1 | #*---------------------------------------------------------------------- |
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2 | * File containg models of columns: distillation, stripping, absorbers |
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3 | * rectifier, .... |
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4 | * |
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5 | * The default nomenclature is: |
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6 | * Type_Column_reboilertype_condensertyper |
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7 | * |
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8 | * where: |
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9 | * Type = refluxed or reboiled or section |
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10 | * Column = Stripping, Absorption, Rectifier, Distillation |
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11 | * Reboiler type (if exists) = kettle or thermosyphon |
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12 | * Condenser type (if exists) = with subccoling or without subcooling |
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13 | * |
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14 | *----------------------------------------------------------------------- |
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15 | * Author: Paula B. Staudt |
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16 | * $Id: column.mso 1 2006-06-20 17:33:53Z rafael $ |
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17 | *---------------------------------------------------------------------*# |
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18 | |
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19 | using "tray"; |
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20 | using "reboiler"; |
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21 | using "condenser"; |
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22 | using "mixers_splitters/splitter"; |
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23 | using "tank"; |
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24 | using "pressure_changers/pump"; |
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25 | |
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26 | #*---------------------------------------------------------------------- |
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27 | * Model of a column section with: |
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28 | * - NTrays=number of trays trays. |
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29 | * |
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30 | *---------------------------------------------------------------------*# |
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31 | Model Section_Column |
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32 | PARAMETERS |
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33 | ext PP as CalcObject; |
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34 | ext NComp as Integer; |
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35 | NTrays as Integer(Brief="Number of trays", Default=2); |
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36 | |
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37 | VARIABLES |
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38 | trays(NTrays) as tray; |
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39 | |
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40 | EQUATIONS |
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41 | "Pressure Drop through the tray" |
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42 | trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * |
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43 | trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P - |
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44 | trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV)); |
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45 | |
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46 | CONNECTIONS |
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47 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
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48 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
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49 | end |
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50 | |
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51 | |
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52 | #*---------------------------------------------------------------------- |
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53 | * Model of a distillation column containing: |
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54 | * - NTrays like tray; |
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55 | * - a kettle reboiler; |
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56 | * - dymamic condenser; |
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57 | * - a splitter which separate reflux and distillate; |
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58 | * - a pump in reflux stream; |
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59 | *---------------------------------------------------------------------*# |
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60 | Model Distillation_kettle_cond |
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61 | PARAMETERS |
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62 | ext PP as CalcObject; |
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63 | ext NComp as Integer; |
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64 | NTrays as Integer(Brief="Number of trays", Default=2); |
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65 | |
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66 | VARIABLES |
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67 | trays(NTrays) as tray; |
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68 | cond as condenser; |
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69 | reb as reboiler; |
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70 | sp as splitter; |
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71 | pump1 as pump; |
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72 | |
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73 | EQUATIONS |
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74 | if (reb.OutletV.P > reb.InletL.P) then |
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75 | "Pressure Drop through the tray" |
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76 | reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P) |
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77 | / (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3 |
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78 | else |
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79 | "Prato selado" |
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80 | reb.OutletV.F = 0.0 * "mol/s"; |
