path: root/Elements_Of_Mass_Transfer_Part_1/ch5.ipynb

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   "cells": [
    {
     "cell_type": "heading",
     "level": 1,
     "metadata": {},
     "source": [
      "Chapter 5 : Humidification"
     ]
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.1 "
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "\n",
      "# Variable Declaration \n",
      "#dry bulb temperature=50  and  wet bulb temperature=35 \n",
      "Tg=50.;                    #dry bulb temperature=50\n",
      "To=0;                    #refrence temperature in degree celcius    \n",
      "Mb=28.84;                #average molecular weight of air\n",
      "Ma=18.;                   #average molecular weight of water\n",
      "\n",
      "#part(i)\n",
      "ybar=.0483                #0.003 kg of water vapour/kg of dry air\n",
      "print \"\\n the humidity(from chart) is  \\t\\t:%f  percent\"%ybar\n",
      "\n",
      "#part(ii)\n",
      "humper=35.;                #humidity percentage\n",
      "print \"\\n the percentage humidity is(from chart) :%f  percent\"%humper\n",
      "\n",
      "# Calculation and Result\n",
      "#part(iii)\n",
      "pt=1.013*10**5;            #total pressure in pascal\n",
      "molhum=0.0483;            #molal humidity =pa/(pt-pa)\n",
      "pa=molhum*pt/(1+molhum);\n",
      "#the vopour pressure of water(steam tables)at 50degree = .1234*10**5 N/m**2\n",
      "relhum=(pa/(.1234*10**5))*100;      #percentage relative humidity =partial pressure/vapour pressure\n",
      "print \"\\n the percentage relative humidity is \\t percent:%f  \"%relhum\n",
      "\n",
      "#part(iv)\n",
      "dewpoint=31.5;            #dew point temperature in degree celcius\n",
      "print \"\\n the dew point temperature \\t\\t :%f degree celcius\"%dewpoint\n",
      "\n",
      "#part(v)\n",
      "Ca=1.005;\n",
      "Cb=1.884;\n",
      "ybar=.03;                #saturation temperature inkg water vapour/kg dry air\n",
      "Cs=Ca+Cb*ybar;            #humid heat  in kj/kg dry air degree celcius\n",
      "print \"\\n we get humid heat as \\t\\t\\t :%f kj/kg dry air degree celcius \"%Cs\n",
      "\n",
      "#part(vi)\n",
      "d=2502;                    #latent heat in kj/kg\n",
      "H=Cs*(Tg-0)+ybar*d;        #enthalpy for refrence temperature of 0 degree\n",
      "print \"\\n we get H as \\t\\t\\t\\t :%f kj/kg\"%H\n",
      "Hsat=274.;                   #enthalpy of sturated air\n",
      "Hdry=50.;                   #enthalpy of dry air in kj/kg\n",
      "Hwet=Hdry+(Hsat-Hdry)*0.35;     #enthalpy of wet air in kj/kg\n",
      "print \"\\n we get enthalpy of wet air  as \\t:%f kj/kg\"%Hwet\n",
      "\n",
      "#part(vii)\n",
      "VH=8315*((1./Mb)+(ybar/Ma))*((Tg+273.)/pt);        #humid volume in m**3mixture/kg of dry air\n",
      "print \"\\n we get VH  as (a)\\t\\t\\t :%f m**3/kg of dry air\"%VH\n",
      "spvol=1.055;              #specific volume of saturated air in m**3*kg\n",
      "vdry=0.91;                #specific volume of dry air in m**3/kg\n",
      "Vh=vdry+(spvol-vdry)*.35  #by interpolation we get Vh in m**3/kg of dry air \n",
      "print \"\\n by interpolation we get specific volume Vh as(b) :%f m**3/kg of dry air\"%Vh\n",
      "\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " the humidity(from chart) is  \t\t:0.048300  percent\n",
        "\n",
        " the percentage humidity is(from chart) :35.000000  percent\n",
        "\n",
        " the percentage relative humidity is \t percent:37.822988  \n",
        "\n",
        " the dew point temperature \t\t :31.500000 degree celcius\n",
        "\n",
        " we get humid heat as \t\t\t :1.061520 kj/kg dry air degree celcius \n",
        "\n",
        " we get H as \t\t\t\t :128.136000 kj/kg\n",
        "\n",
        " we get enthalpy of wet air  as \t:128.400000 kj/kg\n",
        "\n",
        " we get VH  as (a)\t\t\t :0.963494 m**3/kg of dry air\n",
        "\n",
        " by interpolation we get specific volume Vh as(b) :0.960750 m**3/kg of dry air\n"
       ]
      }
     ],
     "prompt_number": 13
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example  5.2 "
