diff options
Diffstat (limited to 'Chemical_Engineering_Thermodynamics')
17 files changed, 263 insertions, 531 deletions
diff --git a/Chemical_Engineering_Thermodynamics/ch10_1.ipynb b/Chemical_Engineering_Thermodynamics/ch10_1.ipynb index ed294198..0a1b388b 100644 --- a/Chemical_Engineering_Thermodynamics/ch10_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch10_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:3b50ad151f89e9ea380ce80c8112ec5468586c82e236862a1e3d8e194fa15249" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,7 +28,6 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Preparation of fugacity and fugacity coefficient\n", "\n", "import math\n", "\n", @@ -113,8 +113,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of enthalpy entropy and internal energy change\n", - "\n", + " \n", "\n", "import math \n", "from scipy.integrate import quad \n", @@ -249,8 +248,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of molar heat capacity\n", - "\n", + " \n", "# Variables\n", "T = 35 + 273.15;\t\t\t#[K] - Temperature\n", "P = 10;\t\t\t#[atm] - Pressure\n", @@ -307,8 +305,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final temperature after expansion\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "\n", "# Variables\n", @@ -387,8 +384,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of fugacity of liquid benzene\n", - "\n", + " \n", "# Variables\n", "T = 220 + 273.15;\t\t\t#[K] - Temperature\n", "Tc = 562.2;\t\t\t#[K] - Critical temperature\n", @@ -463,8 +459,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of molar enthalpy\n", - "\n", + " \n", "# Variables\n", "# C = -0.067 + 30.7/T\n", "# D = 0.0012 - 0.416/T\n", @@ -520,8 +515,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of second and third virial coefficients and fugacity\n", - "\n", + " \n", "# Variables\n", "# (1)\n", "T = 311;\t\t\t#[K] - Temperature\n", @@ -626,8 +620,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of second and third virial coefficients\n", - "\n", + " \n", "# Variables\n", "T = 0 + 273.15;\t\t\t#[K] - Temperature\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", @@ -722,8 +715,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of work done and the exit temperature\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math\n", "from scipy.integrate import quad \n", @@ -948,8 +940,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of temperature and pressure\n", - "\n", + " \n", "# Variables\n", "Vol = 0.15;\t\t\t #[m**(3)] - Volume of the cylinder\n", "P_1 = 100.;\t\t\t #[bar] - Initial pressure\n", @@ -1089,8 +1080,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of change of internal energy enthalpy entropy and exergy\n", - "\n", + " \n", "# Variables\n", "P_1 = 80.;\t\t\t #[bar] - Initial pressure\n", "P_1 = P_1*10.**(5);\t\t\t#[Pa]\n", @@ -1187,8 +1177,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of change in enthalpy\n", - "\n", + " \n", "# Variables\n", "T_1 = 500.;\t\t\t#[K] - Initial temperature\n", "P_1 = 30.;\t\t\t#[atm] - Initial pressure\n", @@ -1255,14 +1244,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final temperature\n", - "\n", - "#(1)\n", - "#This part involves proving a relation in which no mathematical components are involved.\n", - "#For proof refer to this example 10.14 on page number 354 of the book.\n", - "\n", - "\n", - "#(2)\n", + " \n", "\n", "# Variables\n", "Vol_1 = 0.1;\t\t\t#[m**(3)] - Initial volume of each compartment\n", @@ -1311,8 +1293,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of work done and the exit temperature\n", - "\n", + " \n", "# Variables\n", "P_1 = 1*10**(6);\t\t\t#[Pa] - Initial pressure\n", "T_1 = 200 + 273.15;\t\t\t#[K] - Initial temperature\n", @@ -1450,8 +1431,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of molar volume and fugacity\n", - "\n", + " \n", "# Variables\n", "T = 100 + 273.15;\t\t\t#[K] - Temperature\n", "Tc = 647.1;\t\t\t#[K] - Critical temperature of water\n", @@ -1514,9 +1494,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of enthalpy and entropy change\n", - "\n", - "# Variables\n", + " \n", "P_1 = 6;\t\t\t#[bar] - Initial pressure\n", "P_1 = P_1*10**(5);\t\t\t#[Pa]\n", "T_1 = 100 + 273.15;\t\t\t#[T] - Initial temperature\n", @@ -1650,8 +1628,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of fugacity\n", - "\n", + " \n", "# Variables\n", "P = 2.76*10**(6);\t\t\t#[N/m**(2)] - Pressure\n", "T = 310.93;\t\t\t#[K] - Temperature\n", @@ -1739,8 +1716,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of enthalpy change\n", - "\n", + " \n", "# Variables\n", "T = 50+273.15;\t\t\t#[K] - Temperature\n", "P = 25.*10**(3);\t\t\t#[Pa] - Pressure\n", @@ -1878,8 +1854,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of fugacity of water vapour\n", - "\n", + " \n", "# Variables\n", "T = 320 + 273.15;\t\t\t#[K]\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", @@ -1975,8 +1950,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of change in internal energy\n", - "\n", + " \n", "# Variables\n", "Vol = 0.057;\t\t\t#[m**(3)] - Volume of car tyre\n", "P_1 = 300.;\t\t\t#[kPa] - Initial pressure\n", @@ -2071,8 +2045,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of enthalpy and entropy change\n", - "\n", + " \n", "# Variables\n", "T_1 = 150 + 273.15;\t\t\t#[K] - Initial emperature\n", "T_2 = T_1;\t\t\t# Isothermal process\n", @@ -2195,8 +2168,6 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final temperature and pressure\n", - "\n", "# Variables\n", "Vol = 0.15;\t\t\t#[m**(3)]\n", "T_1 = 170;\t\t\t#[K] - Initial emperature\n", @@ -2370,8 +2341,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of vapour pressure\n", - "\n", + " \n", "# Variables\n", "T = 373.15;\t\t\t#[K]\n", "Tc = 562.16;\t\t\t#[K]\n", @@ -2460,8 +2430,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of vapour pressure\n", - "\n", + " \n", "# Variables\n", "T = 150 + 273.15;\t\t\t#[K]\n", "Tc = 647.1;\t\t\t#[K]\n", diff --git a/Chemical_Engineering_Thermodynamics/ch11_1.ipynb b/Chemical_Engineering_Thermodynamics/ch11_1.ipynb index fdf3f695..79f48f9c 100644 --- a/Chemical_Engineering_Thermodynamics/ch11_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch11_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:ea5fa2ce45062851dc4892fcc5b621c33d72fa0443d476b1ef4133dade9e39b0" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of volumes of ethanol and water\n", - "\n", + " \n", "import math\n", "\n", "# Variables\n", @@ -89,8 +89,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Developing an expression\n", - "\n", + " \n", "# Variables\n", "T = 25+273.15;\t\t\t#[K] - Temperature\n", "P = 1;\t\t\t#[atm]\n", @@ -144,8 +143,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of enthalpies\n", - "\n", + " \n", "# Variables\n", "#H = a*x_1 + b*x_2 +c*x_1*x_2\n", "\n", @@ -233,8 +231,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of minimum work required\n", - "\n", + " \n", "# Variables\n", "n = 1*10**(3);\t\t\t#[mol] - No of moles\n", "P = 0.1;\t\t\t#[MPa] - Pressure of the surrounding\n", @@ -289,8 +286,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of fugacity 0f the mixture\n", - "\n", + " \n", "# Variables\n", "x_A = 0.20;\t\t\t# Mole fraction of A\n", "x_B = 0.35;\t\t\t# Mole fraction of B\n", diff --git a/Chemical_Engineering_Thermodynamics/ch12_1.ipynb b/Chemical_Engineering_Thermodynamics/ch12_1.ipynb