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 | * Author: Paula B. Staudt |
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17 | * $Id: reboiler.mso 300 2007-07-04 22:55:05Z arge $ |
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18 | *--------------------------------------------------------------------*# |
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19 | |
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20 | using "streams"; |
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21 | |
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22 | Model reboiler |
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23 | ATTRIBUTES |
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24 | Pallete = true; |
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25 | Icon = "icon/Reboiler"; |
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26 | Brief = "Model of a dynamic reboiler - kettle."; |
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27 | Info = " |
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28 | <h2>Assumptions</h2> |
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29 | <ul> |
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30 | <li>perfect mixing of both phases; |
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31 | <li>thermodynamics equilibrium; |
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32 | <li>no liquid entrainment in the vapour stream. |
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33 | </ul> |
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34 | |
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35 | <h2>Specify</h2> |
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36 | <ul> |
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37 | <li> the inlet stream; |
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38 | <li> the liquid inlet stream; |
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39 | <li> the outlet flows: OutletV.F and OutletL.F; |
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40 | <li> the heat supply. |
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41 | </ul> |
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42 | |
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43 | <h2>Initial Conditions</h2> |
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44 | <ul> |
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45 | <li> the reboiler temperature (OutletL.T); |
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46 | <li> the reboiler liquid level (Level); |
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47 | <li> (NoComps - 1) OutletL (OR OutletV) compositions. |
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48 | </ul> |
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49 | "; |
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50 | |
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51 | PARAMETERS |
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52 | outer PP as Plugin(Brief = "External Physical Properties", Type="PP"); |
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53 | outer NComp as Integer; |
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54 | Across as area (Brief="Cross Section Area of reboiler"); |
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55 | V as volume (Brief="Total volume of reboiler"); |
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56 | |
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57 | VARIABLES |
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58 | in Inlet as stream(Brief="Feed Stream"); |
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59 | in InletL as stream(Brief="Liquid inlet stream"); |
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60 | out OutletL as liquid_stream(Brief="Liquid outlet stream"); |
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61 | out OutletV as vapour_stream(Brief="Vapour outlet stream"); |
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62 | in Q as heat_rate (Brief="Heat supplied"); |
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63 | |
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64 | M(NComp) as mol (Brief="Molar Holdup in the tray"); |
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65 | ML as mol (Brief="Molar liquid holdup"); |
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66 | MV as mol (Brief="Molar vapour holdup"); |
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67 | E as energy (Brief="Total Energy Holdup on tray"); |
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68 | vL as volume_mol (Brief="Liquid Molar Volume"); |
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69 | vV as volume_mol (Brief="Vapour Molar volume"); |
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70 | Level as length (Brief="Level of liquid phase"); |
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71 | rhoV as dens_mass (Brief="Vapour Density"); |
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72 | |
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73 | EQUATIONS |
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74 | "Component Molar Balance" |
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75 | diff(M)= Inlet.F*Inlet.z + InletL.F*InletL.z |
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76 | - OutletL.F*OutletL.z - OutletV.F*OutletV.z; |
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77 | |
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78 | "Energy Balance" |
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79 | diff(E) = Inlet.F*Inlet.h + InletL.F*InletL.h |
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80 | - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q; |
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81 | |
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82 | "Molar Holdup" |
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83 | M = ML*OutletL.z + MV*OutletV.z; |
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84 | |
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85 | "Energy Holdup" |
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86 | E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V; |
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87 | |
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88 | "Mol fraction normalisation" |
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89 | sum(OutletL.z)=1.0; |
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90 | sum(OutletL.z)=sum(OutletV.z); |
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91 | |
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92 | "Vapour Density" |
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93 | rhoV = PP.VapourDensity(OutletV.T, OutletV.P, OutletV.z); |
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94 | |
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95 | "Liquid Volume" |
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96 | vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z); |
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97 | |
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98 | "Vapour Volume" |
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99 | vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z); |
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100 | |
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101 | "Chemical Equilibrium" |
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102 | PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = |
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103 | PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z; |
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104 | |
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105 | "Mechanical Equilibrium" |
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106 | OutletL.P = OutletV.P; |
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107 | |
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108 | "Thermal Equilibrium" |
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109 | OutletL.T = OutletV.T; |
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110 | |
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111 | "Geometry Constraint" |
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112 | V = ML*vL + MV*vV; |
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113 | |
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114 | "Level of liquid phase" |
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115 | Level = ML*vL/Across; |
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116 | end |
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117 | |
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118 | #*---------------------------------------------------------------------- |
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119 | * Model of a Steady State reboiler with no thermodynamics equilibrium |