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "# Variable Declaration \n",
      "\n",
      "#dry bulb temperature=25  and  wet bulb temperature=22\n",
      "Tg=25.;                    #dry bulb temperature=50\n",
      "To=0;                    #refrence temperature in degree celcius    \n",
      "Mb=28.84;                #average molecular weight of air\n",
      "Ma=18.;                   #average molecular weight of water\n",
      "\n",
      "\n",
      "# Calculation and Result\n",
      "#part(i)\n",
      "hum=.0145                #0.0145 kg of water/kg of dry air\n",
      "print \"\\n the saturation humidity(from chart) is :%f  percent\"%hum\n",
      "\n",
      "#part(ii)\n",
      "humper=57.;                #humidity percentage\n",
      "print \"\\n the percentage humidity is  \\t\\t:%f  percent\"%humper\n",
      "\n",
      "#part(iii)\n",
      "pt=1.;            #total pressure in atm\n",
      "sathum=0.0255;            #molal humidity =pa/(pt-pa)\n",
      "pa1=sathum*pt*(28.84/18)/(1+(sathum*(28.84/18)));\n",
      "#the vopour pressure of water(steam tables)at 25 = .0393*10**5 N/m**2\n",
      "pt=1;                     #total pressure in atm\n",
      "molhum=0.0145;            #molal humidity =pa/(pt-pa)\n",
      "pa2=molhum*pt*(28.84/18)/(1+(molhum*pt*(28.84/18)));\n",
      "#the vopour pressure of water(steam tables)at 25 = .0393*10**5 N/m**2\n",
      "relhum=(pa2/pa1)*100;      #percentage relative humidity =partial pressure/vapour pressure\n",
      "print \"\\n the percentage relative humidity is \\t :%f  \"%relhum\n",
      "\n",
      "#part(iv)\n",
      "dewpoint=19.5;            #dew point temperature in degree celcius\n",
      "print \"\\n the dew point temperature \\t :%f degree celcius\"%dewpoint\n",
      "\n",
      "#part(v)\n",
      "Ca=1005.;\n",
      "Cb=1884.;\n",
      "ybar=.0145;                # humidity inkg water /kg dry air\n",
      "Cs=Ca+Cb*ybar;            #humid heat  in j/kg dry air degree celcius\n",
      "d=2502300.;                    #latent heat in j/kg\n",
      "H=Cs*(Tg-0)+ybar*d;        #enthalpy for refrence temperature of 0 degree\n",
      "print \"\\n we get Humid heat H as \\t :%f j/kg\"%H\n",
      "#the actual answer is 62091.3 bt in book it is given 65188.25(calculation mistake in book)\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " the saturation humidity(from chart) is :0.014500  percent\n",
        "\n",
        " the percentage humidity is  \t\t:57.000000  percent\n",
        "\n",
        " the percentage relative humidity is \t :57.842165  \n",
        "\n",
        " the dew point temperature \t :19.500000 degree celcius\n",
        "\n",
        " we get Humid heat H as \t :62091.300000 j/kg\n"
       ]
      }
     ],
     "prompt_number": 14
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.3"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      "  \n",
      "# Variable Declaration \n",
      "\n",
      "#part(i)\n",
      "pt=800.;                    #total pressure in mmHg\n",
      "pa=190.;                    #vapour pressure of acetone at 25 degree \n",
      "ys_bar=pa*(58./28)/(pt-pa)   #\n",
      "#percentage saturation = y_bar/ys_bar *100\n",
      "s=80;                      #percent saturation\n",
      "\n",
      "# Calculation and Result\n",
      "y_bar=ys_bar*s/100.;        #absolute humidity\n",
      "print \"\\n the absolute humidity is \\t :%f kg acetone/kmol N2 \"%y_bar\n",
      "\n",
      "#part(ii)\n",
      "#y_bar=pa*(58/28)/(pt-pa) \n",
      "pa1=pt*y_bar*(28./58)/(1+(y_bar*(28./58)));\n",
      "print \"\\n the partial pressure of acetone is:%f mmHg\"%pa1\n",
      "\n",
      "#part(iii)\n",
      "y=pa1/(pt-pa1);              #absolute molal humidity\n",
      "print \"\\n absolute molal humidity \\t:%f kmol acetone/kmol N2\"%y\n",
      "\n",
      "#part(iv)\n",
      "#volume of .249kmol acetone vapour at NTP =.249*22.14\n",
      "#p1v1/T1 =p2v2/T2\n",
      "p2=800.;                    #final pressure of acetone and nitrogen at 25 degree\n",
      "p1=760.;                    #initial pressure of acetone and nitrogen at 25 degree\n",