index 6b7a0b02..0ee70a67 100644 --- a/Chemical_Engineering_Thermodynamics/ch12_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch12_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:acb0234cca7ef04cf2e231ae1d04809101d746587fbd14cf847d456347c563ea" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of partial molar volume\n", - "\n", + " \n", "\n", "import math \n", "from numpy import *\n", @@ -116,8 +116,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of volume of the mixture\n", - "\n", + " \n", "# Variables\n", "#component 1 = water\n", "#component 2 = methanol\n", @@ -187,11 +186,9 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of volumes\n", + " \n", + " \n", "\n", - "# Variables\n", - "#component 1 = methanol\n", - "#component 2 = water\n", "Vol = 20;\t\t\t#[cm**(3)] - Volume of the solution\n", "T = 22 + 273.15;\t\t\t#[K] - Temperature\n", "W_bottle = 11.5485;\t\t\t#[g] - Weight of density bottle\n", @@ -322,8 +319,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of partial molar volumes\n", - "\n", + " \n", "from numpy import *\n", "\n", "\n", @@ -429,8 +425,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of enthalpy\n", - "\n", + " \n", "# Variables\n", "T = 40 + 273.15;\t\t\t#[K] - Temperature\n", "\n", diff --git a/Chemical_Engineering_Thermodynamics/ch13_1.ipynb b/Chemical_Engineering_Thermodynamics/ch13_1.ipynb index 4dce9007..3cee342e 100644 --- a/Chemical_Engineering_Thermodynamics/ch13_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch13_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:894f18dec91baf4a10867e0d301a68220274d02a1e24c4e2bef1038061daa009" }, "nbformat": 3, "nbformat_minor": 0, @@ -28,8 +29,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Caculation of fugacity coefficients\n", - "\n", + " \n", "import math \n", "\n", "\n", @@ -136,8 +136,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of fugacity coefficients\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "\n", diff --git a/Chemical_Engineering_Thermodynamics/ch14_1.ipynb b/Chemical_Engineering_Thermodynamics/ch14_1.ipynb index 03350db4..be081f3c 100644 --- a/Chemical_Engineering_Thermodynamics/ch14_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch14_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:98f2e1e0f1c561d3ee302fd629093b7572c8b263613f73036059e7020f90d8cc" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Proving a mathematical relation\n", - "\n", + " \n", "import math\n", "\n", "# Variables,\n", @@ -93,9 +93,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Comparision of Margules and van Laar eqations\n", - "\n", - "\n", + " \n", "import math \n", "from numpy import zeros\n", "from scipy.stats import linregress\n", @@ -169,8 +167,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of activity coefficients\n", - "\n", + " \n", "# Variables,\n", "T = 60 + 273.15;\t\t\t#[K] - Temperature\n", "R = 1.987;\t\t\t#[cal/mol*K] - Universal gas constant\n", @@ -244,8 +241,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of the value of activity coefficients\n", - "\n", + " \n", "# Variables \n", "T = 307;\t\t\t#[K]\n", "x_1 = 0.047;\n", @@ -372,8 +368,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of the value of activity coefficients\n", - "\n", + " \n", "# Variables,\n", "T = 25 + 273.15;\t\t\t#[K] - Temperature\n", "R = 1.987;\t\t\t#[cal/mol*K] - Universal gas constant\n", @@ -426,8 +421,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of the value of activity coefficients\n", - "\n", + " \n", "# Variables,\n", "T = 25 + 273.15;\t\t\t#[K] - Temperature\n", "mol_HCl = 0.001;\t\t\t#[mol/kg] - Molality of HCl\n", @@ -479,8 +473,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of the value of activity coefficients\n", - "\n", + " \n", "# Variables,\n", "T = 25 + 273.15;\t\t\t#[K] - Temperature\n", "mol_CaCl2 = 0.001;\t\t\t#[mol/kg] - Molality of HCl\n", @@ -528,8 +521,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Proving a mathematical relation\n", - "\n", + " \n", "# Variables,\n", "T = 50 + 273.15;\t\t\t#[K] - Temperature\n", "R=8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", @@ -583,8 +575,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# calculation of enthalpy entropy and Gibbs free energy\n", - "\n", + " \n", "# Variables\n", "T = 293.15;\t\t\t#[K] - Temperature\n", "R=8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", @@ -654,8 +645,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of Gibbs free energy and enthalpy change\n", - "\n", + " \n", "# Given\n", "T = 60 + 273.15;\t\t\t#[K] - Temperature\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", diff --git a/Chemical_Engineering_Thermodynamics/ch15_1.ipynb b/Chemical_Engineering_Thermodynamics/ch15_1.ipynb index ad62c947..fcfb0cd5 100644 --- a/Chemical_Engineering_Thermodynamics/ch15_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch15_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:aa6f699613cdf9bcba2dda4617212630ca1760d21939d5cd99d17e7e03b7e885" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of number of moles in liquid and vapour phase\n", - "\n", + " \n", "# Variables\n", "T = 90+ 273.15;\t\t\t#[K] - Temperature\n", "P = 1;\t\t\t#[atm] - Pressure\n", @@ -97,8 +97,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure temperature and composition\n", - "\n", + " \n", "import math\n", "\n", "# Variables\n", @@ -232,14 +231,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure temperature and composition\n", - "\n", - "# Variables\n", - "\t\t\t# math.log(P_1_sat) = 14.3916 - 2795.82/(t + 230.00)\n", - "\t\t\t# math.log(P_2_sat) = 14.2724 - 2945.47/(t + 224.00)\n", - "\t\t\t# math.log(P_3_sat) = 14.2043 - 2972.64/(t + 209.00)\n", - "\n", - "\t\t\t#(a)\n", + " \n", "x_1_a = 0.25;\t\t\t# Equilibrium composition of liquid phase\n", "x_2_a = 0.35;\n", "x_3_a = 1 - x_1_a - x_2_a;\n", @@ -381,8 +373,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure and composition\n", - "\n", + " \n", "import math\n", "\n", "# Variables\n", @@ -458,8 +449,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure temperature and composition\n", - "\n", + " \n", "import math\n", "# Variables\n", "T = 27;\t\t\t#[C] - Temperature\n", @@ -556,8 +546,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determinatin of DPT and BPT\n", - "\n", + " \n", "# Variables\n", "P = 90;\t\t\t#[kPa] - Pressure\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", @@ -639,8 +628,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of range of temperature for which two phase exists\n", - "\n", + " \n", "# Variables\n", "P = 1;\t\t\t#[bar] - Pressure\n", "P = P*10**(2);\t\t\t#[kPa]\n", @@ -732,8 +720,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of DPT and BPT\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "\n", @@ -859,8 +846,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of range of pressure for which two phase exists\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "\n", @@ -959,8 +945,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of vapour and liquid phase composition\n", - "\n", + " \n", "# Variables\n", "T = 50;\t\t\t#[C] - Temperature\n", "P = 64;\t\t\t#[kPa] - Pressure\n", @@ -1037,8 +1022,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of temperature\n", - "\n", + " \n", "# Variables\n", "P = 12.25*101325*10**(-3);\t\t\t#[kPa]\n", "z_1 = 0.8;\n", @@ -1121,8 +1105,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of number of moles in liquid and vapour phase\n", - "\n", + " \n", "# Variables\n", "T = 105;\t\t\t#[C]\n", "P = 1.5;\t\t\t#[atm]\n", @@ -1173,8 +1156,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of vapour and liquid phase composition\n", - "\n", + " \n", "# Variables\n", "T = 90;\t\t\t#[C]\n", "P = 1;\t\t\t#[atm]\n", @@ -1235,8 +1217,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Preparation of table having composition and pressure data\n", - "\n", + " \n", "from numpy import zeros\n", "\n", "# Variables\n", @@ -1340,8 +1321,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of DPT and BPT\n", - "\n", + " \n", "# Variables\n", "P_1_sat = 79.80;\t\t\t#[kPa]\n", "P_2_sat = 40.45;\t\t\t#[kPa]\n", @@ -1409,7 +1389,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure\n", + "\n", "\n", "# Variables\n", "T = 78.15;\t\t\t#[C]\n", @@ -1473,8 +1453,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of van Laar activity coefficient parameters\n", - "\n", + " \n", "from scipy.stats import linregress\n", "\n", "# Variables\n", @@ -1546,8 +1525,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Prediction of azeotrrope formation\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "\n", @@ -1623,8 +1601,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Tabulation of activity coefficients relative volatility and compositions\n", - "\n", + " \n", "# Variables\n", "T = 45;\t\t\t#[C] - Temperature\n", "\n", @@ -1733,8 +1710,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Tabulation of partial pressure and total pressure data of components\n", - "\n", + " \n", "# Variables\n", "T = 25;\t\t\t#[C] - Temperature\n", "P_1_sat = 230.4;\t\t\t#[mm Hg]\n", @@ -1837,9 +1813,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of azeotrope formation\n", - "\n", - "# Variables\n", + " \n", "T = 50;\t\t\t#[C]\n", "\t\t\t# At 50 C\n", "P_1_sat = 0.67;\t\t\t#[atm]\n", @@ -1923,8 +1897,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Tabulation of pressure and composition data\n", - "\n", + " \n", "# Variables\n", "T = 25;\t\t\t#[C]\n", "\t\t\t# At 50 C\n", @@ -2027,8 +2000,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of van Laar parameters\n", - "\n", + " \n", "# Variables\n", "T = 58.7;\t\t\t#[C]\n", "P = 1;\t\t\t#[atm]\n", diff --git a/Chemical_Engineering_Thermodynamics/ch16_1.ipynb b/Chemical_Engineering_Thermodynamics/ch16_1.ipynb index 902f4a5c..69003cd3 100644 --- a/Chemical_Engineering_Thermodynamics/ch16_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch16_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:a00a89ec39a5812cdf143d7f00f601a0bb401404f1638737e2689f71d07acb65" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of solubility\n", - "\n", + " \n", "import math \n", "\n", "# Variables\t\t\t\n", @@ -125,8 +125,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of solubility\n", - "\n", + " \n", "import math \n", "from scipy.integrate import quad \n", "\n", @@ -201,8 +200,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of composition\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "\n", @@ -289,8 +287,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of equilibrium composition\n", - "\n", + " \n", "# Variables\n", "T = 300;\t\t\t#[K]\n", "R = 8.314;\t\t\t#[J/mol*K] - universal gas constant\n", @@ -334,9 +331,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of freezing point depression\n", - "\n", - "# Variables\n", + " \n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", "M_wt_meth = 32;\t\t\t# Molecular weight of methanol \n", "M_wt_water = 18;\t\t\t# Molecular weight of water \n", @@ -387,8 +382,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of freezing point\n", - "\n", + " \n", "# Variables\n", "R = 8.314;\t\t\t#[J/mol*K] - universal gas constant\n", "T_f = 273.15;\t\t\t#[K] - Freezing point of water\n", @@ -445,8 +439,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "#Determination of boiling point elevation \n", - "\n", + " \n", "# Variables\n", "R = 8.314;\t\t\t#[J/mol*K] - universal gas constant\n", "T_b = 373.15;\t\t\t#[K] - Boiling point of water\n", @@ -497,8 +490,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of osmotic pressure\n", - "\n", + " \n", "# Variables\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", "T = 25 + 273.15;\t\t\t#[K] - Surrounding temperature \n", @@ -549,7 +541,6 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of pressure\n", "\n", "# Variables\n", "R = 8.314;\t\t\t#[J/mol*K] - universal gas constant\n", @@ -612,8 +603,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "#Determination of amount of precipitate\n", - "\n", + " \n", "# Variables\n", "R = 8.314;\t\t\t#[J/mol*K] - universal gas constant\n", "T = 173.15;\t\t\t#[K] - Surrounding temperature\n", @@ -678,8 +668,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure\n", - "\n", + " \n", "# Variables\n", "R = 8.314;\t\t\t#[J/mol*K] - universal gas constant\n", "T = 350.;\t\t\t#[K] - Surrounding temperature\n", diff --git a/Chemical_Engineering_Thermodynamics/ch17_1.ipynb b/Chemical_Engineering_Thermodynamics/ch17_1.ipynb index f87043e6..004b3bab 100644 --- a/Chemical_Engineering_Thermodynamics/ch17_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch17_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:e354b0525ce1aff27214eb76f8a2c9be56cfff2939a8a4b8688a7fe1cea4959c" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of number of moles\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "\n", @@ -165,8 +165,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of equilibrium composition\n", - "\n", + " \n", "# Variables\n", "T = 600;\t\t\t#[K] - Reactor temperature\n", "P = 300;\t\t\t#[atm] - Reactor pressure\n", @@ -236,8 +235,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of the value of equilibrium constant\n", - "\n", + " \n", "# Variables\t\t\n", "T = 600;\t\t\t#[K] - Reactor temperature\n", "P = 4;\t\t\t#[atm] - Reactor pressure\n", @@ -332,8 +330,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of mole fraction\n", - "\n", + " \n", "# Variables\n", "T = 400;\t\t\t#[K] - Reactor temperature\n", "P = 1;\t\t\t#[atm] - Reactor pressure\n", @@ -380,7 +377,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of number of moles\n", + " \n", "\n", "# Variables\n", "T = 749.;\t\t\t#[K] - Reactor temperature\n", @@ -479,7 +476,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# \t\tCalculation of mole fraction\n", + " \n", "\n", "# Variables\n", "T = 500;\t\t\t#[K]\n", @@ -612,7 +609,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "#Dtermination of heat of reaction \n", + " \n", "\n", "from scipy.optimize import fsolve \n", "import math \n", @@ -740,7 +737,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Tabulation of equilibrium constant values\n", + " \n", "\n", "from numpy import *\n", "\n", @@ -859,7 +856,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of mean standard enthalpy of reaction\n", + " \n", "\n", "# Variables\n", "\t\t\t# SO2 + (1/2)*O2 - SO3\n", @@ -905,7 +902,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of equilibrium composition\n", + " \n", "\n", "# Variables\n", "T_1 = 298.15;\t\t\t#[K]\n", @@ -1069,7 +1066,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of equilibrium composition\n", + " \n", "\n", "# Variables\n", "T = 25 + 298.15;\t\t\t#[K] - Temperature\n", @@ -1135,7 +1132,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of the\n", + " \n", "\n", "# Variables\t\t\t\n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard reaction temperature\n", @@ -1219,7 +1216,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of the value of Gibbs free energy\n", + " \n", "\n", "# Variables\n", "\t\t\t# CaCO3 (s1) - CaO (s2) + CO2 (g)\n", @@ -1284,7 +1281,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of nu\n", + " \n", "\n", "# Variables\n", "T = 700 + 273.15;\t\t\t#[K]\n", @@ -1359,8 +1356,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of value of the equilibrium constant\n", - "\n", + " \n", "# Variables \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard reaction temperature\n", "T_2 = 1042;\t\t\t#[K] - Reaction temperature\n", @@ -1456,7 +1452,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of the value of equilibrium constant\n", + " \n", "\n", "# Variables \n", "T_1 = 298.15;\t\t\t#[k] - Smath.tan(math.radiansard reaction temperature\n", @@ -1545,8 +1541,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of standard equilibrium cell voltage\n", - "\n", + " \n", "# Variables\n", "delta_G_H2O_298 = -237.034;\t\t\t#[kJ/mol] - Smath.tan(math.radiansard Gibbs free energy of formation of H2O (l) at 298 K\n", "F = 96485;\t\t\t#[C/mol] - Faraday constant\n", @@ -1614,8 +1609,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of number of chemical reactions\n", - "\n", + " \n", "# Variables\t\t\t\n", "P = 2;\t\t\t# Number of phases\n", "C = 5;\t\t\t# Number of components\n", @@ -1704,8 +1698,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of number of chemical reactions\n", - "\n", + " \n", "# Variables\t\t\t\n", "T = 400.;\t\t\t#[K] - Temperature\n", "P = 1.;\t\t\t#[atm] - Pressure\n", @@ -1866,9 +1859,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of equilibrium composition\n", - "\n", - "# Variables\n", + " \n", "T = 600;\t\t\t#[K] - Temperature\n", "P = 1;\t\t\t#[atm] - Pressure\n", "R = 1.987;\t\t\t#[cal/mol-K] - Universal gas consatnt\n", @@ -1974,9 +1965,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of number of moles\n", - "\n", - "# Variables \n", + " \n", "T = 600 + 273.15;\t\t\t#[K] - Reaction temperature\n", "P = 1;\t\t\t#[atm] - Reaction pressure\n", "\n", diff --git a/Chemical_Engineering_Thermodynamics/ch18_1.ipynb b/Chemical_Engineering_Thermodynamics/ch18_1.ipynb index 730764b8..46865b0c 100644 --- a/Chemical_Engineering_Thermodynamics/ch18_1.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch18_1.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:32121f42f5b148741ef15da1993d191234c228c3ab7dcf05f69114fbe323a883" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of heat transfer\n", - "\n", + " \n", "\n", "import math \n", "from scipy.integrate import quad \n", @@ -124,7 +124,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of adiabatic flame temperature\n", + " \n", "\n", "from scipy.optimize import fsolve \n", "\n", @@ -205,8 +205,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of mole fraction and average heat capacity\n", - "\n", + " \n", "# Variables\n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard reaction temperature\n", "\n", @@ -258,8 +257,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of adiabatic flame temperature\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "\n", "\n", @@ -348,8 +346,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of conversion\n", - "\n", + " \n", "# Variables\n", "\t\t\t# N2 + 3H2 - 2NH3\n", "T_1 = 700;\t\t\t#[K] - Reaction temperature\n", @@ -406,8 +403,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of maximum pressure\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "from scipy.integrate import quad \n", @@ -497,7 +493,7 @@ "input": [ "from scipy.optimize import fsolve\n", "import math\n", - "# Calculation of number of moles\n", + " \n", "\n", "# Variables\n", "T_1 = 400 + 273.15;\t\t\t#[K]\n", diff --git a/Chemical_Engineering_Thermodynamics/ch1_2.ipynb b/Chemical_Engineering_Thermodynamics/ch1_2.ipynb index 558a147b..b7e6716d 100644 --- a/Chemical_Engineering_Thermodynamics/ch1_2.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch1_2.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:05ef5db2afef7232054abda0278780d1df8c92b807546fcd7648e8885fa4539f" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,11 +28,10 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure and heat transfer in piston cylinder assembly\n", - "\n", + "# \n", "# Variables\n", "#(a)\n", - "# The pressure in the cylinder is due to the weight of the piston and due to surroundings pressure\n", + " \n", "m = 50.;\t\t\t#[kg] - Mass of piston\n", "A = 0.05;\t\t\t#[m**(2)] - Area of piston\n", "g = 9.81;\t\t\t#[m/s**(2)] - Acceleration due to gravity\n", @@ -75,7 +75,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of mass of air contained in a room\n", + " \n", "\n", "# Variables\n", "P = 1.;\t\t\t#[atm] - Atmospheric pressure\n", @@ -123,7 +123,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of work done\n", + " \n", "\n", "# Variables\n", "P1 = 3.;\t\t\t# [bar] - initial pressure\n", @@ -191,7 +191,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of wind energy per unit mass and diameter of the wind turbine\n", + " \n", "\n", "# Variables\n", "#(a)\n", @@ -243,8 +243,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of temperature\n", - "\n", + " \n", "# Given\n", "P = 1.;\t\t\t # [bar] - atospheric pressure\n", "P1guz = 0.75;\t\t\t# [bar] - gauze pressure in 1st evaporator\n", @@ -289,8 +288,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of dryness fraction of steam\n", - "\n", + " \n", "# Variables\n", "V = 1.;\t\t\t # [kg] - volume of tank\n", "P = 10.;\t\t\t# [bar] - pressure\n", @@ -335,8 +333,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of pressure mass and volume\n", - "\n", + " \n", "# Variables\n", "V = 1.;\t\t\t# [m**(3)] - volume of tank\n", "M = 10.;\t\t\t# [m**(3)] - total mass\n", @@ -394,8 +391,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of heat supplied\n", - "\n", + " \n", "# Variables\n", "V = 10.;\t\t\t# [m**(3)] - volume of vessel\n", "P_1 = 1.;\t\t\t# [bar] - initial pressure\n", @@ -464,8 +460,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of saturation temperature\n", - "\n", + " \n", "# Variables\n", "#Antoine equation for water ln(Psat)=16.262-(3799.89/(T_sat + 226.35))\n", "P = 2.;\t\t\t#[atm] - Pressure\n", @@ -511,8 +506,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure and temperature at triple point\n", - "\n", + " \n", "# Variables\n", "# math.log(P)=-(1640/T)+10.56 (solid)\n", "# math.log(P)=-(1159/T)+7.769 (liquid)%where T is in K\n", @@ -556,8 +550,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of value of R Cp0 and Cv0\n", - "\n", + " \n", "# Variables\n", "M_O2 = 31.999;\t\t\t#molecular weight of oxygen\n", "M_N2 = 28.014;\t\t\t#molecular weight of nitrogen\n", @@ -606,8 +599,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of molar heat capacity\n", - "\n", + " \n", "# Variables\n", "Y = 1.4;\t\t\t#molar heat capacities ratio for air\n", "R = 8.314;\t\t\t# [J/mol*K] - Universal gas constant\n", @@ -646,8 +638,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of mean heat capacity\n", - "\n", + " \n", "from scipy.integrate import quad\n", "\n", "# Variables\n", @@ -690,8 +681,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of enthalpy of water\n", - "\n", + " \n", "# Variables\n", "#(a)\n", "P_1 = 0.2;\t\t\t# [MPa] - pressure\n", diff --git a/Chemical_Engineering_Thermodynamics/ch2_2.ipynb b/Chemical_Engineering_Thermodynamics/ch2_2.ipynb index 659ed555..b3f8bd13 100644 --- a/Chemical_Engineering_Thermodynamics/ch2_2.