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| author | hardythe1 | 2015-04-07 15:58:05 +0530 |
|---|---|---|
| committer | hardythe1 | 2015-04-07 15:58:05 +0530 |
| commit | c7fe425ef3c5e8804f2f5de3d8fffedf5e2f1131 (patch) | |
| tree | 725a7d43dc1687edf95bc36d39bebc3000f1de8f /Thermodynamics_An_Engineering_Approach/Chapter3.ipynb | |
| parent | 62aa228e2519ac7b7f1aef53001f2f2e988a6eb1 (diff) | |
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diff --git a/Thermodynamics_An_Engineering_Approach/Chapter3.ipynb b/Thermodynamics_An_Engineering_Approach/Chapter3.ipynb new file mode 100755 index 00000000..9830dbfb --- /dev/null +++ b/Thermodynamics_An_Engineering_Approach/Chapter3.ipynb @@ -0,0 +1,756 @@ +{
+ "metadata": {
+ "name": ""
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+ {
+ "cells": [
+ {
+ "cell_type": "heading",
+ "level": 1,
+ "metadata": {},
+ "source": [
+ "Chapter 3: Properties of Pure Substances"
+ ]
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-1 ,Page No.128"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Given values\n",
+ "m=50;#mass in kg\n",
+ "T=90;#temperature in C\n",
+ "\n",
+ "#Values from Table A-4\n",
+ "P=70.183;#in kPa\n",
+ "v=0.001036;#in m^3/kg\n",
+ "\n",
+ "#Calculation\n",
+ "V=m*v;#equating dimensions\n",
+ "print'pressure is %f kPa'%round(P,3);\n",
+ "print'total volumne of tank becomes %f m^3'%round(V,4)\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "pressure is 70.183000 kPa\n",
+ "total volumne of tank becomes 0.051800 m^3\n"
+ ]
+ }
+ ],
+ "prompt_number": 2
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-2 ,Page No.128"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Given values\n",
+ "V=2.0;#volumne of saturated water vapor in ft^3\n",
+ "P=50.0;#pressure in psia\n",
+ "\n",
+ "#Values from Table A-5E\n",
+ "T=280.99;#in F\n",
+ "v=8.5175;#in ft^3/lbm\n",
+ "\n",
+ "#caluclation\n",
+ "m=V/v;#dimension analysis\n",
+ "print'Temperature inside cylinder %f F'%round(T,2);\n",
+ "print'mass of vapour inside cylinder %f lbm'%round(m,3);\n",
+ "\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Temperature inside cylinder 280.990000 F\n",
+ "mass of vapour inside cylinder 0.235000 lbm\n"
+ ]
+ }
+ ],
+ "prompt_number": 1
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-3 ,Page No.128"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Constants used\n",
+ "Hfg=2257.5;#enthalpy of vaporization in kJ/kg\n",
+ "\n",
+ "#Given values\n",
+ "m=200.0/1000;#mass converting in kg\n",
+ "P=100;#Pressure at which process takes place in kPa\n",
+ "\n",
+ "#Values from Table A-5\n",
+ "vg=1.6941;#specific vol of sat liq\n",
+ "vf=0.001043;#specific vol of vapor\n",
+ "\n",
+ "#Caluclation\n",
+ "vfg=vg-vf;\n",
+ "V=m*vfg;\n",
+ "print'the volume change %f m^3'%round(V,4);\n",
+ "E=m*Hfg;\n",
+ "print'amount of energy transferred to the water %f kJ'%round(E,1)\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "the volume change 0.338600 m^3\n",
+ "amount of energy transferred to the water 451.500000 kJ\n"
+ ]
+ }
+ ],
+ "prompt_number": 4
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-4 ,Page No.131"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Given values\n",
+ "mt=10#mass of water in kg\n",
+ "mf=8;#mass of water in liquid form in kg\n",