      "T2=298.;                    #final temperature of acetone and nitrogenat 25 degree\n",
      "T1=273.;                   #initial temperature of acetone and nitrogen at 25 degree\n",
      "vA1=5.581;                    #initial volume of acetone at 25 degree\n",
      "vN1=22.414;                   #initial volume of nitrogen at 25 degree \n",
      "vA2=T2*vA1*p1/(T1*p2);        #final volume of acetone at 25 degree\n",
      "vN2=T2*vN1*p1/(T1*p2);        #final volume of nitrogen at 25 degree\n",
      "vtotal=vA2+vN2;            #total volume of the mixture\n",
      "vper=vA2*100/vtotal;           #percentage volume of acetone\n",
      "print \"\\n the percentage volume of acetone is :%f m**3\"%vper\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " the absolute humidity is \t :0.516159 kg acetone/kmol N2 \n",
        "\n",
        " the partial pressure of acetone is:159.580052 mmHg\n",
        "\n",
        " absolute molal humidity \t:0.249180 kmol acetone/kmol N2\n",
        "\n",
        " the percentage volume of acetone is :19.935703 m**3\n"
       ]
      }
     ],
     "prompt_number": 15
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example  5.4 "
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "\n",
      "# Variable Declaration \n",
      "\n",
      "#part(i)\n",
      "pa=13.3;                      #pressure in kpa\n",
      "pa2=20.6;                    #vapour pressure at 60 degree\n",
      "pt=106.6                     #total pressure in kpa\n",
      "y=pa/(pt-pa);              #absolute molal humidity\n",
      "\n",
      "# Calculation  and Result\n",
      "y_bar=y*(18/28.84);          #relative humidity\n",
      "print \"\\n absolute  humidity of mixture :%f kg water-vapour/kg dry air\"%y_bar\n",
      "\n",
      "\n",
      "#part(ii)\n",
      "mf=pa/pt;                    #mole fraction\n",
      "print \"\\n the mole fraction is :%f\"%mf\n",
      "\n",
      "#part(iii)\n",
      "vf=mf;                            #volume fraction\n",
      "print \"\\n the volume fraction is :%f\"%vf\n",
      "\n",
      "#part(iv)\n",
      "Ma=18.;                      #molecular weight\n",
      "Mb=28.84;                    #molecular weight\n",
      "Tg=60.;                       #temperature of mixture\n",
      "rh=(pa/pa2)*100.;            #relative humidity in pecentage        \n",
      "print \"\\n we get relative humidity as  as :%f percent\"%rh\n",
      "\n",
      "#part(v)\n",
      "VH=8315.*((1./Mb)+(y_bar/Ma))*((Tg+273)/pt)*10**-3;        #humid volume in m**3mixture/kg of dry air\n",
      "x=y_bar/VH;                 #g water/m**3 mixture \n",
      "print \"\\n we get x i.e. gwater/m**3 mixture as :%f \"%(x*1000)\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " absolute  humidity of mixture :0.088971 kg water-vapour/kg dry air\n",
        "\n",
        " the mole fraction is :0.124765\n",
        "\n",
        " the volume fraction is :0.124765\n",
        "\n",
        " we get relative humidity as  as :64.563107 percent\n",
        "\n",
        " we get x i.e. gwater/m**3 mixture as :86.460483 \n"
       ]
      }
     ],
     "prompt_number": 16
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.5 "
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "\n",
      "# Variable Declaration \n",
      "\n",
      "#part(i)\n",
      "y_bar=.0183;                #kg water vapour/kg dry air\n",
      "print \"\\n we get humidity as(from chart)  :%f kg of water/kg dry air\"%y_bar\n",
      "print \"\\n we get saturation humidity as(from chart)  :%d percent\"%67\n",
      "Ma=18.;                      #molecular weight\n",
      "Mb=28.84;                    #molecular weight\n",
      "Tg=30.;   \n",
      "pa = 13.3\n",
      "pa2 = 20.6                    #temperature of mixture\n",
      "rh=(pa/pa2)*100;            #relative humidity in pecentage        \n",
      "pt=1.013*10**5;            #total pressure in pascal\n",
      "\n",
      "# Calculation  and  Result\n",
      "VH=8315*((1./Mb)+(y_bar/Ma))*((Tg+273)/pt);        #humid volume in m**3mixture/kg of dry air\n",