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81 | end |
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82 | |
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83 | "Pressure Drop through the tray" |
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84 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * |
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85 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
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86 | cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
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87 | |
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88 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
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89 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
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90 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
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91 | |
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92 | CONNECTIONS |
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93 | #vapor |
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94 | reb.OutletV to trays([NTrays]).InletV; |
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95 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
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96 | trays(1).OutletV to cond.InletV; |
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97 | |
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98 | #liquid |
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99 | cond.OutletL to sp.Inlet; |
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100 | sp.Outlet2 to pump1.Inlet; |
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101 | pump1.Outlet to trays(1).InletL; |
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102 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
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103 | trays(NTrays).OutletL to reb.InletL; |
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104 | end |
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105 | |
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106 | |
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107 | #* ------------------------------------------------------------------- |
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108 | * Distillation Column model with: |
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109 | * |
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110 | * - NTrays like tray; |
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111 | * - a vessel in the bottom of column; |
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112 | * - a splitter who separate the bottom product and the stream to reboiler; |
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113 | * - steady state reboiler (thermosyphon); |
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114 | * - a steady state condenser with subcooling; |
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115 | * - a vessel drum (layed cilinder); |
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116 | * - a splitter which separate reflux and distillate; |
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117 | * - a pump in reflux stream. |
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118 | * |
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119 | * ------------------------------------------------------------------*# |
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120 | Model Distillation_thermosyphon_subcooling |
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121 | PARAMETERS |
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122 | ext PP as CalcObject; |
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123 | ext NComp as Integer; |
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124 | NTrays as Integer(Brief="Number of trays", Default=2); |
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125 | |
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126 | VARIABLES |
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127 | trays(NTrays) as tray; |
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128 | cond as condenserSteady; |
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129 | reb as reboilerSteady; |
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130 | tbottom as tank; |
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131 | ttop as tank_cylindrical; |
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132 | spbottom as splitter; |
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133 | sptop as splitter; |
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134 | pump1 as pump; |
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135 | |
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136 | EQUATIONS |
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137 | if (reb.OutletV.P > reb.InletL.P) then |
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138 | "Pressure Drop through the tray" |
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139 | reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P) |
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140 | / (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3 |
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141 | else |
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142 | "Prato selado" |
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143 | reb.OutletV.F = 0.0 * "mol/s"; |
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144 | end |
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145 | |
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146 | "Pressure Drop through the tray" |
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147 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * |
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148 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
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149 | ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
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150 | |
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151 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
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152 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
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153 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
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154 | |
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155 | CONNECTIONS |
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156 | #vapor |
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157 | reb.OutletV to trays(NTrays).InletV; |
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158 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
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159 | trays(1).OutletV to cond.InletV; |