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch2_2.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:6aa23fb1475338cf467e7afb5732b8b9e456bbb3ad63c14224d73232d920457e" }, "nbformat": 3, "nbformat_minor": 0, @@ -28,8 +29,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of acentric factor\n", - "\n", + " \n", "import math\n", "\n", "# Variables\n", @@ -71,8 +71,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of acentric factor\n", - "\n", + " \n", "# Variables\n", "\t\t\t#math.log10(Psat)=8.1122-(1592.864/(t+226.184))\t\t\t# 'Psat' in [mm Hg] and 't' in [c]\n", "Tc = 513.9;\t\t\t#[K] - Critical temperature\n", @@ -116,8 +115,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of virial coefficients\n", - "\n", + " \n", "# Variables\n", "T = 380;\t\t\t#[K] - Temperature\n", "Tc = 562.1;\t\t\t#[K] - Critical temperature\n", @@ -173,8 +171,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of mass using virial equation of state\n", - "\n", + " \n", "# Variables\n", "V_1 = 0.3;\t\t\t#[m**(3)]\t\t\t#volume of cylinder\n", "T = 60+273.15;\t\t\t#[K] - Temperature\n", @@ -234,8 +231,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of molar volume\n", - "\n", + " \n", "# Variables\n", "T = 373.15;\t\t\t#[K] - Temperature\n", "P = 101325;\t\t\t#[N/m**(2)] - Pressure\n", @@ -288,8 +284,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of molar volume and virial coefficients\n", - "\n", + " \n", "# Variables\n", "T = 50+273.15;\t\t\t#[K] - Temperature\n", "P = 15*10**(5)\t\t\t#[N/m**(2)] - Pressure\n", @@ -405,9 +400,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of second and third virial coefficients\n", - "\n", - "# Variables\n", + " \n", "T = 0 + 273.15;\t\t\t#[K] - Temperature\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", "from numpy import linalg,array\n", @@ -464,9 +457,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of second virial coefficient\n", - "\n", - "# Variables\n", + " \n", "T = 444.3;\t\t\t#[K] - Temperature\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", "B_11 = -8.1;\t\t\t#[cm**(3)/mol]\n", @@ -532,9 +523,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of molar volume\n", - "\n", - "# Variables\n", + " \n", "T = 71+273.15;\t\t\t#[K] - Temperature\n", "P = 69*10**(5)\t\t\t#[N/m**(2)] - Pressure\n", "y1 = 0.5;\t\t\t#[mol] - mole fraction of equimolar mixture\n", @@ -625,9 +614,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of maximum temperature\n", - "\n", - "# Variables\n", + " \n", "P = 6.*10**(6)\t\t\t# [Pa] - Pressure\n", "P_max = 12.*10**(6)\t\t\t# [Pa] - Max pressure to which cylinder may be math.exposed\n", "T = 280.;\t\t\t#[K] - Temperature\n", @@ -755,10 +742,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure\n", - "\n", - "# Variables\n", - "\n", + " \n", "V_vessel = 0.1;\t\t\t#[m**(3)]\t\t\t# Volume of vessel\n", "T = 25 + 273.15;\t\t#[K] - Temperature\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", @@ -815,9 +799,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure\n", - "\n", - "# Variables\n", + " \n", "\n", "V_vessel = 360*10**(-3)\t\t\t#[m**(3)] - volume of vessel\n", "T = 62+273.15;\t\t\t#[K] - Temperature\n", @@ -905,9 +887,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of compressibility factor\n", - "\n", - "# Variables\n", + " \n", "T = 500+273.15;\t\t\t#[K] - Temperature\n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", "P = 325*1000;\t\t\t#[Pa] - Pressure\n", @@ -981,8 +961,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of molar volume\n", - "\n", + " \n", "from scipy.optimize import fsolve\n", "\n", "\n", @@ -1054,8 +1033,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of volume\n", - "\n", + " \n", "# Variables\n", "T = 500+273.15;\t\t\t#[K] - Temperature\n", "P = 15.;\t\t\t#[atm] - Pressure\n", @@ -1173,8 +1151,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of compressibility factor\n", - "\n", + " \n", "# Variables\n", "T = 310.93;\t\t\t#[K] - Temperature\n", "P = 2.76*10**(6)\t\t\t#[N/m**(2)] - Pressure\n", diff --git a/Chemical_Engineering_Thermodynamics/ch3_2.ipynb b/Chemical_Engineering_Thermodynamics/ch3_2.ipynb index dd655676..1dbe2b34 100644 --- a/Chemical_Engineering_Thermodynamics/ch3_2.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch3_2.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:8255c3a74c7b52da7fb922c8e6e009ed3e07e5e50a88f1302c38a2c832cbdc1f" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of temperature\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "\n", @@ -149,8 +149,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of heat required\n", - "\n", + " \n", "import math\n", "\n", "# Variables\n", @@ -208,8 +207,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of temperature internal energy and enthalpy\n", - "\n", + " \n", "# Variables\n", "M_vap_sat = 0.22;\t\t\t#[kg] - mass of saturated vapour\n", "M_liq_sat = 1.78;\t\t\t#[kg] - mass of saturated liquid\n", @@ -283,8 +281,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "from scipy.integrate import quad \n", @@ -369,8 +366,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done\n", - "\n", + " \n", "# Variables\n", "\n", "T = 300;\t\t\t#[K] - Temperature\n", @@ -491,8 +487,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done\n", - "\n", + " \n", "# Variables\n", "T = 125+273.15;\t\t\t#[K] - Temperature\n", "P1 = 1;\t\t\t#[bar] - Initial pressure\n", @@ -654,9 +649,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done\n", - "\n", - "# Variables\n", + " \n", "T = 20 + 273.15;\t\t\t#[K] - Temperature\n", "P_1 = 140.;\t\t\t#[kPa] - Initial pressure\n", "P_1 = P_1*10.**(3);\t\t\t#[Pa]\n", @@ -723,9 +716,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final temperature\n", - "\n", - "# Variables\n", + " \n", "m_ice = 1000;\t\t\t#[g] - Mass of ice\n", "m_water = 1000;\t\t\t#[g] - Mass of water\n", "T_ice = 273.15;\t\t\t#[K] - Temperature of ice\n", @@ -790,8 +781,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final pressure\n", - "\n", + " \n", "# Variables\n", "n = 1.5;\t\t\t# - ratio of heat capacities\n", "T_1 = 500.;\t\t\t#[K] - Initial temperature\n", @@ -852,9 +842,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of slope and work done\n", - "\n", - "# Variables\n", + " \n", "P_1 = 150*10**(3);\t\t\t#[Pa] - Initial pressure\n", "V_1 = 0.001;\t\t\t#[m**(3)] - Initial volume\n", "P_2 = 1000*10**(3);\t\t\t#[Pa] - Final pressure\n", @@ -914,9 +902,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done and final temperature\n", - "\n", - "# Variables\n", + " \n", "V = 36;\t\t\t#[L] - Vol of gas on each side\n", "P_1 = 1;\t\t\t#[atm] - pressure on left side of the piston\n", "P_1 = P_1*101325;\t\t\t#[Pa]\n", @@ -1001,9 +987,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of powerand discharge head\n", - "\n", - "# Variables\n", + " \n", "P_2 = 0.2;\t\t\t#[bar]\n", "P_2 = P_2*10**(5);\t\t\t#[Pa]\n", "int_dia_2 = 2.4*10**(-2);\t\t\t#[m] - internal diameter at state 2.