      "print \"\\n we get humid volume as \\t:%f  m**3/kg dry air\"%VH\n",
      "\n",
      "#part(ii)\n",
      "Ca=1005.;\n",
      "Cb=1884.;\n",
      "Cs=Ca+Cb*y_bar;            #humid heat  in j/kg dry air degree celcius\n",
      "print \"\\n we get humid heat as \\t\\t :%f j/kg dry air degree celcius \"%Cs\n",
      "\n",
      "#part(iii)\n",
      "d=2502300.;                    #latent heat in j/kg\n",
      "H=Cs*(Tg-0)+y_bar*d;        #enthalpy for refrence temperature of 0 degree\n",
      "print \"\\n we get Enthalpy H as \\t\\t:%f j/kg dry air\"%H\n",
      "\n",
      "#part(iv)\n",
      "dewpoint=23.5;            #dew point temperature in degree celcius\n",
      "print \"\\n the dew point temperature \\t :%f degree celcius\"%dewpoint\n",
      "\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " we get humidity as(from chart)  :0.018300 kg of water/kg dry air\n",
        "\n",
        " we get saturation humidity as(from chart)  :67 percent\n",
        "\n",
        " we get humid volume as \t:0.887669  m**3/kg dry air\n",
        "\n",
        " we get humid heat as \t\t :1039.477200 j/kg dry air degree celcius \n",
        "\n",
        " we get Enthalpy H as \t\t:76976.406000 j/kg dry air\n",
        "\n",
        " the dew point temperature \t :23.500000 degree celcius\n"
       ]
      }
     ],
     "prompt_number": 17
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.6 "
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "# Variable Declaration \n",
      "\n",
      "#part(i)\n",
      "y=.048;                      #humidity kmol water vapour/kmol dry air\n",
      "y_bar=y*(18/28.84);          #(from chart) absolute humidity\n",
      "print \"we get absolute humidity as  :%f kg of water/kg dry air\"%(y_bar)\n",
      "print \"we get percentage humidity as(from chart)  :%f percent\"%(25.5);\n",
      "\n",
      "# Calculation and Result\n",
      "y_bar=y*(18/28.84);          #relative humidity\n",
      "Ma=18.;                      #molecular weight\n",
      "Mb=28.84;                    #molecular weight\n",
      "Tg=55.;                       #temperature of mixture\n",
      "pt=1.013*10**5;            #total pressure in pascal\n",
      "VH=8315*((1./Mb)+(y_bar/Ma))*((Tg+273)/pt);        #humid volume in m**3mixture/kg of dry air\n",
      "print \"\\n we get VH  as \\t :%f m**3/kg dry air\"%VH\n",
      "\n",
      "#part(ii)\n",
      "Ca=1005.;\n",
      "Cb=1884.;\n",
      "Cs=Ca+Cb*y_bar;            #humid heat  in j/kg dry air degree celcius\n",
      "print \"\\n we get humid heat as \\t :%f j/kg dry air degree celcius \"%Cs\n",
      "\n",
      "#part(iii)\n",
      "d=2502300.;                    #latent heat in j/kg\n",
      "H=Cs*(Tg-0)+y_bar*d;        #enthalpy for refrence temperature of 0 degree\n",
      "print \"\\n we get H as \\t :%f j/kg dry air\"%H\n",
      "\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "we get absolute humidity as  :0.029958 kg of water/kg dry air\n",
        "we get percentage humidity as(from chart)  :25.500000 percent\n",
        "\n",
        " we get VH  as \t :0.978346 m**3/kg dry air\n",
        "\n",
        " we get humid heat as \t :1061.441609 j/kg dry air degree celcius \n",
        "\n",
        " we get H as \t :133344.170596 j/kg dry air\n"
       ]
      }
     ],
     "prompt_number": 18
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.7 "
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "\n",
      "# Variable Declaration \n",
      "\n",
      " \n",
      "ft=46;                #final temperature in degree celcius\n",
      "# Calculation and Result\n",
      "print \"\\n final temperature is (from chart):%f degree celcius\"%ft\n",
      "y_bar=.0475;        # humidity of air\n",
      "print \"\\n the humidity of air(from chart) :%f kg water vapour /kg dry air\"%y_bar\n",
      "\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " final temperature is (from chart):46.000000 degree celcius\n",
        "\n",
        " the humidity of air(from chart) :0.047500 kg water vapour /kg dry air\n"
       ]
      }
     ],
     "prompt_number": 19
