{ "metadata": { "name": "ch5", "signature": "sha256:2ee4e5f8137c7268975819ca4a31ef66c4a59076a802f56667cecd1c3f67b2a9" }, "nbformat": 3, "nbformat_minor": 0, "worksheets": [ { "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", "%matplotlib 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\n2NjYKpuSWrduDZFIVO+g9UXFgRDSUKQyKdb+uRa/xP6Cnd474d7Vne9IStNgxWHGjBnYunUrXF1d\nqywOr169Qu/evbF79+76p60HKg6EkIaQWZAJ/0P+YGD4Y9wfTa4Z6V0N3qwkk8mgoSF/IXVJSQl0\ndHTg4eHR6E1LVBwIIe/r3JNzmHxkMmb0nYFVg1ZBU0OT70hK1+BjK02fPl3ueUFBATe2Eh/nHAgh\npL6kMilWXVyFyUcmY+fYnVjjuqZZFIb6qLE4mJub09hKhBC1l56fDredbriSegU3Z91U66udGwON\nrUQIafKiHkch8GggZvedjS8GfdEsjxZobCVCCPn/SWQSBIuDsf3WduwauwtDLYfyHYk3DVYcgoKC\n5Hop0dhKhBB1kp6fDr9DftDW0MbucbvRTr8d35F4pfSL4PhGxYEQUpMz/5xB0LEgzHWci/8M/E+z\nbEZ6V4P3VnrXzz//jH379kEikdT43tTUVAwZMgQ2Njbo1asXQkJCAADBwcGwsLCAg4MDHBwccOrU\nKW6e9evXo3v37ujRowf1hiKE1IlEJsHKCysxNWIq9vrsxZeDv6TCUE91PnLYsmULHjx4gOTkZBw/\nfrza92ZmZiIzMxP29vYoKChA3759cfToUezfvx9CoRCLFi2Se39CQgL8/f1x48YNpKWlYdiwYUhM\nTJS7zoKOHAghVUl7nQa/Q37Q0dLBrrG7YKbf+GO/qbIGG7JbkXnz5tX6ve3atUO7dm/b+fT19dGz\nZ0+kpaUBQJUhjx07Bj8/P2hra0MkEqFbt26Ijo6Gi4tLXWMSQpqR0/+cRtDRIMx3mo8VA1dAQ1Dn\nRhHyjkYbXerp06eIi4uDi4sLrly5gs2bN2Pnzp1wdHTEDz/8ACMjI6Snp8sVAgsLC66YVBQcHMw9\ndnV1haurayN8A0KIqpHIJPjy4pfYdXsX9n2yD4NFg/mOpDLEYjHEYnG952+UE9IFBQVwdXXFF198\nAW9vbzx//hwmJiYAgC+//BIZGRnYtm0b5s+fDxcXF0ycOBHA26uzR44cKddtlpqVCCEAkJqXCr9D\nftBroYddY3fBVM+U70gqTeknpOuqrKwMPj4+mDRpEry9vQEApqamEAgEEAgEmD59OqKjowG8vRo7\nNTWVm/fZs2cwN1fvW/MRQhreyUcn0W9rP4zsPhKnJp6iwqAENRaHvn374ueff0ZOTk6dF84Yw7Rp\n02BtbY1aPgdKAAAgAElEQVSFCxdy0zMyMrjHR44cga2tLQDAy8sL4eHhKC0tRVJSEh49egQnJ6c6\nfy4hpGkqk5Zh2bllmBU5C/s/3Y//DPwPnV9QkhrPOYSHh2P79u3o168fHB0dMWXKFHh4eNTqdqFX\nrlzB7t270bt3bzg4OAAA1q1bh7179+LWrVsQCASwtLTEL7/8AgCwtraGr68vrK2toaWlhdDQULot\nKSEEwNtmpAmHJsCgpQFuzrwJEz0TviM1abU+5yCTyRAZGYk5c+ZAQ0MDU6dOxWeffYbWrVsrO6Mc\nOudASPMTmRiJaRHTsMhlEZZ8tISOFupBKV1Zb9++je3bt+PUqVPw8fGBv78/Ll++jKFDh+LWrVv1\nDksIIdUpk5bhPxf+g3339uGQ7yEM6DSA70jNRo3FoW/fvjA0NMT06dOxYcMG6OjoAADXJZUQQpQh\nOTcZEw5NQOtWrXFz1k201W3Ld6RmpcZmpcePH6Nr166NladG1KxESNN3/OFxTD8+Hf/+8N9Y3H8x\nNSM1gAZvVjI0NMT8+fNx+fJlCAQCDBw4EKtWrUKbNm3eKyghhLyrVFqKFedX4ED8ARz2PYyPOn3E\nd6Rmq8ZyPGHCBJiamuLw4cM4ePAgTExMMH78+MbIRghpRpJzkzFo+yA8fPkQcbPiqDDwrMZmpV69\neuHevXty02xtbXH37l2lBlOEmpUIaXqOPTiGmZEzsaT/Eiz6cBE1IylBg18h7eHhgb1790Imk0Em\nk2Hfvn3w8PB4r5CEEAK8bUZadGYRFpxegKPjj9L5BRVS45GDvr4+ioqKuGGzZTIZ9PT03s4sEOD1\n69fKT1kBHTkQ0jQk5SRhwqEJMNMzww7vHWjdqnGvmWpu6E5whBCVd+T+EcyKnIXlA5bjc5fPaSSE\nRtBgvZViY2Or/Qfr06dP3ZIRQpq9Umkplp5diqMPjiLCLwIuFnSvFlWl8MjB1dW12uJw8eJFpYWq\nDh05EKKenuQ8wfiD42EuNMf2Mdth3MqY70jNCjUrEUJUzuH7hzE7cjb+M/A/+Mz5M2pG4oFSxla6\ne/cu7t+/j5KSEm7a5MmT656OENKsvJG8wZKzS3A88Tgi/SPhZE5D8KuLGotDcHAwLl26hPj4eIwa\nNQqnTp3CgAEDqDgQQqr1JOcJfA/4oqNhR9yceZOakdRMjR2KDx48iHPnzqF9+/bYvn07bt++jdzc\n3MbIRghRUwcTDsLlNxdMtpuMw76HqTCooRqPHFq1agVNTU1oaWkhLy8PpqamcrfyJISQciWSEiyO\nWoyTj07ihP8J9DPvx3ckUk81Fod+/fohJycHM2bMgKOjI/T09NC/f//GyEYIUSP/ZP8D3wO+sDS2\nxM1ZN2GkY8R3JPIe6tRbKSkpCfn5+ejdu7cyM1WLeisRonr2x+/Hv07+C6sHr8a/+v2LeiOpIKV0\nZU1LS0NycjIkEgkYYxAIBBg0aNB7Ba0vKg6EqI4SSQkWnVmEM4/PYP8n+9G3Q1++IxEFGrwr67Jl\ny7Bv3z5YW1tDU1OTm85XcSCEqIZHrx7B96AvurXuhpszb8JQx5DvSKQB1XjkYGVlhbt376Jly5aN\nlaladORACP/23duHeafmIXhwMOb2m0vNSGqgwY8cunbtitLSUpUpDoQQ/pRISvD5mc9x9vFZnJl0\nBn3a0xhrTZXC4jB//nwAgK6uLuzt7eHm5sYVCIFAgJCQkMZJSAhRCYmvEuF7wBcftP0AN2fdhEFL\nA74jESVSWBz69u3LHSp6enpyj8tPSNdGamoqJk+ejOfPn0MgEGDmzJlYsGABsrOzMX78eCQnJ0Mk\nEmH//v0wMnrb7W39+vX4/fffoampiZCQELqxECEqYO/dvVhwegHWDlmLWX1nUTNSc8Bq8P/+