+ "T=90;#temperature in C\n",
+ "\n",
+ "#Values from Table A-4\n",
+ "P=70.183;#in kPa\n",
+ "vf=0.001036;#in m^3\n",
+ "vg=2.3593;#in m^3\n",
+ "\n",
+ "#Caluclation\n",
+ "mg=mt-mf;\n",
+ "V=mf*vf+mg*vg;# V= Vg + Vf\n",
+ "print'the volume of the tank %f m^3'%round(V,2);\n",
+ "print'the pressure in the tank %f kPa'%round(P,3)\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "the volume of the tank 4.730000 m^3\n",
+ "the pressure in the tank 70.183000 kPa\n"
+ ]
+ }
+ ],
+ "prompt_number": 5
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-5 ,Page No.131"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Given values\n",
+ "m=4;#mass of refrigerant-134a in kg\n",
+ "V=80.0/1000;#volumne converting into m^3\n",
+ "P=160;#pressure in kPa\n",
+ "\n",
+ "#Values from Table A-12\n",
+ "vf=0.0007437;\n",
+ "vg=0.12348;\n",
+ "T=-15.60;\n",
+ "hf=31.21;\n",
+ "hfg=209.90;\n",
+ "\n",
+ "#Caluclations\n",
+ "v=V/m;\n",
+ "#vg>v>vf therefore it is a saturated mix\n",
+ "#hence temp will same as saturation temp\n",
+ "print'the temperature %f celcius'%round(T,2)\n",
+ "x=(v-vf)/(vg-vf);#x=vg/vfg i.e the dryness fraction\n",
+ "print'the quality is %f'%round(x,3);\n",
+ "h=hf+x*hfg;\n",
+ "print'the enthalpy of the refrigerant %f kJ/kg'%round(h,1);\n",
+ "mg=x*m;\n",
+ "Vg=mg*vg;\n",
+ "print'the volume occupied by the vapor phase %f m^3'%round(Vg,4)\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "the temperature -15.600000 celcius\n",
+ "the quality is 0.157000\n",
+ "the enthalpy of the refrigerant 64.100000 kJ/kg\n",
+ "the volume occupied by the vapor phase 0.077500 m^3\n"
+ ]
+ }
+ ],
+ "prompt_number": 1
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-7 ,Page No.133"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Given values\n",
+ "P=0.5;#pressure in MPa\n",
+ "h=2890.0;#enthaply in kJ/kg\n",
+ "\n",
+ "#from Table A\u20136\n",
+ "#at P=0.5 MPa\n",
+ "T1=200.0;\n",
+ "h1=2855.8;\n",
+ "T2=250;\n",
+ "h2=2961.0;\n",
+ "# we need linear interpolation \n",
+ "\n",
+ "#calculatiom\n",
+ "#by interpolation we can say that\n",
+ "#h=h1+(T-T1)/(T2-T1)*(h2-h1)\n",
+ "#we have to find T\n",
+ "T=(h-h1)/(h2-h1)*(T2-T1)+T1;\n",
+ "print'temperature of water %f celcius'%round(T,1)\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "temperature of water 216.300000 celcius\n"
+ ]
+ }
+ ],
+ "prompt_number": 6
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-8 ,Page No.134"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Given values\n",
+ "T=80;#temperature of compressed liquid water in C\n",
+ "P=5;#pressure in KPa\n",
+ "\n",
+ "#from Table A\u20137\n",
+ "#at compressed liq given conditions\n",
+ "u=333.82;\n",
+ "\n",
+ "#from Table A-4\n",
+ "#at saturation\n",
+ "usat=334.97;\n",
+ "\n",
+ "#calcualtion\n",
+ "e=(usat-u)/u*100;\n",
+ "print'internal energy of compressed liquid water using data from the compressed liquid table %f kJ/kg '%round(u,2);\n",
+ "print'internal energy of compressed liquid water using saturated liquid data %f kJ/kg '%round(usat,2);\n",
+ "print'the error involved %f the second case'%round(e,2)\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "internal energy of compressed liquid water using data from the compressed liquid table 333.820000 kJ/kg \n",