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.8"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "# Variable Declaration \n",
      "\n",
      "pa1=4.24            #data:vapour pressure of water at 30degree = 4.24 kpa\n",
      "pa2=1.70            #vapour pressure of water at 30degree = 1.70 kpa\n",
      "\n",
      "#part(i)\n",
      "pt=100.;                         #total pressure\n",
      "\n",
      "# Calculation  \n",
      "ys_bar=pa1/(pt-pa1);              #kg water vapour/kg dry air\n",
      "rh=.8;                          #relative humidity\n",
      "pa3=rh*pa1;                       #partial pressure\n",
      "y_bar=pa3*(18/28.84)/(pt-pa3);               #molal humidity\n",
      "print \"\\n the molal humidity:%f kg/kg dry air\"%y_bar\n",
      "\n",
      "#part(ii)\n",
      "\n",
      "pa=1.7;    \n",
      "pt=200.;\n",
      "ys=pa/(pt-pa);\n",
      "ys_bar=ys*(18/28.84);\n",
      "\n",
      "# Result\n",
      "print \"\\n the molal humidity if pressure doubled and temp. is 15 :%f kg/kg dry air\"%ys_bar\n",
      "\n",
      "#part(iii) \n",
      "Ma=18.;                        #molecular weight\n",
      "Mb=28.84;                    #molecular weight\n",
      "Tg=30.;                       #temperature of mixture\n",
      "rh=(pa/pa2)*100;            #relative humidity in pecentage        \n",
      "pt=10**5;              #total pressure in pascal\n",
      "VH=8315*((1./Mb)+(y_bar/Ma))*((Tg+273)/pt);        #humid volume in m**3mixture/kg of dry air\n",
      "print \"\\n we get humid volume VH  as \\t :%f m**3/kg of dry air\"%VH\n",
      "w=100/VH;                   #100 m**3 of original air \n",
      "wo= w*y_bar;                #water present in original air\n",
      "wf= w*ys_bar;              #water present finally\n",
      "wc=wo-wf;                   #water condensed from 100m**3 of original sample\n",
      "print \"\\n the weight water condensed from 100m**3 of original sample:%f kg\"%wc\n",
      "\n",
      "#part(iv)\n",
      "Tg=15.;                       #temperature of mixture       \n",
      "pt=2*10**5;            #total pressure in pascal\n",
      "VH=8315*((1./Mb)+(ys_bar/Ma))*((Tg+273)/pt);        #humid volume in m**3mixture/kg of dry air\n",
      "vf=VH*110.6;                #final volume of mixture\n",
      "print \"\\n we get VH final volume of mixture as \\t :%f m**3\"%vf\n",
      "\n",
      "#end\n"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " the molal humidity:0.021914 kg/kg dry air\n",
        "\n",
        " the molal humidity if pressure doubled and temp. is 15 :0.005351 kg/kg dry air\n",
        "\n",
        " we get humid volume VH  as \t :0.904267 m**3/kg of dry air\n",
        "\n",
        " the weight water condensed from 100m**3 of original sample:1.831684 kg\n",
        "\n",
        " we get VH final volume of mixture as \t :46.311825 m**3\n"
       ]
      }
     ],
     "prompt_number": 20
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example  5.9"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "# Variable Declaration \n",
      "\n",
      "#part(i)\n",
      "y_bar=.03;                   # humidity inkg water /kg dry air\n",
      "pt=760.;                     #total pressure in pascal\n",
      "pa2=118.;                    #final pressure\n",
      "\n",
      "# Calculation  and  Result\n",
      "y=y_bar/(18/28.84);        #humidity kmol water vapour/kmol dry air\n",
      "pa=(y*pt)/(y+1);           #partial pressure\n",
      "rh=pa/pa2;                  #relative humidity\n",
      "sh=pa2/(pt-pa2);            #saturated humidity\n",
      "ph=(y/sh)*100;                #percentage humidity\n",
      "print \"\\n percentage humidity is :%f\"%ph\n",
      "\n",
      "#/part(ii)\n",
      "Ma=18.;                      #molecular weight\n",
      "Mb=28.84;                    #molecular weight\n",
      "Tg=55.;                       #temperature of mixture\n",
      "pt=1.013*10**5;            #total pressure in pascal\n",
      "VH=8315*((1./Mb)+(y_bar/Ma))*((Tg+273)/pt);        #humid volume in m**3mixture/kg of dry air\n",