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160 | |
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161 | #liquid |
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162 | cond.OutletL to ttop.Inlet; |
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163 | ttop.Outlet to sptop.Inlet; |
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164 | sptop.Outlet2 to pump1.Inlet; |
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165 | pump1.Outlet to trays(1).InletL; |
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166 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
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167 | trays(NTrays).OutletL to tbottom.Inlet; |
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168 | tbottom.Outlet to spbottom.Inlet; |
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169 | spbottom.Outlet2 to reb.InletL; |
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170 | end |
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171 | |
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172 | |
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173 | #* ------------------------------------------------------------------- |
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174 | * Distillation Column model with: |
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175 | * |
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176 | * - NTrays like tray; |
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177 | * - a vessel in the bottom of column; |
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178 | * - a splitter who separate the bottom product and the stream to reboiler; |
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179 | * - steady state reboiler (thermosyphon); |
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180 | * - a dynamic condenser without subcooling; |
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181 | * - a splitter which separate reflux and distillate; |
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182 | * - a pump in reflux stream. |
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183 | * |
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184 | * ------------------------------------------------------------------*# |
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185 | Model Distillation_thermosyphon_cond |
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186 | PARAMETERS |
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187 | ext PP as CalcObject; |
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188 | ext NComp as Integer; |
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189 | NTrays as Integer(Brief="Number of trays", Default=2); |
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190 | |
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191 | VARIABLES |
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192 | trays(NTrays) as tray; |
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193 | cond as condenser; |
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194 | reb as reboilerSteady; |
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195 | tbottom as tank; |
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196 | spbottom as splitter; |
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197 | sptop as splitter; |
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198 | pump1 as pump; |
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199 | |
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200 | EQUATIONS |
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201 | if (reb.OutletV.P > reb.InletL.P) then |
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202 | "Pressure Drop through the tray" |
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203 | reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P) |
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204 | / (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3 |
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205 | else |
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206 | "Prato selado" |
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207 | reb.OutletV.F = 0.0 * "mol/s"; |
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208 | end |
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209 | |
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210 | "Pressure Drop through the tray" |
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211 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * |
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212 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
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213 | cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
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214 | |
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215 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
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216 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
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217 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
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218 | |
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219 | CONNECTIONS |
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220 | #vapor |
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221 | reb.OutletV to trays(NTrays).InletV; |
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222 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
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223 | trays(1).OutletV to cond.InletV; |
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224 | |
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225 | #liquid |
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226 | cond.OutletL to sptop.Inlet; |
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227 | sptop.Outlet2 to pump1.Inlet; |
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228 | pump1.Outlet to trays(1).InletL; |
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229 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
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230 | trays(NTrays).OutletL to tbottom.Inlet; |
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231 | tbottom.Outlet to spbottom.Inlet; |
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232 | spbottom.Outlet2 to reb.InletL; |
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233 | end |
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234 | |
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235 | |
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236 | #* ------------------------------------------------------------------- |
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237 | * Distillation Column model with: |
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238 | * |
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239 | * - NTrays like tray; |