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120 | *---------------------------------------------------------------------*# |
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121 | Model reboilerSteady |
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122 | ATTRIBUTES |
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123 | Pallete = true; |
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124 | Icon = "icon/ReboilerSteady"; |
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125 | Brief = "Model of a Steady State reboiler with no thermodynamics equilibrium - thermosyphon."; |
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126 | Info = |
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127 | "Assumptions: |
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128 | * perfect mixing of both phases; |
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129 | * no thermodynamics equilibrium; |
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130 | * no liquid entrainment in the vapour stream. |
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131 | |
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132 | Specify: |
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133 | * the InletL stream; |
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134 | * the heat supply OR the outlet temperature (OutletV.T); |
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135 | "; |
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136 | |
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137 | PARAMETERS |
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138 | outer PP as Plugin(Brief = "External Physical Properties", Type="PP"); |
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139 | outer NComp as Integer; |
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140 | DP as press_delta (Brief="Pressure Drop in the reboiler"); |
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141 | |
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142 | VARIABLES |
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143 | in InletL as stream(Brief="Liquid inlet stream"); |
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144 | out OutletV as vapour_stream(Brief="Vapour outlet stream"); |
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145 | in Q as heat_rate (Brief="Heat supplied"); |
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146 | vV as volume_mol (Brief="Vapour Molar volume"); |
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147 | rhoV as dens_mass (Brief="Vapour Density"); |
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148 | |
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149 | EQUATIONS |
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150 | "Molar Balance" |
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151 | InletL.F = OutletV.F; |
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152 | InletL.z = OutletV.z; |
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153 | |
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154 | "Vapour Volume" |
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155 | vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z); |
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156 | |
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157 | "Vapour Density" |
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158 | rhoV = PP.VapourDensity(OutletV.T, OutletV.P, OutletV.z); |
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159 | |
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160 | "Energy Balance" |
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161 | InletL.F*InletL.h + Q = OutletV.F*OutletV.h; |
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162 | |
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163 | "Pressure" |
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164 | DP = InletL.P - OutletV.P; |
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165 | end |
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166 | |
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167 | #*---------------------------------------------------------------------- |
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168 | * Model of a Steady State reboiler with fake calculation of |
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169 | * vaporisation fraction and output temperature, but with a real |
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170 | * calculation of the output stream enthalpy |
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171 | *---------------------------------------------------------------------*# |
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172 | Model reboilerSteady_fakeH |
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173 | ATTRIBUTES |
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174 | Pallete = true; |
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175 | Icon = "icon/ReboilerSteady"; |
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176 | Brief = "Model of a Steady State reboiler with fake calculation of outlet conditions."; |
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177 | Info = |
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178 | "Model of a Steady State reboiler with fake calculation of |
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179 | vaporisation fraction and output temperature, but with a real |
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180 | calculation of the output stream enthalpy. |
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181 | "; |
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182 | |
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183 | PARAMETERS |
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184 | outer PP as Plugin(Brief = "External Physical Properties", Type="PP"); |
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185 | outer NComp as Integer; |
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186 | DP as press_delta (Brief="Pressure Drop in the reboiler"); |
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187 | k as Real (Brief = "Flow Constant", Unit='mol/J'); |
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188 | |
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189 | VARIABLES |
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190 | in InletL as stream(Brief="Liquid inlet stream"); |
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191 | out OutletV as stream(Brief="Vapour outlet stream"); |
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192 | in Q as heat_rate (Brief="Heat supplied"); |
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193 | |
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194 | EQUATIONS |
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195 | "Molar Balance" |
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196 | InletL.F = OutletV.F; |
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197 | InletL.z = OutletV.z; |
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198 | |
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199 | "Energy Balance" |
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200 | InletL.F*InletL.h + Q = OutletV.F*OutletV.h; |
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201 | |
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202 | "Pressure" |
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203 | DP = InletL.P - OutletV.P; |
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204 | |
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205 | "Fake Vapourisation Fraction" |
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206 | OutletV.v = 1.0; |
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207 | |
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208 | "Fake output temperature" |
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209 | OutletV.T = 300*'K'; |
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210 | |
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211 | "Pressure Drop through the reboiler" |
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212 | OutletV.F = k*Q; |
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213 | end |
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214 | |
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215 | #*------------------------------------------------------------------- |
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216 | * Model of a dynamic reboiler with reaction |
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217 | *-------------------------------------------------------------------*# |
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218 | Model reboilerReact |
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219 | ATTRIBUTES |
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220 | Pallete = true; |
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221 | Icon = "icon/Reboiler"; |
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222 | Brief = "Model of a dynamic reboiler with reaction."; |