      "print \"\\n we get VH humid volume as  :%f m**3/kg dry air\"%VH\n",
      "\n",
      "\n",
      "#part(iii)\n",
      "Ca=1005.;\n",
      "Cb=1884.;\n",
      "Cs=Ca+Cb*y_bar;                #humid heat  in j/kg dry air degree celcius\n",
      "print \"\\n we get humid heat as \\t :%f j/kg dry air degree celcius \"%Cs\n",
      "d=2502300;                    #latent heat in j/kg\n",
      "H=Cs*(Tg-0)+y_bar*d;         #enthalpy for refrence temperature of 0 degree\n",
      "print \"\\n we get H enthalpy as \\t :%f j/kg\"%H\n",
      "\n",
      "#part(iv)\n",
      "v=100.;                        #volume of air\n",
      "mass=v/VH;                    #mass of dry air\n",
      "Tg=110.;                       #temperature of mixture\n",
      "d=2502300.;                    #latent heat in j\n",
      "H_final=Cs*(Tg-0)+y_bar*d;    #enthalpy for refrence temperature of 0 degree\n",
      "H_added=(H_final-H)*102.25;     #HEAT added  in kj     \n",
      "print \"\\n we get heat added as \\t :%f kj\"%(H_added/1000)\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " percentage humidity is :26.151525\n",
        "\n",
        " we get VH humid volume as  :0.978409 m**3/kg dry air\n",
        "\n",
        " we get humid heat as \t :1061.520000 j/kg dry air degree celcius \n",
        "\n",
        " we get H enthalpy as \t :133452.600000 j/kg\n",
        "\n",
        " we get heat added as \t :5969.723100 kj\n"
       ]
      }
     ],
     "prompt_number": 21
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.10"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "# Variable Declaration \n",
      "\n",
      "%pylab inline\n",
      "L=2000.;                    #flow rate of water to be cooled in kg/min\n",
      "T1=50.;                    #temperature of inlet water\n",
      "T2=30.;                    #temp. of outlet water\n",
      "H1=.016;                  #humidity of incoming air\n",
      "cp=4.18;                  #specific heat of water\n",
      "cpair=1.005;              #specific heat capcity of air\n",
      "cpwater=1.884;            #specific heat capcity of water\n",
      "tg=20.;                    #temperature in degree\n",
      "to=0;\n",
      "ybar=0.016;               #saturated humidity at 20 degree\n",
      "d=2502.;                   #latent heat\n",
      "Ky_a=2500.;                #value of masstransfer coefficient in kg/hr*m**3*dybar\n",
      "\n",
      "# Calculation  \n",
      "E=cpair*(tg-to)+(cpwater*(tg-to)+d)*ybar;    #enthalpy\n",
      "#similarly for other temperatures\n",
      "T=[20,30,40,50,55]            #differnt temperature for different enthalpy calculation\n",
      "i=0;\n",
      "E= [0,0,0,0,0]\n",
      "while(i<5):                   #looping for different enthalpy calculation of operating line\n",
      "    E[i]=cpair*(T[i]-to)+(cpwater*(T[i]-to)+d)*ybar;\n",
      "    print \"\\n the enhalpy at :%f is :%f\"%(T[i],E[i]);\n",
      "    i=i+1;\n",
      "\n",
      "ES=[60.735,101.79,166.49,278.72,354.92]        #enthalpy of eqll condition\n",
      "from matplotlib.pyplot import *\n",
      "\n",
      "# Result\n",
      "plot(T,E);\n",
      "plot(T,ES);\n",
      "title(\"Fig.5.10(b),Temperature-Enthalpy plot\");\n",
      "xlabel(\"X-- Temperature, degree celcius\");\n",
      "ylabel(\"Y-- Enthalpy ,kj/kg\");\n",
      "legend(\"operating line\",\"Enthalpy at saturated cond\")\n",
      "show()\n",
      "\n",
      "Hg1=71.09;                     #point on the oper. line(incoming air)\n",
      "Hg2=253.;                       #point after drawing the tangent\n",
      "slope=(Hg2-Hg1)/(T1-T2);       #we gt slope of the tangent\n",
      "    #slope = (L*Cl/G)_min\n",
      "Cl=4.18;\n",
      "G_min=L*60*Cl/slope;                  #tangent gives minimum value of the gas flow rate\n",
      "G_actual=G_min*1.3;                  #since actual flow rate is 1.3 times the minimum\n",
      "slope2=L*Cl*60/G_actual;            #slope of operating line\n",
      "Hg2_actual=slope2*(T1-T2)+Hg1;     #actual humidityat pt 2\n",
      "Ggas=10000.;                       #minimum gas rate in kg/hr*m**2\n",
