0.4, 0.1, 0.3]; |
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481 | |
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482 | # column trays |
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483 | col.trays.OutletL.T = [290:(330-290)/(col.NTrays-1):330] * "K"; |
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484 | col.trays.Level = 1.2 * col.trays.hw; |
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485 | col.trays.OutletL.z([1:4]) = [0.15, 0.3, 0.25, 0.2]; |
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486 | |
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487 | OPTIONS |
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488 | relativeAccuracy = 1e-3; |
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489 | time = [0:0.01:0.1, 0.11:0.01:2]*"h"; |
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490 | #initialFile = "Column_ctrl.rlt"; |
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491 | #guessFile = "Column_ctrl.rlt"; |
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492 | #mode = "steady"; |
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493 | end |
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494 | |
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