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240 | * - a kettle reboiler; |
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241 | * - a steady state condenser with subcooling; |
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242 | * - a vessel drum (layed cilinder); |
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243 | * - a splitter which separate reflux and distillate; |
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244 | * - a pump in reflux stream. |
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245 | * |
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246 | * ------------------------------------------------------------------*# |
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247 | Model Distillation_kettle_subcooling |
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248 | PARAMETERS |
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249 | ext PP as CalcObject; |
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250 | ext NComp as Integer; |
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251 | NTrays as Integer(Brief="Number of trays", Default=2); |
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252 | |
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253 | VARIABLES |
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254 | trays(NTrays) as tray; |
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255 | cond as condenserSteady; |
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256 | reb as reboiler; |
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257 | ttop as tank_cylindrical; |
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258 | sptop as splitter; |
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259 | pump1 as pump; |
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260 | |
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261 | EQUATIONS |
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262 | if (reb.OutletV.P > reb.InletL.P) then |
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263 | "Pressure Drop through the tray" |
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264 | reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P) |
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265 | / (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3 |
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266 | else |
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267 | "Prato selado" |
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268 | reb.OutletV.F = 0.0 * "mol/s"; |
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269 | end |
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270 | |
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271 | "Pressure Drop through the tray" |
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272 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * |
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273 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
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274 | ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
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275 | |
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276 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
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277 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
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278 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
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279 | |
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280 | CONNECTIONS |
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281 | #vapor |
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282 | reb.OutletV to trays(NTrays).InletV; |
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283 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
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284 | trays(1).OutletV to cond.InletV; |
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285 | |
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286 | #liquid |
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287 | cond.OutletL to ttop.Inlet; |
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288 | ttop.Outlet to sptop.Inlet; |
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289 | sptop.Outlet2 to pump1.Inlet; |
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290 | pump1.Outlet to trays(1).InletL; |
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291 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
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292 | trays(NTrays).OutletL to reb.InletL; |
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293 | end |
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294 | |
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295 | |
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296 | #*---------------------------------------------------------------------- |
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297 | * Model of a rectifier containing: |
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298 | * - NTrays like tray; |
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299 | * - dymamic condenser without subcooling; |
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300 | * - a splitter which separate reflux and distillate; |
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301 | * - a pump in reflux stream; |
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302 | *---------------------------------------------------------------------*# |
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303 | Model Rectifier |
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304 | PARAMETERS |
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305 | ext PP as CalcObject; |
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306 | ext NComp as Integer; |
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307 | NTrays as Integer(Brief="Number of trays", Default=2); |
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308 | |
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309 | VARIABLES |
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310 | trays(NTrays) as tray; |
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311 | cond as condenser; |
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312 | sp as splitter; |
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313 | pump1 as pump; |
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314 | |
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315 | EQUATIONS |
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316 | "Pressure Drop through the tray" |
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317 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * |
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318 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
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319 | cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