+ "internal energy of compressed liquid water using saturated liquid data 334.970000 kJ/kg \n",
+ "the error involved 0.340000 the second case\n"
+ ]
+ }
+ ],
+ "prompt_number": 18
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-9 ,Page No.135"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#part a\n",
+ "print('Part a');\n",
+ "\n",
+ "#given values\n",
+ "P=200;#in KPa\n",
+ "x=0.6;\n",
+ "\n",
+ "#from Table A-5\n",
+ "T=120.21;\n",
+ "uf=504.50;\n",
+ "ufg=2024.6;\n",
+ "\n",
+ "#calcualtions\n",
+ "u=uf+(x*ufg);\n",
+ "print'temperature %f Celcius '%round(T,2);\n",
+ "print'internal energy %f kJ/kg'%round(u,2);\n",
+ "print('saturated liquid\u2013vapor mixture at a pressure of 200 kPa');\n",
+ "\n",
+ "#part b\n",
+ "print('Part b');\n",
+ "\n",
+ "#given values\n",
+ "T=125;#in C\n",
+ "u=1600;#in kJ/kg\n",
+ "\n",
+ "#from Table A\u20134\n",
+ "uf=524.83;\n",
+ "ug=2534.3;\n",
+ "#ug>u>ufg so its aturated liquid\u2013vapor mixture\n",
+ "P=232.23;\n",
+ "\n",
+ "#calculation\n",
+ "ufg=ug-uf;\n",
+ "x=(u-uf)/ufg;\n",
+ "print'Pressure %f kPa'%round(P,2);\n",
+ "print'x is %f'%round(x,3);\n",
+ "print('saturated liquid\u2013vapor mixture at a temp of 125 of celcius');\n",
+ "\n",
+ "#part c\n",
+ "print('Part c');\n",
+ "\n",
+ "#given values\n",
+ "P=1000;#in kPa\n",
+ "u=2950;#in kJ/kg\n",
+ "\n",
+ "#from Table A\u20136\n",
+ "uf=761.39;\n",
+ "ug=2582.8;\n",
+ "#u>ug so its superheated steam\n",
+ "T=395.2;\n",
+ "\n",
+ "#calculation\n",
+ "print'temperature %f Celcius'%round(T,1);\n",
+ "print('superheated vapor at 1MPa');\n",
+ "\n",
+ "#part d\n",
+ "print('Part d');\n",
+ "\n",
+ "#given values\n",
+ "T=75;#in C\n",
+ "P=100;#in kPa\n",
+ "\n",
+ "#from Table A\u20135\n",
+ "Tsat=151.83;\n",
+ "#T<Tsat so it is a compressed liquid\n",
+ "#the given pressure is much lower than the lowest pressure value in the compressed liquid table i.e 5 MPa\n",
+ "#assuming, the compressed liquid as saturated liquid at the given temperature\n",
+ "\n",
+ "#from Table A-4\n",
+ "u=313.99;\n",
+ "print'Internal energy %f kJ/kg'%round(u,2);\n",
+ "print('the compressed liquid condition');\n",
+ "\n",
+ "#Part e\n",
+ "print('Part e');\n",
+ "\n",
+ "#given values\n",
+ "P=850;#in kPa\n",
+ "x=0;\n",
+ "\n",
+ "#x=0 therefore it is a saturateed liquid condition\n",
+ "#from Table A-5\n",
+ "T=172.94;\n",
+ "u=731.00;\n",
+ "print'temperature %f Celcius'%round(T,2);\n",
+ "print'Internal energy %f kJ/kg'%round(u,2);\n",
+ "print('saturateed liquid condition')\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "Part a\n",
+ "temperature 120.210000 Celcius \n",
+ "internal energy 1719.260000 kJ/kg\n",
+ "saturated liquid\u2013vapor mixture at a pressure of 200 kPa\n",
+ "Part b\n",
+ "Pressure 232.230000 kPa\n",
+ "x is 0.535000\n",
+ "saturated liquid\u2013vapor mixture at a temp of 125 of celcius\n",
+ "Part c\n",
+ "temperature 395.200000 Celcius\n",
+ "superheated vapor at 1MPa\n",
+ "Part d\n",
+ "Internal energy 313.990000 kJ/kg\n",
+ "the compressed liquid condition\n",
+ "Part e\n",
+ "temperature 172.940000 Celcius\n",
+ "Internal energy 731.000000 kJ/kg\n",
+ "saturateed liquid condition\n"
+ ]
+ }
+ ],
+ "prompt_number": 7
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-10 ,Page No.139"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#constants used\n",