      "Area1=G_actual/Ggas;             #maximum area of the tower(based on gas)\n",
      "Gliq=12000.;                     #minimum liquid rate in kg/hr*m**2\n",
      "Area2=60*L/Gliq;               #maximum area of the tower(based on liquid)\n",
      "print \"\\n \\n the maximum area of the tower(based on gas) is :%f m**2\"%Area1\n",
      "print \"\\n the maximum area of the tower(based on liquid) is :%f m**2\"%Area2\n",
      "dia=(Area1*4/3.14)**0.5;        #diameter of the tower in m\n",
      "\n",
      "\n",
      " \n",
      "#table\n",
      "T=[20,30,40,50,55]            #differnt temperature for different enthalpy calculation\n",
      "#enthaly \n",
      "H_bar=[101.79,133.0,166.49,210.0,278.72]        #H_bar i.e. at equl.\n",
      "Hg=[71.09,103.00,140.00,173.00,211.09]        #Hg i.e. of operating line\n",
      "i=0;\n",
      "y = [0,0,0,0,0]\n",
      "while(i<5):          #looping for different enthalpy calculation of operating line\n",
      "    y[i]=1./(H_bar[i]-Hg[i]);\n",
      "    print \"\\n the enhalpy at :%f is :%f\"%(T[i],y[i]);\n",
      "    i=i+1;\n",
      "\n",
      "plot(Hg,y,\"o-\");\n",
      "\n",
      "#area under this curve gives Ntog =4.26\n",
      "Ntog=4.26;                #no. of transfer unit\n",
      "Gs=10000.;                  #gas flow rate\n",
      "Htog=Gs/Ky_a;              # height of transfer unit\n",
      "height=Ntog*Htog;          #height of the tower\n",
      "print \"\\n \\nthe tower height is :%f m\"%height\n",
      "\n",
      "\n",
      "#M = E + B + W\n",
      "W=.2/100 *L*60;                #windage loss(W)\n",
      "B=0;                        #blow down loss neglected\n",
      "E=G_actual*(.064-.016);     #assuming air leaves fully saturated\n",
      "M = E + B + W;                #make up water is based onevaporation loss(E),blow down loss(B),windage loss(W)\n",
      "print \"\\n make up water is based onevaporation loss(E),blow down loss(B),windage loss(W) is :%f kg /hr\"%M\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        "Welcome to pylab, a matplotlib-based Python environment [backend: module://IPython.zmq.pylab.backend_inline].\n",
        "For more information, type 'help(pylab)'.\n"
       ]
      },
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " the enhalpy at :20.000000 is :60.734880\n",
        "\n",
        " the enhalpy at :30.000000 is :71.086320\n",
        "\n",
        " the enhalpy at :40.000000 is :81.437760\n",
        "\n",
        " the enhalpy at :50.000000 is :91.789200\n",
        "\n",
        " the enhalpy at :55.000000 is :96.964920\n"
       ]
      },
      {
       "output_type": "stream",
       "stream": "stderr",
       "text": [
        "C:\\Anaconda\\lib\\site-packages\\matplotlib\\legend.py:336: UserWarning: Unrecognized location \"Enthalpy at saturated cond\". Falling back on \"best\"; valid locations are\n",
        "\tright\n",
        "\tcenter left\n",
        "\tupper right\n",
        "\tlower right\n",
        "\tbest\n",
        "\tcenter\n",
        "\tlower left\n",
        "\tcenter right\n",
        "\tupper left\n",
        "\tupper center\n",
        "\tlower center\n",
        "\n",
        "  % (loc, '\\n\\t'.join(self.codes.iterkeys())))\n"
       ]
      },
      {
       "output_type": "display_data",
       "png": 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KUVFRiIqKqnPA90XFgRDS0C4kXcCkw5Mwrc80rB68ukk2IzVYcbh//z569uyJ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\nXJQcRETERclBRERc3gD5uXssNmBL3wAAAABJRU5ErkJggg==\n"
      },
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " \n",
        " the maximum area of the tower(based on gas) is :7.169260 m**2\n",
        "\n",
        " the maximum area of the tower(based on liquid) is :10.000000 m**2\n",
        "\n",
        " the enhalpy at :20.000000 is :0.032573\n",
        "\n",
        " the enhalpy at :30.000000 is :0.033333\n",
        "\n",
        " the enhalpy at :40.000000 is :0.037750\n",
        "\n",
        " the enhalpy at :50.000000 is :0.027027\n",
        "\n",
        " the enhalpy at :55.000000 is :0.014786\n",
        "\n",
        " \n",
        "the tower height is :17.040000 m"