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320 | |
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321 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
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322 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
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323 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
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324 | |
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325 | CONNECTIONS |
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326 | #vapor |
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327 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
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328 | trays(1).OutletV to cond.InletV; |
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329 | |
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330 | #liquid |
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331 | cond.OutletL to sp.Inlet; |
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332 | sp.Outlet2 to pump1.Inlet; |
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333 | pump1.Outlet to trays(1).InletL; |
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334 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
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335 | end |
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336 | |
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337 | |
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338 | #* ------------------------------------------------------------------- |
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339 | * Rectifier Column with: |
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340 | * |
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341 | * - NTrays like tray; |
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342 | * - a steady state condenser with subcooling; |
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343 | * - a vessel drum (layed cilinder); |
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344 | * - a splitter which separate reflux and distillate; |
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345 | * - a pump in reflux stream. |
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346 | * |
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347 | * ------------------------------------------------------------------*# |
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348 | Model Rectifier_subcooling |
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349 | PARAMETERS |
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350 | ext PP as CalcObject; |
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351 | ext NComp as Integer; |
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352 | NTrays as Integer(Brief="Number of trays", Default=2); |
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353 | |
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354 | VARIABLES |
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355 | trays(NTrays) as tray; |
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356 | cond as condenserSteady; |
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357 | ttop as tank_cylindrical; |
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358 | sptop as splitter; |
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359 | pump1 as pump; |
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360 | |
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361 | EQUATIONS |
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362 | "Pressure Drop through the tray" |
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363 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * |
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364 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
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365 | ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
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366 | |
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367 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
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368 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
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369 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
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370 | |
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371 | CONNECTIONS |
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372 | #vapor |
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373 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
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374 | trays(1).OutletV to cond.InletV; |
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375 | |
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376 | #liquid |
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377 | cond.OutletL to ttop.Inlet; |
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378 | ttop.Outlet to sptop.Inlet; |
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379 | sptop.Outlet2 to pump1.Inlet; |
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380 | pump1.Outlet to trays(1).InletL; |
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381 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
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382 | end |
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383 | |
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384 | |
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385 | #*---------------------------------------------------------------------- |
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386 | * Model of a Refluxed Stripping column containing: |
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387 | * - NTrays like tray; |
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388 | * - dymamic condenser without subcooling; |
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389 | * - a splitter which separate reflux and distillate; |
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390 | * - a pump in reflux stream; |
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391 | *---------------------------------------------------------------------*# |
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392 | Model Refluxed_Stripping |
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393 | PARAMETERS |
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394 | ext PP as CalcObject; |
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395 | ext NComp as Integer; |
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396 | NTrays as Integer(Brief="Number of trays", Default=2); |
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397 | |
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398 | VARIABLES |
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399 | trays(NTrays) as tray; |
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400 | cond as condenser; |