+ "R=0.287# in kPa m^3/kg K\n",
+ "\n",
+ "#given values\n",
+ "l=4;#dimensions of room in m\n",
+ "b=5;#dimensions of room in m\n",
+ "h=6;#dimensions of room in m\n",
+ "P=100.0;#pressure in kPa\n",
+ "T=25+273.0;#temperature in Kelvin\n",
+ "\n",
+ "#calculation\n",
+ "V=l*b*h;\n",
+ "m=P*V/R/T;\n",
+ "print'the mass of the air %f kg'%round(m,1)\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "the mass of the air 140.300000 kg\n"
+ ]
+ }
+ ],
+ "prompt_number": 23
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-11 ,Page No.142"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#given values\n",
+ "P=1;#pressure in MPa\n",
+ "T=50+273;#tempearture converting into Kelvin\n",
+ "vgiv=0.021796;#specific vol. given in m^3\n",
+ "\n",
+ "#from Table A-1\n",
+ "R=0.0815;\n",
+ "Pcr=4.059;\n",
+ "Tcr=374.2;\n",
+ "\n",
+ "#calculation\n",
+ "\n",
+ "#Part A\n",
+ "v1=R*T/(P*1000);\n",
+ "print'specific volume of refrigerant-134a under the ideal-gas assumption %fm^3/kg'%round(v1,6);\n",
+ "e=(v1-vgiv)/vgiv;\n",
+ "print'an error of %f'%round(e,3);\n",
+ "\n",
+ "#Part B\n",
+ "#determine Z from the compressibility chart, we will calculate the reduced pressure and temperature\n",
+ "Pr=P/Pcr;\n",
+ "Tr=T/Tcr;\n",
+ "#from chart\n",
+ "Z=0.84;\n",
+ "v=Z*v1;\n",
+ "print'specific volume of refrigerant-134a under the generalized compressibility chart %f m^3/kg'%round(v,6);\n",
+ "e=(v-vgiv)/vgiv;\n",
+ "print'an error of %f'%round(e,3);\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "specific volume of refrigerant-134a under the ideal-gas assumption 0.026325m^3/kg\n",
+ "an error of 0.208000\n",
+ "specific volume of refrigerant-134a under the generalized compressibility chart 0.022113 m^3/kg\n",
+ "an error of 0.015000\n"
+ ]
+ }
+ ],
+ "prompt_number": 8
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-12 ,Page No.143"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#given values\n",
+ "v=0.51431;\n",
+ "T=600;\n",
+ "\n",
+ "#from Table A-1E\n",
+ "R=0.5956;\n",
+ "Pcr=3200;\n",
+ "Tcr=1164.8;\n",
+ "\n",
+ "#calculation\n",
+ "\n",
+ "#Part A\n",
+ "#from Table A-6E\n",
+ "Pa=1000.0;#in psia\n",
+ "print'from the steam tables %i psia'%Pa;\n",
+ "\n",
+ "#Part B\n",
+ "T=1060;#converted into R from F\n",
+ "Pb=R*T/v;\n",
+ "print'from the ideal-gas equation %i psia'%round(Pb,0);\n",
+ "e=(Pb-Pa)/Pa;\n",
+ "print'treating the steam as an ideal gas would result in an error of %f'%round(e,3)\n",
+ "\n",
+ "#Part C\n",
+ "#calculating the pseudo-reduced specific volume and the reduced temperature\n",
+ "Vr=v/(R*Tcr/Pcr);\n",
+ "Tr=T/Tcr;\n",
+ "#from the compressibility chart\n",
+ "Pr=0.33;\n",
+ "P=Pr*Pcr;\n",
+ "print'from the generalized compressibility chart %i psia'%P\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "from the steam tables 1000 psia\n",
+ "from the ideal-gas equation 1228 psia\n",
+ "treating the steam as an ideal gas would result in an error of 0.228000\n",
+ "from the generalized compressibility chart 1056 psia\n"
+ ]
+ }
+ ],
+ "prompt_number": 12
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-13 ,Page No.147"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#Answer of part c-d are having slight difference due to approximation in molar volumne in the textbook which here is caluculated to the approximation of 7 decimal digits\n",