\n", @@ -1059,9 +1043,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of discharge velocity\n", - "\n", - "# Variables\n", + " \n", "T_1 = 1000.;\t\t\t#[K] - Temperature at entry\n", "P_1 = 0.6;\t\t\t#[MPa] - Pressure at entry\n", "P_2 = 0.2;\t\t\t#[MPa] - Exit pressure\n", @@ -1117,9 +1099,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of change in enthalpy\n", - "\n", - "# Variables\n", + " \n", "P_entry = 10;\t\t\t#[bar] - Pressure at entry\n", "V_entry = 200;\t\t\t#[m/s] - Velocity at entry\n", "P_exit = 1;\t\t\t#[bar] - Vressure at exit\n", @@ -1162,9 +1142,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done and change in enthalpy\n", - "\n", - "# Variables\n", + " \n", "T_1 = 280;\t\t\t#[K] - Temperature at entry\n", "P_1 = 100;\t\t\t#[kPa] - Pressure at entry\n", "T_2 = 400;\t\t\t#[K] - Temperature at exit\n", @@ -1226,9 +1204,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done per unit mass\n", - "\n", - "# Variables\n", + " \n", "T_1 = 300;\t\t\t#[K] - Temperature at entry\n", "P_1 = 100;\t\t\t#[kPa] - Pressure at entry\n", "P_2 = 900;\t\t\t#[kPa] - Pressure at exit\n", @@ -1296,9 +1272,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of inlet and outlet velocity and power\n", - "\n", - "# Variables\n", + " \n", "T_1 = 600;\t\t\t#[C] - Temperature at entry\n", "P_1 = 15;\t\t\t#[MPa] - Pressure at entry\n", "T_2 = 400;\t\t\t#[K] - Temperature at exit\n", @@ -1360,9 +1334,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Proving a mathematical relation\n", - "\n", - "# Variables,\n", + " \n", "R = 8.314;\t\t\t#[J/mol-K] - Universal gas constant\n", "Cp_0 = 2.5*R;\t\t\t#[J/mol-K] - Specific heat capacity at constant pressure\n", "Cv_0 = 1.5*R;\t\t\t#[J/mol-K] - Specific heat capacity at constant volume\n", @@ -1403,9 +1375,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of equilibrium temperature\n", - "\n", - "# Variables\n", + " \n", "T_1 = 40 + 273.15;\t\t\t#[K] - Initial temperature.\n", "P_1 = 1;\t\t\t#[bar] - Initial pressure.\n", "P_1 = P_1*10**(5);\t\t\t#[Pa]\n", @@ -1474,9 +1444,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of mass\n", - "\n", - "# Variables\n", + " \n", "V_total = 5;\t\t\t#[L] - Volume of pressure cooker.\n", "V_total = V_total*10**(-3);\t\t\t#m**(3)\n", "P_gauze = 15;\t\t\t#[psi] - Operating pressure (gauze)of pressure cooker.\n", diff --git a/Chemical_Engineering_Thermodynamics/ch4_2.ipynb b/Chemical_Engineering_Thermodynamics/ch4_2.ipynb index 2e333961..52c2044d 100644 --- a/Chemical_Engineering_Thermodynamics/ch4_2.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch4_2.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:8185298e7063d37f738c422b0f9a0946dd677189cdf544f54e436d8d650cb521" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of entropy change\n", - "\n", + " \n", "import math\n", "\n", "# Variables\n", @@ -117,8 +117,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of whether the process is reversible or not\n", - "\n", + " \n", "# Variables\n", "T = 400.;\t\t\t#[K] - Temperature\n", "P_1 = 500.*10**(3);\t\t\t#[Pa] - Initial pressure\n", @@ -184,9 +183,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final pressure temperature and increase in entropy\n", - "\n", - "# Variables\n", + " \n", "R = 8.314;\t\t\t#[J/mol*K] - Universal gas constant\n", "\t\t\t# For side A\n", "V_A = 1;\t\t\t#[L] - Volume\n", @@ -261,9 +258,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# CAlculation of final temperature heat transfer and change of entropy\n", - "\n", - "# Variables\n", + " \n", "V_vessel = 0.2;\t\t\t#[m**(3)] - Volume of the vessel\n", "P_1 = 10;\t\t\t#[bar] - Initial pressure inside the vessel\n", "P_1 = P_1*10**(5);\t\t\t#[Pa]\n", @@ -358,8 +353,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final temperature work and heat transfer\n", - "\n", + " \n", "from math import *\n", "# Variables\n", "m = 1000.;\t\t\t#[g] - Mass of fluid\n", @@ -477,8 +471,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final temperature and work done\n", - "\n", + " \n", "# Variables\n", "m = 1000;\t\t\t#[g] - Mass of fluid\n", "P_1 = 20;\t\t\t#[bar] - Initial pressure\n", @@ -556,8 +549,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of index of isentropic expansion\n", - "\n", + " \n", "# Variables\n", "P_1 = 15.;\t\t\t#[bar] - Initial pressure\n", "P_2 = 0.15;\t\t\t#[bar] - Final pressure\n", @@ -622,9 +614,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of entropy production\n", - "\n", - "# Variables\n", + " \n", "P_1 = 40;\t\t\t#[bar] - Initial pressure\n", "T_1 = 500;\t\t\t#[C] - Initial temperature\n", "Vel_1 = 140;\t\t\t#[m/s] - Initial velocity\n", @@ -692,9 +682,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of work required and exit temperature\n", - "\n", - "# Variables\n", + " \n", "P_1 = 1.;\t\t\t#[MPa] - Initial pressure\n", "T_1 = 200 + 273.15;\t\t\t#[K] - Initial temperature\n", "P_2 = 8.;\t\t\t#[MPa] - Final pressure\n", @@ -757,8 +745,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of work required and exit temperature\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "from scipy.integrate import quad \n", @@ -847,8 +834,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of work required and exit temperature\n", - "\n", + " \n", "# Variables\n", "P_1 = 1;\t\t\t#[MPa] - Initial pressure\n", "T_1 = 200 + 273.15;\t\t\t#[K] - Initial temperature\n", @@ -934,9 +920,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of work required and discharge temperature\n", - "\n", - "# Variables\n", + " \n", "P_1 = 140.;\t\t\t#[kPa] - Initial pressure\n", "T_1 = 20. + 273.15;\t\t\t#[K] - Initial temperature\n", "P_2 = 560.;\t\t\t#[kPa] - Final pressure\n", @@ -1021,9 +1005,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Dtermination of power output entropy and exit temperature\n", - "\n", - "# Variables\n", + " \n", "P_1 = 10;\t\t\t#[bar] - Initial pressure\n", "T_1 = 500 + 273.15;\t\t\t#[K] - Initial temperature\n", "P_2 = 2;\t\t\t#[psia] - Final pressure\n", @@ -1135,9 +1117,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work output per unit mass\n", - "\n", - "# Variables\n", + " \n", "P_1 = 6;\t\t\t#[MPa] - Initial pressure\n", "T_1 = 500 + 273.15;\t\t\t#[K] - Initial temperature\n", "P_2 = 10;\t\t\t#[kPa] - Final pressure\n", @@ -1231,9 +1211,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of final velocity\n", - "\n", - "# Variables\n", + " \n", "P_1 = 3.;\t\t\t#[bar] - Initial pressure\n", "T_1 = 150. + 273.15;\t\t\t#[K] - Initial temperature\n", "Vel_1 = 90.;\t\t\t#[m/s] - Initial velocity\n", @@ -1312,8 +1290,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of final velocity and increase in entropy\n", - "\n", + " \n", "# Variables\n", "P_1 = 300.;\t\t\t#[kPa] - Initial pressure\n", "T_1 = 450.;\t\t\t#[K] - Initial temperature\n", @@ -1387,9 +1364,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done and heat transfer\n", - "\n", - "# Variables\n", + " \n", "P_1 = 1;\t\t\t#[bar] - Initial pressure\n", "T_1 = 150 + 273.15;\t\t\t#[K] - Initial temperature\n", "V_2 = 0.28;\t\t\t#[m**(3)/kg] - Final specific volume\n", @@ -1474,9 +1449,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of air velocity and change in entropy\n", - "\n", - "# Variables\n", + " \n", "P_1 = 7*10**(5);\t\t\t#[Pa] - Initial pressure\n", "T_1 = 95 + 273.15;\t\t\t#[K] - Initial temperature\n", "P_2 = 3.5*10**(5);\t\t\t#[Pa] - Final pressure\n", diff --git a/Chemical_Engineering_Thermodynamics/ch5_2.ipynb b/Chemical_Engineering_Thermodynamics/ch5_2.ipynb index db8558ce..82489a66 100644 --- a/Chemical_Engineering_Thermodynamics/ch5_2.