       ]
      },
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        "\n",
        " make up water is based onevaporation loss(E),blow down loss(B),windage loss(W) is :3681.244571 kg /hr\n"
       ]
      },
      {
       "output_type": "display_data",
       "png": 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WFi6XixEjRjBixAiKiopaeRgiIsGvXz9riurixVZyCEY+k4LX62XOnDkUFRWx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\n3JueAAAAAElFTkSuQmCC\n"
      }
     ],
     "prompt_number": 1
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.11"
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      " \n",
      "T1=30.;              #temperature at the inlet in degree celcius\n",
      "T2=17.;              #temperature at the exit in degree celcius\n",
      "f=100000.;           #flow rate of water in kg/hr\n",
      "hi=.004;            #humidity of incoming air in kg/kg of dry air\n",
      "hl=.015;            #humidity of leaving air in kg/kg of dry air\n",
      "Hi=18.11;           #enthalpy of incoming air in kg/kg of dry air\n",
      "Hl=57.16;            #enthalpy of leaving air in kg/kg of dry air\n",
      "#w=mdry*(hl-hi) = mdry*0.011;                             -----equn 1st  \n",
      "#mass of water evaporated\n",
      "\n",
      "#making energy balance:  total heat in = total heat out\n",
      "#heat in entering water + heat in entering air = heat in leaving water + heat in leaving air\n",
      "#100000*1*(30-0) + mdry*Hi = (100000-w)*1*(17-0) + mdry*Hl  ----eqn 2nd\n",
      "\n",
      "#substituting eqn 1st in 2nd we get;\n",
      "a=14.4;                                   #cross sectional area of the tower in m**2\n",
      "\n",
      "# Calculation  \n",
      "mdry=(T1*f-T2*f)/(Hl-Hi-T2*.011);        #mass of dry air\n",
      "velocity=mdry/a;                          #air velocity in kg/m**2* hr\n",
      "x=mdry*.011;                             #make up water needed in kg/hr\n",
      "\n",
      "# Result\n",
      "print \"\\n the make up water needed is :%f kg /hr\"%x\n",
      "print \"\\n the velocity of air is as :%f kg/hr\"%velocity\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " the make up water needed is :367.959241 kg /hr\n",
        "\n",
        " the velocity of air is as :2322.975009 kg/hr\n"
       ]
      }
     ],
     "prompt_number": 22
    },
    {
     "cell_type": "heading",
     "level": 3,
     "metadata": {},
     "source": [
      "Example 5.12 "
     ]
    },
    {
     "cell_type": "code",
     "collapsed": false,
     "input": [
      " \n",
      "import math\n",
      " \n",
      "\n",
      "T1=65;              #dry bulb temperature at the inlet in degree celcius\n",
      "f=3.5;           #flow rate of air in m**3/s\n",
      "hi=1.017;            #humidity of incoming air in kg/kg of dry air\n",
      "hl=.03;            #humidity of leaving air in kg/kg of dry air\n",
      "k=1.12;            #mass transfer coefficient in kg/m**3*s\n",
      "y1=.017;           #molefraction at recieving end\n",
      "y2=.03;            #molefraction at leaving end\n",
      "\n",
      "#substituting eqn 1st in 2nd we get;\n",
      "a=2;                                   #cross sectional area of the tower in m**2\n",
      "d=1.113;                                  #density o fair in kg/m**3\n",
      "\n",
      "# Calculation  \n",
      "m=(f*d)                                   #mass flow rate  of  air\n",
      "gs=m/hi;                                 #air velocity in kg/m**2* hr\n",
      "ys_bar=.032;\n",
      "#for recirculation humidifier\n",
      "# Result\n",
      "z=math.log((ys_bar-y1)/(ys_bar-y2))*gs/k;          #length of the chamber required\n",
      "print \"\\n the length of the chamber required is :%f m\"%z\n",
      "\n",
      "#end"
     ],
     "language": "python",
     "metadata": {},
     "outputs": [
      {
       "output_type": "stream",
       "stream": "stdout",
       "text": [
        "\n",
        " the length of the chamber required is :6.890939 m\n"
       ]
      }
     ],
     "prompt_number": 12
    }
   ],
   "metadata": {}
  }
 ]
}