+ "\n",
+ "from math import exp\n",
+ "\n",
+ "#given values\n",
+ "T=175.0;#temperature in C\n",
+ "v=0.00375;#sp. volumne in m^3/kg\n",
+ "Pex=10000;#experimentaion determination\n",
+ "\n",
+ "#from Table A-1\n",
+ "R=0.2968# in kPa m^3/kg K\n",
+ "\n",
+ "#calculating\n",
+ "\n",
+ "#Part-a\n",
+ "P=R*T/v;\n",
+ "print'using the ideal-gas equation of state %i kPa'%(round(P))\n",
+ "e=(P-Pex)/Pex*100;\n",
+ "print'error is %f percent'%e;\n",
+ "\n",
+ "#Part-b\n",
+ "#van der Waals constants from Eq. 3-23\n",
+ "a=0.175;\n",
+ "b=0.00138;\n",
+ "#from van der waal eq.\n",
+ "P=R*T/(v-b)-a/v**2;\n",
+ "print'using the van der Waals equation of state is %i kPa'%(round(P));\n",
+ "e=(P-Pex)/Pex*100;\n",
+ "print'error is %f percent'%e;\n",
+ "\n",
+ "#Part-c\n",
+ "#constants in the Beattie-Bridgeman equation from Table 3\u20134\n",
+ "A=102.29;\n",
+ "B=0.05378;\n",
+ "c=4.2*10**4;\n",
+ "Ru=8.314;#in kPa m^3/kmol K\n",
+ "M=28.013;#molecular weight in kg/mol\n",
+ "vb=M*v;#molar vol.\n",
+ "P=(Ru*T)/(vb**2)*(1-((c)/(vb*T**3)))*(vb+B)-(A/vb**2);\n",
+ "print'using the Beattie-Bridgeman equationis %i kPa'%(round(P));\n",
+ "e=(P-Pex)/Pex*100;\n",
+ "print'error is %f percent'%e;\n",
+ "\n",
+ "#Part-d\n",
+ "#constants of Benedict-Webb-Rubin equation from Table 3\u20134\n",
+ "a=2.54;\n",
+ "b=0.002328;\n",
+ "c=7.379*10**4;\n",
+ "alp=1.272*10**-4;\n",
+ "Ao=106.73;\n",
+ "Bo=0.040704;\n",
+ "Co=8.164*10**5;\n",
+ "gam=0.0053;\n",
+ "P=((Ru*T)/vb)+((Bo*Ru*T)-Ao-Co/T**2)/vb**2+(b*Ru*T-a)/vb**3+(a*alp/vb**6)+(c/((vb**3)*(T**2)))*(1 + (gam/vb**2))*exp(-gam/vb**2);\n",
+ "print'using Benedict-Webb-Rubin equation %i kPa'%(round(P));\n",
+ "e=(P-Pex)/Pex*100;\n",
+ "print'error is %f percent'%e;\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "using the ideal-gas equation of state 13851 kPa\n",
+ "error is 38.506667 percent\n",
+ "using the van der Waals equation of state is 9471 kPa\n",
+ "error is -5.288326 percent\n",
+ "using the Beattie-Bridgeman equationis 10109 kPa\n",
+ "error is 1.092970 percent\n",
+ "using Benedict-Webb-Rubin equation 10004 kPa\n",
+ "error is 0.039256 percent\n"
+ ]
+ }
+ ],
+ "prompt_number": 14
+ },
+ {
+ "cell_type": "heading",
+ "level": 2,
+ "metadata": {},
+ "source": [
+ "Example 3-14 ,Page No.152"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "#given value\n",
+ "T=25;#air temperature over a lake in C\n",
+ "\n",
+ "#from table 3-1\n",
+ "Psat=3.17;#in kPa\n",
+ "\n",
+ "#calculations\n",
+ "\n",
+ "#Relative Humidity 10%\n",
+ "Pv1=0.1*Psat\n",
+ "#Relative Humidity 80%\n",
+ "Pv2=0.8*Psat\n",
+ "#Relative Humidity 100%\n",
+ "Pv3=1*Psat\n",
+ "\n",
+ "# from table 3-1 Tsat at these Pressures are\n",
+ "T1=-8.0;\n",
+ "T2=21.2;\n",
+ "T3=25.0;\n",
+ "print'with relative humidity 10, temperature is %i in C'%T1\n",
+ "print'with relative humidity 80, temperature is %i in C'%T2\n",
+ "print'with relative humidity 100, temperature is %i in C'%T3\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "with relative humidity 10, temperature is -8 in C\n",
+ "with relative humidity 80, temperature is 21 in C\n",
+ "with relative humidity 100, temperature is 25 in C\n"
+ ]
+ }
+ ],
+ "prompt_number": 15
+ }
+ ],
+ "metadata": {}
+ }
+ ]
+}
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