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch5_2.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:beb354ab1f11a4413c580f54f984be6db9b7dd2c39bed82bc1f4874533d75759" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of fraction of the availability loss\n", - "\n", + " \n", "import math\n", "\n", "# Variables\n", @@ -76,8 +76,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of availability change and irreversibility\n", - "\n", + " \n", "# Variables\n", "T_1 = 300.;\t\t\t#[K] - Initial temperature.\n", "P_1 = 100.;\t\t\t#[kPa] - Initial pressure.\n", @@ -143,8 +142,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of availability change and irreversibility\n", - "\n", + " \n", "import math\n", "# Variables\n", "P_1 = 15.;\t\t\t#[bar] - Initial pressure\n", @@ -296,9 +294,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of useful work and irreversibility\n", - "\n", - "# Variables\n", + " \n", "T_1 = 150+273.15;\t\t\t#[K] - Initial temperature.\n", "m = 4.6;\t\t\t#[kg] - mass of water\n", "P_1 = 1;\t\t\t#[MPa] - Initial pressure\n", @@ -380,9 +376,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of reversible work and irreversibility\n", - "\n", - "# Variables\n", + " \n", "T_1 = 700+273.15;\t\t\t#[K] - Initial temperature.\n", "P_1 = 12;\t\t\t#[MPa] - Initial pressure\n", "P_2 = 0.6;\t\t\t#[MPa] - Final pressure\n", @@ -480,9 +474,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of maximum obtainable work and efficiency\n", - "\n", - "# Variables\n", + " \n", "P_1 = 8.;\t\t\t#[bar] - Initial pressure\n", "T_1 = 93. + 273.15;\t\t\t#[C] - Initial temperature\n", "V_1 = 100.;\t\t\t#[m/s] - Initial velocity\n", @@ -545,9 +537,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of entropy generation rate and irreversibility\n", - "\n", - "# Variables\n", + " \n", "m_cold_water = 60;\t\t\t#[kg/s] - mass flow rate of cold water\n", "P_1 = 50;\t\t\t#[kPa]\n", "T_2 = 250;\t\t\t#[C]\n", @@ -617,9 +607,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of exit temperature entropy and irreversibility rate\n", - "\n", - "# Variables\n", + " \n", "m_water = 10000.;\t\t\t#[kg/h] - Mass flow rate of cold water\n", "m_water = m_water/3600;\t\t\t#[kg/s]\n", "T_1_water = 30. + 273.15;\t\t\t#[K] - Cold water entering temperature\n", @@ -686,9 +674,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determinatio of exit temperature availability change and irreversibility\n", - "\n", - "# Variables\n", + " \n", "T_1_hotgas = 800.;\t\t\t#[K]\n", "P_1_hotgas = 1.;\t\t\t#[bar]\n", "T_2_hotgas = 700.;\t\t\t#[K]\n", diff --git a/Chemical_Engineering_Thermodynamics/ch6_2.ipynb b/Chemical_Engineering_Thermodynamics/ch6_2.ipynb index 301b4be1..71808e15 100644 --- a/Chemical_Engineering_Thermodynamics/ch6_2.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch6_2.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:5875fd58ba5a3eb4a34d80c6cbf01fc2219f223f8352a521a425e02950a18a26" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of enthalpy entropy and Gibbs free energy change of reaction\n", - "\n", + " \n", "import math \n", "from scipy.integrate import quad \n", "\t\t\t\n", @@ -131,9 +131,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of standard enthalpy and Gibbs free energy change of reaction\n", - "\n", - "# Variables\n", + " \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard temperature\n", "T_2 = 400;\t\t\t#[K] - Reaction temperature\n", "\n", @@ -220,9 +218,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of standard enthalpy and Gibbs free energy change of reaction\n", - "\n", - "# Variables\n", + " \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard temperature\n", "T_2 = 1200;\t\t\t#[K] - Reaction temperature\n", "\n", @@ -316,9 +312,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of standard enthalpy and Gibbs free energy change of reaction\n", - "\n", - "# Variables\n", + " \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard temperature\n", "T_2 = 500;\t\t\t#[K] - Reaction temperature\n", "\n", @@ -402,10 +396,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of standard enthalpy and Gibbs free energy change of reaction\n", - "\n", - "# Variables\n", - "\t\t\t#Cp_0 = 7.7 + 0.04594*10**(-2)*T + 0.2521*10**(-5)*T**(2) - 0.8587*10**(-9)*T**(3)\n", + " \n", "\n", "delta_H_rkn_298 = -57.7979*10**(3);\t\t\t#[cal/mol] - Reaction enthalpy at 298.15 K\n", "delta_G_rkn_298 = -54.6351*10**(3);\t\t\t#[cal/mol] - Gibbs free energy change for formation of H2O at 298.15 K\n", @@ -486,9 +477,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of heat exchange\n", - "\n", - "# Variables\n", + " \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard temperature\n", "T_2 = 500.;\t\t\t#[K] - Reaction temperature\n", "\n", @@ -563,9 +552,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of change in entropy\n", - "\n", - "# Variables\n", + " \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard temperature\n", "T_2 = 600.;\t\t\t#[K] - Reaction temperature\n", "\n", @@ -638,9 +625,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of standard enthalpy change and Gibbs free energy change\n", - "\n", - "# Variables\n", + " \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard temperature\n", "T_2 = 973.15;\t\t\t#[K] - Reaction temperature\n", "\n", @@ -715,9 +700,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of standard enthalpy change and Gibbs free energy change\n", - "\n", - "# Variables\n", + " \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard temperature\n", "T_2 = 1000;\t\t\t#[K] - Reaction temperature\n", "\n", @@ -796,9 +779,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of standard enthalpy change and Gibbs free energy change\n", - "\n", - "# Variables\n", + " \n", "T_1 = 298.15;\t\t\t#[K] - Smath.tan(math.radiansard temperature\n", "T_2 = 1042;\t\t\t#[K] - Reaction temperature\n", "\n", diff --git a/Chemical_Engineering_Thermodynamics/ch7_2.ipynb b/Chemical_Engineering_Thermodynamics/ch7_2.ipynb index 11e9b4cd..dae2b7f0 100644 --- a/Chemical_Engineering_Thermodynamics/ch7_2.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch7_2.