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401 | sp as splitter; |
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402 | pump1 as pump; |
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403 | |
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404 | EQUATIONS |
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405 | "Pressure Drop through the tray" |
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406 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * |
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407 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
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408 | cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
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409 | |
---|
410 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
---|
411 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
---|
412 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
---|
413 | |
---|
414 | CONNECTIONS |
---|
415 | #vapor |
---|
416 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
---|
417 | trays(1).OutletV to cond.InletV; |
---|
418 | |
---|
419 | #liquid |
---|
420 | cond.OutletL to sp.Inlet; |
---|
421 | sp.Outlet2 to pump1.Inlet; |
---|
422 | pump1.Outlet to trays(1).InletL; |
---|
423 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
---|
424 | end |
---|
425 | |
---|
426 | |
---|
427 | #* ------------------------------------------------------------------- |
---|
428 | * Refluxed Stripping Column with: |
---|
429 | * |
---|
430 | * - NTrays like tray; |
---|
431 | * - a steady state condenser (with subcooling); |
---|
432 | * - a vessel drum (layed cilinder); |
---|
433 | * - a splitter which separate reflux and distillate; |
---|
434 | * - a pump in reflux stream. |
---|
435 | * |
---|
436 | * ------------------------------------------------------------------*# |
---|
437 | Model Refluxed_Stripping_subcooling |
---|
438 | PARAMETERS |
---|
439 | ext PP as CalcObject; |
---|
440 | ext NComp as Integer; |
---|
441 | NTrays as Integer(Brief="Number of trays", Default=2); |
---|
442 | |
---|
443 | VARIABLES |
---|
444 | trays(NTrays) as tray; |
---|
445 | cond as condenserSteady; |
---|
446 | ttop as tank_cylindrical; |
---|
447 | sptop as splitter; |
---|
448 | pump1 as pump; |
---|
449 | |
---|
450 | EQUATIONS |
---|
451 | "Pressure Drop through the tray" |
---|
452 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * |
---|
453 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
---|
454 | ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
---|
455 | |
---|
456 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
---|
457 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
---|
458 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
---|
459 | |
---|
460 | CONNECTIONS |
---|
461 | #vapor |
---|
462 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
---|
463 | trays(1).OutletV to cond.InletV; |
---|
464 | |
---|
465 | #liquid |
---|
466 | cond.OutletL to ttop.Inlet; |
---|
467 | ttop.Outlet to sptop.Inlet; |
---|
468 | sptop.Outlet2 to pump1.Inlet; |
---|
469 | pump1.Outlet to trays(1).InletL; |
---|
470 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
---|
471 | end |
---|
472 | |
---|
473 | |
---|
474 | #*---------------------------------------------------------------------- |
---|
475 | * Model of a Refluxed Absorption column containing: |
---|
476 | * - NTrays like tray; |
---|
477 | * - dymamic condenser without subcooling; |
---|
478 | * - a splitter which separate reflux and distillate; |
---|
479 | * - a pump in reflux stream; |
---|
480 | *---------------------------------------------------------------------*# |
---|
481 | Model Refluxed_Absorption |
---|
482 | PARAMETERS |
---|
483 | ext PP as CalcObject; |
---|
484 | ext NComp as Integer; |
---|
485 | NTrays as Integer(Brief="Number of trays", Default=2); |
---|
486 | |
---|
487 | VARIABLES |
---|
488 | trays(NTrays) as tray; |
---|
489 | cond as condenser; |
---|
490 | sp as splitter; |
---|
491 | pump1 as pump; |
---|
492 | |
---|
493 | EQUATIONS |
---|
494 | "Pressure Drop through the tray" |
---|
495 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * |
---|
496 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
---|
497 | cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
---|
498 | |
---|
499 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
---|
500 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
---|
501 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
---|
502 | |
---|
503 | CONNECTIONS |
---|
504 | #vapor |
---|
505 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
---|
506 | trays(1).OutletV to cond.InletV; |
---|
507 | |
---|
508 | #liquid |
---|
509 | cond.OutletL to sp.Inlet; |
---|
510 | sp.Outlet2 to pump1.Inlet; |
---|
511 | pump1.Outlet to trays(1).InletL; |
---|
512 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
---|
513 | end |
---|
514 | |
---|
515 | |
---|
516 | #* ------------------------------------------------------------------- |
---|
517 | * Refluxed Absorption Column with: |
---|
518 | * |
---|
519 | * - NTrays like tray; |
---|
520 | * - a steady state condenser (with subcooling); |
---|
521 | * - a vessel drum (layed cilinder); |
---|
522 | * - a splitter which separate reflux and distillate; |
---|
523 | * - a pump in reflux stream. |
---|
524 | * |
---|
525 | * ------------------------------------------------------------------*# |
---|
526 | Model Refluxed_Absorption_subcooling |
---|
527 | PARAMETERS |
---|
528 | ext PP as CalcObject; |
---|
529 | ext NComp as Integer; |
---|
530 | NTrays as Integer(Brief="Number of trays", Default=2); |
---|
531 | |
---|
532 | VARIABLES |
---|
533 | trays(NTrays) as tray; |
---|
534 | cond as condenserSteady; |
---|
535 | ttop as tank_cylindrical; |
---|
536 | sptop as splitter; |
---|
537 | pump1 as pump; |
---|
538 | |
---|
539 | EQUATIONS |
---|
540 | "Pressure Drop through the tray" |
---|
541 | trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * |
---|
542 | trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P - |
---|
543 | ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV)); |
---|
544 | |
---|
545 | trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * |
---|
546 | trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P - |
---|
547 | trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV)); |
---|
548 | |
---|
549 | CONNECTIONS |
---|
550 | #vapor |
---|
551 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
---|
552 | trays(1).OutletV to cond.InletV; |
---|
553 | |
---|
554 | #liquid |
---|
555 | cond.OutletL to ttop.Inlet; |
---|
556 | ttop.Outlet to sptop.Inlet; |
---|
557 | sptop.Outlet2 to pump1.Inlet; |
---|
558 | pump1.Outlet to trays(1).InletL; |
---|
559 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
---|
560 | end |
---|
561 | |
---|
562 | |
---|
563 | #* ------------------------------------------------------------------- |
---|
564 | * Reboiled Stripping Column model with: |
---|
565 | * |
---|