3/+r\n1bSqZGRksLi4OMYYY/n5+czKyoolJCSwJUuWsG+//ZYxxtiGDRvYsmXLGGOMxcfHMzs7O1ZaWsqS\nkpJY165dmVQqlVtmLSITQhpIUWkRm3l8JusW0o3dTL/JdxzyHuq67axx+IywsLBK03bs2FGrwtOu\nXTvY29sDeHtHuZ49eyItLQ0REREIDAwEAAQGBuLo0aMAgGPHjsHPzw/a2toQiUTo1q0boqOja1fl\nCCEN6uHLh3DZ5oK8kjzEzoyFQ3sHviORRqSwWWnv3r3Ys2cPkpKS4OnpyU3Pz89HmzZt6vxBT58+\nRVxcHJydnZGVlQUzMzMAgJmZGbKysgAA6enpcHH5v5t/WFhYIC0trdKygoODuceurq5wdXWtcx5C\niGJ/3PkDC88sxNdDvsbMvjOpGUkNicViiMXies+vsDj0798f7du3x4sXL7B48WKuC5RQKISdnV2d\nPqSgoAA+Pj7YtGkThEKh3GsCgaDaH15Vr1UsDoSQhlNcVowFpxfg0tNLOBtwFvbt7PmOROrp3R3n\nNWvW1Gl+hcWhc+fO6Ny5M65du1bvcABQVlYGHx8fBAQEwNvbG8Dbo4XMzEy0a9cOGRkZMDU1BQCY\nm5vLDer37NkzmJubv9fnE0Jq58HLB/A94Itepr0QOzMWwpbCmmciTVaN5xwOHTqE7t27w8DAAEKh\nEEKhEAYGtevCxhjDtGnTYG1tjYULF3LTvby8uHMZYWFhXNHw8vJCeHg4SktLkZSUhEePHsHJiW4O\nQoiy7b6zGwO3D8R8p/n4Y9wfVBhIzVdId+3aFZGRkejZs2edF3758mUMGjQIvXv35pqH1q9fDycn\nJ/j6+iIlJaVSV9Z169bh999/h5aWFjZt2oThw4fLB6YrpAlpMEVlRZh/aj6upFzB/k/3o7cZf4Nq\nEuVq8IH3PvroI1y5cuW9gzUUKg6ENIyEFwnwPeAL+3b2+O+o/9LRQhPX4MNnODo6Yvz48fD29kaL\nFi24Dxk3blz9UxJCeLXz9k78O+rf2OC2AVMdplJvJFJJjcUhLy8PrVq1QlRUlNx0Kg6EqJ/C0kLM\nOzUP155dw4XJF2BrZst3JKKi6nSzH1VAzUqE1E/CiwR8euBT9G3fF6GjQqHfQp/vSKQR1XXbqbC3\nkq+vL/d42bJlcq/ReEeEqJcdt3Zg8I7BWPzhYoR5h1FhIDVSWBwePXrEPX63SenFixfKS0QIaTCF\npYUIOhqE7658B3GgGFMcptD5BVIrNV7nQAhRT/ee30O/rf0AADdm3ICNqQ3PiYg6UXhCuri4GDdv\n3gRjjHsMgHtOCFFNjDFsv7Udy84tw/fu3yPIPojvSEQNKTwh7erqWu09HC5evKj8dFWgE9KEKFZQ\nWoC5J+YiNiMWBz49AGsTa74jERXR4BfBqRoqDoRU7W7WXfge9MWHFh9i84jN0Guhx3ckokIarLcS\nIUQ9MMaw7eY2DN05FCsGrMDvY36nwkDeW40XwRFCVFdBaQFmR87Grcxb+DPoT/Q0qfsYaIRUhY4c\nCFFTd7LuwPFXR+ho6SB6RjQVBtKg6lQc6CY7hPCPMYZfY3+F2043fDHoC/zm9Rt0tXX5jkWamDqd\nkHZwcEBcXJwy89SITkiT5iz/TT5mRc7Cvef3sP/T/ejRtgffkYiaUOoJadooE8Kf25m30ffXvtBv\noY/r069TYSBKVacjB5lMBg0Nfk9T0JEDaW7iMuKw6fomRCZGYtPHmzCx90S+IxE1pNQjB0dHxzoH\nIoTUnUQmwYH4Axi4fSDGhI9Bz7Y98XDeQyoMpNEo7Mo6YsQIhIaGwtLSkptGe+yEKNerolfYenMr\nQm+EQmQkwmfOn8G7hze0NKjXOWlcCo8cpk6diuHDh+Obb75BWVkZAGDUqFGNFoyQ5uRu1l3MOD4D\n3TZ3w8NXD3F0wlH8OeVPfGL9CRUGwotqzzkUFBTgq6++wpkzZxAQEMCNryQQCLBo0aJGC1kRnXMg\nTYVUJsXxxOMIuR6Ch68eYo7jHMzsOxOmeqZ8RyNNUIPeQ1pbWxv6+vooKSlBfn4+7yejCWkKckty\nse3mNmy5sQVmemb4zPkz+Fj7oIVmC76jEcJRWBxOnz6NRYsWwdPTE3FxcdDVpYtsCHkf91/cx+bo\nzQi/F46R3Uci3CcczhbOfMcipEoKm5UGDhyI//3vf7CxUa0bhFCzElEnMibDqUenEBIdgtuZtzHL\ncRZm952N9sL2fEcjzUyDdWX9888/37swTJ06FWZmZrC1teWmBQcHw8LCAg4ODnBwcMCpU6e419av\nX4/u3bujR48elW5NSog6ef3mNUKuh+CDLR9glXgVJtpORPLCZKxxXUOFgagFpd7P4a+//oK+vj4m\nT56Mu3fvAgDWrFkDoVBY6YR2QkIC/P39cePGDaSlpWHYsGFITEysdJ6DjhyIKvsn+x9sjt6MXbd3\nwb2rOxY4LUD/jv3pvs2Edyp1P4eBAwfC2Ni40vSqAh47dgx+fn7Q1taGSCRCt27dEB0drcx4hDQI\nxhiiHkdh9J7R6L+tP/S09XB79m3s+2QfPur0ERUGopZ46UC9efNm7Ny5E46Ojvjhhx9gZGSE9PR0\nuLi4cO+xsLBAWlpalfNXHB3W1dUVrq6uSk5MSGWFpYXYeXsnNkdvhramNhY4LcCBTw+glXYrvqMR\nArFYDLFYXO/5G704zJkzB6tWrQIAfPnll/j3v/+Nbdu2VfleRXtcNHQ44VNSThJ+vvEzdtzagUGd\nByF0VCgGdx5MRwhEpby747xmzZo6zd/oxcHU9P8u8Jk+fTo8PT0BAObm5khNTeVee/bsGczNzRs7\nHiFVYoxB/FSMkOgQ/JX8F6Y4TEHMzBiIjER8RyNEKRq9OGRkZKB9+7e9NY4cOcL1ZPLy8oK/vz8W\nLVqEtLQ0PHr0CE5OTo0djxA5xWXF+OPuHwi5HgKJTIIFzguwe+xuukczafKUWhz8/Pxw6dIlvHz5\nEh07dsSaNWsgFotx69YtCAQCWFpa4pdffgEAWFtbw9fXF9bW1tDS0kJoaCgdphPepOalIjQmFNtu\nboOzhTN+8PgBw7oMo98kaTaU2pVVGagrK1EWxhiupF5ByPUQnE86j4DeAZjnNA/dWnfjOxoh762u\n204qDqTZeyN5g/B74QiJDkH+m3zMd5qPIPsgCFsK+Y5GSIOh4kBILaXnp+N/Mf/Dr7G/wr6dPRY4\nL8DH3T6GhoAGmCRNT4OOykpIU3T92XWERIfg1KNT8LP1gzhITPdjJuQddORAmoVSaSkOJhxEyPUQ\nPC98jnlO8zDVYSqMdIz4jkZIo6BmJUIqeF74HL/E/IL/xvwXPU16YoHTAoy2Gg1NDU2+oxHSqKhZ\niRAANzNuIuR6CI49PIZPrT9FVEAUepn24jsWIWqDjhxIkyGRSXDk/hGERIcgOTcZ85zmYZrDNLTR\nbcN3NEJ4R0cOpNl5VfQKW29uReiNUIiMRFjovBBjeoyBlgb9vAmpL/rfQ9TW3ay7CIkOwcGEg/Du\n4Y1jE47Bob0D37EIaRKoOBC1IpVJcTzxOEKuh+Dhq4eY6zgXD+c9hKmeac0zE0JqjYoDUQs5xTn4\nPe53bLmxBe302+Ez58/g09MH2prafEcjpEmi4kBU2v0X97E5ejPC74VjlNUo7PtkH5zMabReQpSN\nigNROTImw6lHp7Dp+ibcybqD2Y6zET83Hu2F7fmORkizQcWBqIzXb15jx60d2By9GYYtDfGZ82fw\ntfFFS62WfEcjpNmh4kB49+jVI2y5sQW7bu+Ce1d3hHmH4UOLD+neCYTwiIoD4QVjDGefnEXI9RBE\np0VjRt8ZuDPnDiwMLPiORggBXSFNGllBaQF23d6FkOgQtNBsgc+cP4NfLz+00m7FdzRCmjS6Qpqo\npKScJPx842fsuLUDg0WD8b9R/8OgzoOo6YgQFUXFgSgNYwzip2Jsur4Jl1MuY6rDVMTMjIHISMR3\nNEJIDahZiTS4orIi7Lm7ByHXQyBlUixwWoBJvSdBr4Ue39EIabbofg6EN6l5qQiNCcW2m9vgYuGC\nBc4L4GbpRk1HhKgAOudAGhVjDFdSryDkegjOJ53HZLvJuDrtKrq17sZ3NELIe6AjB1IvJZIS7Lu3\nD5uub0JhWSHmO81HoF0ghC2FfEcjhFShrttODSVmwdSpU2FmZgZbW1tuWnZ2Ntzd3WFlZQUPDw/k\n5uZyr61fvx7du3dHjx49EBUVpcxopJ7S89Ox6uIqiH4SITw+HN8M/Qb3/3Uf85zmUWEgpAlRanGY\nMmUKTp8+LTdtw4YNcHd3R2JiItzc3LBhwwYAQEJCAvbt24eEhAScPn0ac+fOhUwmU2Y8UkvJucnY\nGrsV4/aNQ6/QXsguzoY4SIxTE09hRPcR0BAo9WdECOGBUs85DBw4EE+fPpWbFhERgUuXLgEAAgMD\n4erqig0bNuDYsWPw8/ODtrY2RCIRunXrhujoaLi4uCgzIqlCQWkBxE/FiHochTOPzyCnOAceXT0w\n5oMx+H3M7zDSMeI7IiFEyRr9hHRWVhbMzMwAAGZmZsjKygIApKenyxUCCwsLpKWlVbmM4OBg7rGr\nqytcXV2Vlrc5kDEZbmbcRNTjKEQ9jkJsRiyczJ3g0cUD4T7hsGtnR0cHhKgZsVgMsVhc7/l57a0k\nEAiq7eao6LWKxYHUT2peKs4+OYuox1E49+QczPTN4NHVA8s+WoZBnQfRNQmEqAmpFMjLA7Kz3/7l\n5JQ/doWWlis3HVhTp+U2enEwMzNDZmYm2rVrh4yMDJiavr29o7m5OVJTU7n3PXv2DObm5o0dr8kq\nLC3EpeRL3NHB88LncO/qjuFdh2Ojx0Ya8I4QnhUXV7WBr/lxfj4gFAKtW7/9MzaWf2xuDvTqBYSF\n1S1PoxcHLy8vhIWFYdmyZQgLC4O3tzc33d/fH4sWLUJaWhoePXoEJye641d9yZgMtzNvvy0GT6IQ\nnRYNxw6O8OjigV1jd8GhvQM1FRHSwCruxddlA/92z17xBr51a8DWturphoaApmbN2aZNq9t3Uep1\nDn5+frh06RJevnwJMzMzfPXVVxgzZgx8fX2RkpICkUiE/fv3w8jo7QnOdevW4ffff4eWlhY2bdqE\n4cOHVw