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223 | Info = |
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224 | "Assumptions: |
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225 | * perfect mixing of both phases; |
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226 | * thermodynamics equilibrium; |
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227 | * no liquid entrainment in the vapour stream; |
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228 | * the reaction takes place only in the liquid phase. |
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229 | |
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230 | Specify: |
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231 | * the kinetics variables; |
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232 | * the inlet stream; |
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233 | * the liquid inlet stream; |
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234 | * the outlet flows: OutletV.F and OutletL.F; |
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235 | * the heat supply. |
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236 | |
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237 | Initial Conditions: |
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238 | * the reboiler temperature (OutletL.T); |
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239 | * the reboiler liquid level (Level); |
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240 | * (NoComps - 1) OutletL (OR OutletV) compositions. |
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241 | "; |
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242 | |
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243 | PARAMETERS |
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244 | outer PP as Plugin(Type="PP"); |
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245 | outer NComp as Integer; |
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246 | Across as area (Brief="Cross Section Area of reboiler"); |
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247 | V as volume (Brief="Total volume of reboiler"); |
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248 | |
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249 | stoic(NComp) as Real(Brief="Stoichiometric matrix"); |
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250 | Hr as energy_mol; |
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251 | Pstartup as pressure; |
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252 | |
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253 | VARIABLES |
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254 | in Inlet as stream(Brief="Feed Stream"); |
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255 | in InletL as stream(Brief="Liquid inlet stream"); |
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256 | out OutletL as liquid_stream(Brief="Liquid outlet stream"); |
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257 | out OutletV as vapour_stream(Brief="Vapour outlet stream"); |
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258 | |
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259 | Q as heat_rate (Brief="Heat supplied"); |
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260 | M(NComp) as mol (Brief="Molar Holdup in the tray"); |
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261 | ML as mol (Brief="Molar liquid holdup"); |
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262 | MV as mol (Brief="Molar vapour holdup"); |
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263 | E as energy (Brief="Total Energy Holdup on tray"); |
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264 | vL as volume_mol (Brief="Liquid Molar Volume"); |
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265 | vV as volume_mol (Brief="Vapour Molar volume"); |
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266 | Level as length (Brief="Level of liquid phase"); |
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267 | Vol as volume; |
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268 | startup as Real; |
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269 | rhoV as dens_mass; |
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270 | r3 as reaction_mol (Brief = "Reaction resulting ethyl acetate", DisplayUnit = 'mol/l/s'); |
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271 | C(NComp) as conc_mol (Brief = "Molar concentration", Lower = -1); |
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272 | |
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273 | EQUATIONS |
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274 | "Molar Concentration" |
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275 | OutletL.z = vL * C; |
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276 | |
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277 | "Reaction" |
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278 | r3 = exp(-7150*'K'/OutletL.T)*(4.85e4*C(1)*C(2) - 1.23e4*C(3)*C(4)) * 'l/mol/s'; |
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279 | |
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280 | "Component Molar Balance" |
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281 | diff(M)= Inlet.F*Inlet.z + InletL.F*InletL.z |
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282 | - OutletL.F*OutletL.z - OutletV.F*OutletV.z + stoic*r3*ML*vL; |
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283 | |
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284 | "Energy Balance" |
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285 | diff(E) = Inlet.F*Inlet.h + InletL.F*InletL.h |
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286 | - OutletL.F*OutletL.h - OutletV.F*OutletV.h + Q + Hr * r3 * vL*ML; |
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287 | |
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288 | "Molar Holdup" |
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289 | M = ML*OutletL.z + MV*OutletV.z; |
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290 | |
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291 | "Energy Holdup" |
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292 | E = ML*OutletL.h + MV*OutletV.h - OutletL.P*V; |
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293 | |
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294 | "Mol fraction normalisation" |
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295 | sum(OutletL.z)=1.0; |
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296 | |
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297 | "Liquid Volume" |
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298 | vL = PP.LiquidVolume(OutletL.T, OutletL.P, OutletL.z); |
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299 | "Vapour Volume" |
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300 | vV = PP.VapourVolume(OutletV.T, OutletV.P, OutletV.z); |
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301 | "Vapour Density" |
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302 | rhoV = PP.VapourDensity(OutletV.T, OutletV.P, OutletV.z); |
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303 | |
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304 | "Level of liquid phase" |
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305 | Level = ML*vL/Across; |
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306 | |
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307 | Vol = ML*vL; |
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308 | |
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309 | "Mechanical Equilibrium" |
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310 | OutletL.P = OutletV.P; |
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311 | |
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312 | "Thermal Equilibrium" |
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313 | OutletL.T = OutletV.T; |
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314 | |
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315 | "Geometry Constraint" |
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316 | V = ML*vL + MV*vV; |
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317 | |
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318 | "Chemical Equilibrium" |
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319 | PP.LiquidFugacityCoefficient(OutletL.T, OutletL.P, OutletL.z)*OutletL.z = |
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320 | PP.VapourFugacityCoefficient(OutletV.T, OutletV.P, OutletV.z)*OutletV.z; |
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321 | |
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322 | sum(OutletL.z)=sum(OutletV.z); |
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323 | |
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324 | end |
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