566 | * - NTrays like tray; |
---|
567 | * - a kettle reboiler; |
---|
568 | * |
---|
569 | * ------------------------------------------------------------------*# |
---|
570 | Model Reboiled_Stripping_kettle |
---|
571 | PARAMETERS |
---|
572 | ext PP as CalcObject; |
---|
573 | ext NComp as Integer; |
---|
574 | NTrays as Integer(Brief="Number of trays", Default=2); |
---|
575 | |
---|
576 | VARIABLES |
---|
577 | trays(NTrays) as tray; |
---|
578 | reb as reboiler; |
---|
579 | |
---|
580 | EQUATIONS |
---|
581 | if (reb.OutletV.P > reb.InletL.P) then |
---|
582 | "Pressure Drop through the tray" |
---|
583 | reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P) |
---|
584 | / (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3 |
---|
585 | else |
---|
586 | "Prato selado" |
---|
587 | reb.OutletV.F = 0.0 * "mol/s"; |
---|
588 | end |
---|
589 | |
---|
590 | "Pressure Drop through the tray" |
---|
591 | trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * |
---|
592 | trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P - |
---|
593 | trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV)); |
---|
594 | |
---|
595 | CONNECTIONS |
---|
596 | #vapor |
---|
597 | reb.OutletV to trays(NTrays).InletV; |
---|
598 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
---|
599 | |
---|
600 | #liquid |
---|
601 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
---|
602 | trays(NTrays).OutletL to reb.InletL; |
---|
603 | end |
---|
604 | |
---|
605 | |
---|
606 | #* ------------------------------------------------------------------- |
---|
607 | * Reboiled Stripping Column model with: |
---|
608 | * |
---|
609 | * - NTrays like tray; |
---|
610 | * - a vessel in the bottom of column; |
---|
611 | * - a splitter which separate the bottom product and the stream to reboiler; |
---|
612 | * - steady state reboiler (thermosyphon); |
---|
613 | * |
---|
614 | * ------------------------------------------------------------------*# |
---|
615 | Model Reboiled_Stripping_thermosyphon |
---|
616 | PARAMETERS |
---|
617 | ext PP as CalcObject; |
---|
618 | ext NComp as Integer; |
---|
619 | NTrays as Integer(Brief="Number of trays", Default=2); |
---|
620 | |
---|
621 | VARIABLES |
---|
622 | trays(NTrays) as tray; |
---|
623 | reb as reboilerSteady; |
---|
624 | spbottom as splitter; |
---|
625 | tbottom as tank; |
---|
626 | |
---|
627 | EQUATIONS |
---|
628 | if (reb.OutletV.P > reb.InletL.P) then |
---|
629 | "Pressure Drop through the tray" |
---|
630 | reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P) |
---|
631 | / (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3 |
---|
632 | else |
---|
633 | "Prato selado" |
---|
634 | reb.OutletV.F = 0.0 * "mol/s"; |
---|
635 | end |
---|
636 | |
---|
637 | "Pressure Drop through the tray" |
---|
638 | trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * |
---|
639 | trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P - |
---|
640 | trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV)); |
---|
641 | |
---|
642 | CONNECTIONS |
---|
643 | #vapor |
---|
644 | reb.OutletV to trays(NTrays).InletV; |
---|
645 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
---|
646 | |
---|
647 | #liquid |
---|
648 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
---|
649 | trays(NTrays).OutletL to tbottom.Inlet; |
---|
650 | tbottom.Outlet to spbottom.Inlet; |
---|
651 | spbottom.Outlet2 to reb.InletL; |
---|
652 | end |
---|
653 | |
---|
654 | |
---|
655 | #* ------------------------------------------------------------------- |
---|
656 | * Reboiled Absorption Column model with: |
---|
657 | * |
---|
658 | * - NTrays like tray; |
---|
659 | * - a kettle reboiler; |
---|
660 | * |
---|
661 | * ------------------------------------------------------------------*# |
---|
662 | Model Reboiled_Absorption_kettle |
---|
663 | PARAMETERS |
---|
664 | ext PP as CalcObject; |
---|
665 | ext NComp as Integer; |
---|
666 | NTrays as Integer(Brief="Number of trays", Default=2); |
---|
667 | |
---|
668 | VARIABLES |
---|
669 | trays(NTrays) as tray; |
---|
670 | reb as reboiler; |
---|
671 | |
---|
672 | EQUATIONS |
---|
673 | if (reb.OutletV.P > reb.InletL.P) then |
---|
674 | "Pressure Drop through the tray" |
---|
675 | reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P) |
---|
676 | / (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3 |
---|
677 | else |
---|
678 | "Prato selado" |
---|
679 | reb.OutletV.F = 0.0 * "mol/s"; |
---|
680 | end |
---|
681 | |
---|
682 | "Pressure Drop through the tray" |
---|
683 | trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * |
---|
684 | trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P - |
---|
685 | trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV)); |
---|
686 | |
---|
687 | CONNECTIONS |
---|
688 | #vapor |
---|
689 | reb.OutletV to trays(NTrays).InletV; |
---|
690 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
---|
691 | |
---|
692 | #liquid |
---|
693 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
---|
694 | trays(NTrays).OutletL to reb.InletL; |
---|
695 | end |
---|
696 | |
---|
697 | |
---|
698 | #* ------------------------------------------------------------------- |
---|
699 | * Reboiled Absorption Column model with: |
---|
700 | * |
---|
701 | * - NTrays like tray; |
---|
702 | * - a vessel in the bottom of column; |
---|
703 | * - a splitter which separate the bottom product and the stream to reboiler; |
---|
704 | * - steady state reboiler (thermosyphon); |
---|
705 | * |
---|
706 | * ------------------------------------------------------------------*# |
---|
707 | Model Reboiled_Absorption_thermosyphon |
---|
708 | PARAMETERS |
---|
709 | ext PP as CalcObject; |
---|
710 | ext NComp as Integer; |
---|
711 | NTrays as Integer(Brief="Number of trays", Default=2); |
---|
712 | |
---|
713 | VARIABLES |
---|
714 | trays(NTrays) as tray; |
---|
715 | reb as reboilerSteady; |
---|
716 | spbottom as splitter; |
---|
717 | tbottom as tank; |
---|
718 | |
---|
719 | EQUATIONS |
---|
720 | if (reb.OutletV.P > reb.InletL.P) then |
---|
721 | "Pressure Drop through the tray" |
---|
722 | reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P) |
---|
723 | / (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3 |
---|
724 | else |
---|
725 | "Prato selado" |
---|
726 | reb.OutletV.F = 0.0 * "mol/s"; |
---|
727 | end |
---|
728 | |
---|
729 | "Pressure Drop through the tray" |
---|
730 | trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * |
---|
731 | trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P - |
---|
732 | trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV)); |
---|
733 | |
---|
734 | CONNECTIONS |
---|
735 | #vapor |
---|
736 | reb.OutletV to trays(NTrays).InletV; |
---|
737 | trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV; |
---|
738 | |
---|
739 | #liquid |
---|
740 | trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL; |
---|
741 | trays(NTrays).OutletL to tbottom.Inlet; |
---|
742 | tbottom.Outlet to spbottom.Inlet; |
---|
743 | spbottom.Outlet2 to reb.InletL; |
---|
744 | end |
---|