5M1zkolJ6fjrOPzyLqSRTOPj6L1q1aw6OrBzy6emBw58HU1ZSQWirfi6/rBl7RXnxVG/V3\nH7dS8sDENHxGM1JUVoS/kv9C1JO3TUXp+elws3SDR1cPuHdxR2ejznxHJIQ35Xvxdd3A5+QAjFW/\ngVe0ka/tXjwfqDg0YYwx3Mm6wzUVXXt2DQ7tHLijg77t+0JTQ0V/mYTUU3Fx/Tbwr1//3158bfbc\nG3Mvng9UHJqYzIJMuaYiYUshhncdDo+uHnAVucKgpQHfEQmpkUymqEdNzY9lMqBNm7pv4FV5L54P\nVBzUXImkBJdTLnO9ipLzkjHUcig8unjAvas7uhh34TsiacZKSuq3gS/fi6/rBt7Y+O1ePA3s+/6o\nOKgZxhjiX8RzxeBK6hX0NusNjy5vm4r6mfeDlgYNnksaTvlevKINenUbe5ms5nb3qh4bGdFePN+o\nOKiB54XPce7JOa4g6GjpYHi34fDo4oEhlkNoeApSK+V78VVtyKvbk8/LA/T1676BL2+Lp7149UTF\nQQW9kbzBldQrXDF4kvMEriJXeHT1wPCuw9G1dVe+IxKeyGRvm1zq01QjldZvA0978c0TFQcVwBjD\ng5cPuIHrLqdchrWJNderyNncGdqa2nzHJA2opKR2e+3vPq64F1/TRv3drpS0F0/qgooDT14WvcT5\nJ+e5aw40BBpcr6KhlkPRulVrviOSGlTci69r18nyvfj69KjRolNKpBFQcWgkpdJS/J36N1cMEl8l\nYnDnwdzRQffW3eneyTx586Z+G/jyvfj69KjR1aW9eKLaqDgoCWMMia8SuQvQ/kz+E1ZtrN4Wgy4e\n+LDjh2ih2aLRczVV5Xvx9bn4qays/j1qaC+eNFVUHBpQdnE2LiRd4E4kS5mUKwZuXdzQVrdto+RQ\nZ2/e1G8Dn5sL6OnV74Qr7cUTUhkVh/dQJi3D9bTrXDFIeJGAgZ0Hctcc9Gjbo1k2FclkbwcUq0+P\nmop78XXtUUN78YQ0HCoOdcAYw+Ocx1wxED8Vo2vrrtzRQf+O/dFSq2WDfJYqULQXX9MGvnwvvjYD\nj737mPbiCVENVBxqkFuSK9dUVCIp4U4iD+syDKZ6pg2YtuExVv9+8eV78XU94Up78YSoPyoO75DI\nJLiRdgNnHp9B1OMo3H1+Fx91/IgrCDYmNrw0FVXci6/LBr6qvfjaPtbTo714QporKg4AknKSuF5F\nF5IuoLNhZ64YDOg0ADpaOg2Spa578RWnlZXVbwNvZARo0/VzhJA6apbF4fWb17iYdJG75uD1m9fc\neYNhXYahvbB9tct8n714Xd36nXClvXhCSGNqFsVBIpUgJj2GOzq4lXkLLuYuGGTugb5GHjCFLXJz\nNGq9sS8trX+PGtqLJ4Sog2ZRHFp8aYwWb8yhn+UBjSQPlDwciLyXutxefF2ba2gvnhDS1NW1OKhl\nH5Tvu9xFN1PzSj1qaC+eEEIahloeOah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ErkJggg==\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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} ], "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": {} } ] }