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diff --git a/Engineering_Heat_Transfer_by_W_S_Janna/CHAPTER9.ipynb b/Engineering_Heat_Transfer_by_W_S_Janna/CHAPTER9.ipynb new file mode 100755 index 00000000..d66004ef --- /dev/null +++ b/Engineering_Heat_Transfer_by_W_S_Janna/CHAPTER9.ipynb @@ -0,0 +1,482 @@ +{
+ "metadata": {
+ "name": "CHAPTER9"
+ },
+ "nbformat": 3,
+ "nbformat_minor": 0,
+ "worksheets": [
+ {
+ "cells": [
+ {
+ "cell_type": "heading",
+ "level": 1,
+ "metadata": {},
+ "source": [
+ "Chapter 9: Heat Exchanger"
+ ]
+ },
+ {
+ "cell_type": "heading",
+ "level": 3,
+ "metadata": {},
+ "source": [
+ "Example 9.1 Page No.458"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "\n",
+ "T1=100.0 \n",
+ "T2=75.0\n",
+ "t1=5.0\n",
+ "t2=50.0\n",
+ "\n",
+ "import math\n",
+ "LMTD_counter=((T1-t2)-(T2-t1))/(math.log((T1-t2)/(T2-t1)))\n",
+ "LMTD_parallel=((T1-t1)-(T2-t2))/(math.log((T1-t1)/(T2-t2)))\n",
+ "\n",
+ "print\"The LMTD for counter flow configuration is \",round(LMTD_counter,1),\"C\"\n",
+ "print\"The LMTD for parallel flow configuration is \",round(LMTD_parallel,2),\"C\""
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "The LMTD for counter flow configuration is 59.4 C\n",
+ "The LMTD for parallel flow configuration is 52.43 C\n"
+ ]
+ }
+ ],
+ "prompt_number": 2
+ },
+ {
+ "cell_type": "heading",
+ "level": 3,
+ "metadata": {},
+ "source": [
+ "Example 9.2 Page No. 459"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "\n",
+ "T1=250\n",
+ "T2=150\n",
+ "t1=100\n",
+ "t2=150\n",
+ "\n",
+ "import math\n",
+ "LMTD_counter=((T1-t2)-(T2-t1))/(math.log((T1-t2)/(T2-t1)));\n",
+ "LMTD_parrelel=0\n",
+ "\n",
+ "print\"The LMTD for counter flow configuration is\",round(LMTD_counter,1),\"C\"\n",
+ "print\"if parallel flow is to give equal outlet temperatures,then the area needed must be infinite which is not feasible economically.\"\n",
+ "print\"The LMTD for parrelel flow configuration is\",LMTD_parrelel,\"C\"\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "The LMTD for counter flow configuration is 72.1 C\n",
+ "if parallel flow is to give equal outlet temperatures,then the area needed must be infinite which is not feasible economically.\n",
+ "The LMTD for parrelel flow configuration is 0 C\n"
+ ]
+ }
+ ],
+ "prompt_number": 8
+ },
+ {
+ "cell_type": "heading",
+ "level": 3,
+ "metadata": {},
+ "source": [
+ "Example 9.3 Page No.463"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "\n",
+ "rou_1= 0.985*62.4 # density in lbm/ft**3 \n",
+ "cp_1=0.9994 # specific heat BTU/(lbm-degree Rankine) \n",
+ "v_1= 0.514e-5 # viscosity in ft**2/s \n",
+ "kf_1 = 0.376 # thermal conductivity in BTU/(hr.ft.degree Rankine) \n",
+ "a_1 = 6.02e-3 # diffusivity in ft**2/hr \n",
+ "Pr_1 = 3.02 # Prandtl Number \n",