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:1fc4ec5605309ff88ba6d75ddff6c3046fc8a8dc45dca2d12f7651c49812921e" }, "nbformat": 3, "nbformat_minor": 0, @@ -27,8 +28,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of entropy change\n", - "\n", + " \n", "import math \n", "\n", "\n", @@ -81,8 +81,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of work done\n", - "\n", + " \n", "import math \n", "from scipy.integrate import quad \n", "\t\t\t\n", @@ -161,8 +160,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Evaluation of beta and K for nitrogen gas\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "\n", "\n", @@ -226,9 +224,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of temperature change and entropy change of water\n", - "\n", - "# Variables\n", + " \n", "T = 45+273.15;\t\t\t#[K]\n", "P_1 = 10;\t\t\t#[kPa] - Initial pressure\n", "P_2 = 8600;\t\t\t#[kPa] - Final pressure\n", @@ -300,9 +296,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of change in entropy and enthalpy\n", - "\n", - "# Variables\n", + " \n", "T = 270;\t\t\t#[K]\n", "P_1 = 381;\t\t\t#[kPa] - Initial pressure\n", "P_2 = 1200;\t\t\t#[kPa] - Final pressure\n", @@ -353,8 +347,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of percentage change in volume\n", - "\n", + " \n", "# Variables\n", "T_1 = 0;\t\t\t#[C] - Initial tempetaure\n", "T_2 = 100;\t\t\t#[C] - Final temperature\n", @@ -404,9 +397,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of enthalpy and entropy change\n", - "\n", - "# Variables\n", + " \n", "T_1 = 25 + 273.15;\t\t\t#[C] - Initial tempetaure\n", "T_2 = 50 + 273.15;\t\t\t#[C] - Final temperature\n", "P_1 = 1;\t\t\t#[bar] - Initial pressure\n", @@ -479,8 +470,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "#Calculation of volume expansivity and isothermal compressibility\n", - "\n", + " \n", "# Variables\n", "T = 100 + 273.15;\t\t\t#[K]\n", "P = 10;\t\t\t#[MPa]\n", @@ -535,8 +525,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of specific heat capacity\n", - "\n", + " \n", "# Variables\n", "T = 300 + 273.15;\t\t\t#[K]\n", "P = 4;\t\t\t#[MPa] \n", @@ -589,9 +578,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of specific heat capacity\n", - "\n", - "# Variables\n", + " \n", "T = 300 + 273.15;\t\t\t#[K]\n", "P = 2.0;\t\t\t#[MPa]\n", "\n", @@ -632,9 +619,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of volume expansivity and isothermal compressibility\n", - "\n", - "# Variables\n", + " \n", "T = 80 + 273.15;\t\t\t#[K]\n", "P = 10;\t\t\t#[MPa] \n", "\n", @@ -699,8 +684,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of mean Joule Thomson coefficient\n", - "\n", + " \n", "# Variables\n", "P_1 = 150;\t\t\t#[bar]\n", "P_2 = 1;\t\t\t#[bar]\n", @@ -771,8 +755,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of Joule Thomson coefficient\n", - "\n", + " \n", "# Variables\n", "T = 300;\t\t\t#[K] - Temperature\n", "P = 5;\t\t\t#[atm] - Pressure\n", @@ -825,8 +808,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of pressure\n", - "\n", + " \n", "# Variables\n", "den_liq = 13690.;\t\t\t#[kg/m**(3)] - Density of liquid mercury\n", "den_solid = 14190.;\t\t\t#[kg/m**(3)] - Density of solid mercury\n", @@ -878,8 +860,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of enthalpy change and entropy change\n", - "\n", + " \n", "# Calculations and Results\n", "\t\t\t#(1)\n", "\t\t\t# At 1 bar\n", @@ -932,8 +913,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of ratio of temperature change and pressure change\n", - "\n", + " \n", "# Variables\n", "H_fus = 80;\t\t\t#[cal/g] - Heat of fusion at 0 C and 1 atm pressure\n", "T = 0+273.15;\t\t\t#[K] - Temperature\n", @@ -975,7 +955,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of boiling point of water\n", + " \n", "\n", "# Variables\n", "P = 2;\t\t\t#[atm] - Surrounding pressure\n", @@ -1025,8 +1005,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of enthalpy and entropy of vaporization of water\n", - "\n", + " \n", "# Variables\n", "T_1 = 0.01 +273.15;\t\t\t#[K]\n", "T_2 = 1 + 273.15;\t\t\t#[K]\n", @@ -1075,7 +1054,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of heat of vaporization of water\n", + " \n", "\n", "# Variables\n", "T = 100. + 273.15;\t\t\t#[K]\n", @@ -1129,7 +1108,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of latent heat of vaporization\n", + " \n", "\n", "# Variables\n", "T_1 = 100 + 273.15;\t\t\t#[K]\n", @@ -1189,7 +1168,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of temperature dependence\n", + " \n", "from scipy.integrate import quad \n", "from scipy.optimize import *\n", "\n", @@ -1292,8 +1271,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of fugacity of water\n", - "\n", + " \n", "# Variables\n", "T = 300 + 273.15;\t\t\t#[K] - Temperature\n", "P = 9000;\t\t\t#[kPa] - Pressure\n", @@ -1340,7 +1318,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of fugacity of saturated steam\n", + " \n", "\n", "# Variables\n", "T = 200 + 273.15;\t\t\t#[K] - Temperature\n", @@ -1401,7 +1379,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Estimation of fugacity of steam\n", + " \n", "\n", "# Variables\n", "T = 320 + 273.15;\t\t\t#[K]\n", @@ -1509,7 +1487,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of fugacities at two states\n", + " \n", "\n", "# Variables\n", "T = 300 + 273.15;\t\t\t#[K]\n", diff --git a/Chemical_Engineering_Thermodynamics/ch8_2.ipynb b/Chemical_Engineering_Thermodynamics/ch8_2.ipynb index e4dd389d..6b83d68c 100644 --- a/Chemical_Engineering_Thermodynamics/ch8_2.ipynb +++ b/Chemical_Engineering_Thermodynamics/ch8_2.ipynb @@ -1,6 +1,7 @@ { "metadata": { - "name": "" + "name": "", + "signature": "sha256:8df6804e24ffba947b26128cacd98ede56f82be4a3089c7567d672249f51ebda" }, "nbformat": 3, "nbformat_minor": 0, @@ -28,8 +29,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of work done\n", - "\n", + " \n", "import math\n", "\n", "# Variables\n", @@ -144,9 +144,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of efficiency of Rankine cycle\n", - "\n", - "# Variables\n", + " \n", "T_max = 700+273.15;\t\t\t#[K] - Maximum temperature.\n", "P_boiler = 10*10**(6);\t\t\t#[Pa] - Constant pressure in the boiler\n", "P_condenser = 10*10**(3);\t\t\t#[Pa] - Constant pressure in the condenser\n", @@ -226,9 +224,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculatrion of COP of carnot refrigerator and heat rejected\n", - "\n", - "# Variables\n", + " \n", "W = 1.1;\t\t\t#[kW] - Work done per ton of refrigeration \n", "\t\t\t#1 ton refrigeration = 3.517 kW, therefore\n", "H = 3.517;\t\t\t#[kW] - Heat absorbed\n", @@ -277,9 +273,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of minimum power required\n", - "\n", - "# Variables\n", + " \n", "T_high = 20 + 273.15;\t\t\t#[K] - High temperature\n", "T_low = 0 + 273.15;\t\t\t#[K] - Low temperature\n", "Q_H = 10;\t\t\t#[kW] - Heat supplied\n", @@ -320,9 +314,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of COP and power required\n", - "\n", - "# Variables\n", + " \n", "T_high = 40 + 273.15;\t\t\t#[K] - High temperature\n", "T_low = -20 + 273.15;\t\t\t#[K] - Low temperature\n", "C = 10;\t\t\t#[tons of refrigeration] - Capacity\n", @@ -366,9 +358,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of maximum refrigeration effect\n", - "\n", - "# Variables\n", + " \n", "COP = 4;\t\t\t#Coefficient of performance\n", "P = 10;\t\t\t#[kW] - Work done on the cycle\n", "\n", @@ -412,9 +402,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of refrigeration effect power consumed and COP of refrigerator\n", - "\n", - "# Variables\n", + " \n", "m = 0.6;\t\t\t#[kg/s] - mass flow rate\n", "T_low = -20+273.15;\t\t\t#[K] - Temperature at which vapour enters the compressor\n", "T_high = 30+273.15;\t\t\t#[K] - Temperature at which vapour leaves the condenser\n", @@ -527,8 +515,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of amount of air\n", - "\n", + " \n", "from scipy.optimize import fsolve \n", "import math \n", "\t\t\n", @@ -601,8 +588,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Calculation of amount of air and temperature\n", - "\n", + " \n", "# Variables\n", "\t\t\t#At 1 bar, 310 K \n", "H_1 = 310.38;\t\t\t#[kJ/kg]\n", @@ -702,9 +688,7 @@ "cell_type": "code", "collapsed": false, "input": [ - "# Determination of temperature of air\n", - "\n", - "# Variables\n", + " \n", "P_high = 40;\t\t\t#[bar]\n", "P_low = 5;\t\t\t#[bar]\n", "m_1 = 0.5;\t\t\t#[kg/s] - Rate of mass moving through the expander\n", |