+ "m_1=5000 # mass flow rate in lbm/hr\n",
+ "T_1=195 # temperature in degree F\n",
+ "rou_2= 1.087*62.4 # density in lbm/ft**3 \n",
+ "cp_2=0.612 # specific heat BTU/(lbm-degree Rankine) \n",
+ "v_2= 5.11e-5 # viscosity in ft**2/s \n",
+ "kf_2 = 0.150 # thermal conductivity in BTU/(hr.ft.degree Rankine) \n",
+ "a_2 = 3.61e-3 # diffusivity in ft**2/hr \n",
+ "Pr_2 = 51 # Prandtl Number \n",
+ "m_2=12000 # mass flow rate in lbm/hr\n",
+ "T_2=85 # temperature in degree F\n",
+ "ID_a=0.1674\n",
+ "ID_p=0.1076\n",
+ "OD_p=1.375/12\n",
+ "A_p=math.pi*ID_p**2/4\n",
+ "A_a=math.pi*((ID_a)**2-(OD_p)**2)/4\n",
+ "\n",
+ "D_h=ID_a-OD_p\n",
+ "D_e=(ID_a**2-OD_p**2)/(OD_p)\n",
+ "\n",
+ "Re_1=(m_1/3600.0)*(ID_p)/(v_1*rou_1*A_p)\n",
+ "Re_2=(m_2/3600.0)*(D_e)/(v_2*rou_2*A_a)\n",
+ "\n",
+ "Nu_1=0.023*(Re_1)**(4/5.0)*(Pr_1)**0.3\n",
+ "Nu_2=0.023*(Re_2)**(4/5.0)*(Pr_2)**0.4\n",
+ "\n",
+ "h_1i=Nu_1*kf_1/ID_p\n",
+ "h_1o=h_1i*ID_p/OD_p\n",
+ "h_2=Nu_2*kf_2/D_e\n",
+ "\n",
+ "Uo=1/((1/h_1o)+(1/h_2))\n",
+ "R=(m_2*cp_2)/(m_1*cp_1)\n",
+ "L=20\n",
+ "A=math.pi*OD_p*L\n",
+ "T1=195\n",
+ "t1=85\n",
+ "T2=((T1*(R-1))-(R*t1*(1-exp((Uo*A*(R-1))/(m_2*cp_2)))))/(R*exp(Uo*A*(R-1)/(m_2*cp_2))-1)\n",
+ "t2=t1+(T1-T2)/R\n",
+ "print\"The outlet temperature of Ethylene glycol is %.1f degree F\",round(t2,1),\"F\"\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "The outlet temperature of Ethylene glycol is %.1f degree F 99.4 F\n"
+ ]
+ }
+ ],
+ "prompt_number": 14
+ },
+ {
+ "cell_type": "heading",
+ "level": 3,
+ "metadata": {},
+ "source": [
+ "Example 9.4 Page No. 467"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "\n",
+ "rou_1= 1.088 \t\t# density in kg/m**3 \n",
+ "cp_1= 1007\t\t # specific heat in J/(kg*K) \n",
+ "v_1= 18.2e-6\t\t # viscosity in m**2/s \n",
+ "Pr_1 =0.703 \t\t# Prandtl Number \n",
+ "kf_1= 0.02814 \t\t# thermal conductivity in W/(m.K)\n",
+ "a_1 = 0.26e-4 \t\t# diffusivity in m**2/s \n",
+ "m_1=100 \t\t # mass flow rate in kg/hr\n",
+ "t1_air=20+273 \n",
+ "t2_air=80+273\n",
+ "rou_2= 1.0732\t\t # density in kg/m**3 \n",
+ "cp_2= 1013 \t\t# specific heat in J/(kg*K) \n",
+ "v_2= 21.67e-6 \t #viscosity in m**2/s \n",
+ "Pr_2 =0.702 \t\t# Prandtl Number \n",
+ "kf_2= 0.03352 \t\t# thermal conductivity in W/(m.K)\n",
+ "a_2 = 0.3084e-4 \t\t# diffusivity in m**2/s \n",
+ "m_2=90\t\t\t # mass flow rate in kg/hr\n",
+ "T1_CO2=600 \n",
+ "ID_a=.098\n",
+ "ID_p=.07384\n",
+ "OD_p=.07938\n",
+ "\n",
+ "import math\n",
+ "A_p=math.pi*ID_p**(2)/4.0\n",
+ "A_a=math.pi*((ID_a)**2-(OD_p)**2)/4.0\n",
+ "\n",
+ "q_air=(m_1/3600.0)*(cp_1)*(t2_air-t1_air)\n",
+ "T2_CO2=T1_CO2-(q_air/(m_2*cp_2/3600.0))\n",
+ "\n",
+ "LMTD_counter=((T1_CO2-t2_air)-(T2_CO2-t1_air))/(log((T1_CO2-t2_air)/(T2_CO2-t1_air)))\n",
+ "D_h=ID_a-OD_p\n",
+ "D_e=(ID_a**2-OD_p**2)/(OD_p)\n",
+ "\n",
+ "Re_1=(m_1/3600.0)*(ID_p)/(v_1*rou_1*A_p)\n",
+ "Re_2=(m_2/3600.0)*(D_e)/(v_2*rou_2*A_a)\n",
+ "\n",
+ "Nu_1=0.023*(Re_1)**(0.8)*(Pr_1)**0.3\n",
+ "Nu_2=0.023*(Re_2)**(0.8)*(Pr_2)**0.4\n",
+ "\n",
+ "\n",
+ "h_1i=Nu_1*kf_1/ID_p\n",
+ "h_1o=h_1i*ID_p/OD_p\n",
+ "h_2=Nu_2*kf_2/D_e\n",
+ "\n",
+ "Rd_air=0.0004\n",
+ "Rd_CO2=0.002\n",
+ "\n",
+ "Uo=1/((1/h_1o)+(1/h_2))\n",
+ "Uo=1/((1/Uo)+Rd_air+Rd_CO2)\n",
+ "\n",
+ "A=q_air/(Uo*LMTD_counter)\n",
+ "\n",
+ "L=(A/(math.pi*OD_p)) # length of each exchanger\n",
+ "L_available=2 # available exchanger length\n",
+ "N=L_available/L # no. of exchangers\n",
+ "\n",
+ "fp=0.0245 #friction factor for air fom figure 6.14 corresponding to Re\n",
+ "fa=0.033 #friction factor for cCO2fom figure 6.14 corresponding to Re\n",
+ "V_air=(m_1/3600.0)/(rou_1*A_p)\n",
+ "V_CO2=(m_2/3600.0)/(rou_2*A_a)\n",
+ "\n",
+ "dP_p=(fp*L_available*rou_1*V_air**2)/(ID_p*2)\n",
+ "dP_a=((rou_2*V_CO2**2)/2.0)*((fa*L_available/D_h)+1)\n",
+ "\n",
+ "print\"(a)The number of exchangers is \",round(N,0)\n",
+ "print\"(b)The overall exchanger coefficient is \",round(Uo,1),\" W/(sq.m.K)\"\n",
+ "print\"(c)The pressure drop for tube side is \",round(dP_p,2),\"Pa\"\n",
+ "print\"The pressure drop for shell side is \",round(dP_a,1),\"Pa\"\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "(a)The number of exchangers is 1.0\n",
+ "(b)The overall exchanger coefficient is 14.2 W/(sq.m.K)\n",
+ "(c)The pressure drop for tube side is 12.83 Pa\n",
+ "The pressure drop for shell side is 196.7 Pa\n"
+ ]
+ }
+ ],
+ "prompt_number": 24
+ },
+ {
+ "cell_type": "heading",
+ "level": 3,
+ "metadata": {},
+ "source": [
+ "Example 9.5 Page No. 484"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "\n",
+ "rou_1= 0.994*62.4 # density in lbm/ft**3 \n",
+ "cp_1=0.998 # specific heat BTU/(lbm-degree Rankine) \n",
+ "v_1= 0.708e-5 # viscosity in ft**2/s \n",
+ "kf_1 = 0.363 # thermal conductivity in BTU/(hr.ft.degree Rankine) \n",
+ "a_1 = 5.86e-3 # diffusivity in ft**2/hr \n",
+ "Pr_1 = 4.34 # Prandtl Number \n",
+ "m_1=170000 # mass flow rate in lbm/hr\n",
+ "T1=110.0 # temperature in degree F\n",
+ "rou_2= 62.4 # density in lbm/ft**3 \n",
+ "cp_2=0.9988 # specific heat BTU/(lbm-degree Rankine) \n",
+ "v_2= 1.083e-5 # viscosity in ft**2/s \n",
+ "kf_2 = 0.345 # thermal conductivity in BTU/(hr.ft.degree Rankine) \n",
+ "a_2 = 5.54e-3 # diffusivity in ft**2/hr \n",
+ "Pr_2 = 7.02 # Prandtl Number \n",
+ "m_2=150000 # mass flow rate in lbm/hr\n",
+ "t1=65 # temperature in degree F\n",
+ "OD=3/(4*12.0)\n",
+ "ID=0.652/12.0\n",
+ "OD_p=1.375/12.0\n",
+ "Nt=224.0 # from table 9.3\n",
+ "Np=2 # no. of tube passes\n",
+ "Ds=17.25/12.0\n",
+ "Nb=15.0 # no. of baffles\n",
+ "B=1\n",
+ "sT=15/(16*12.0)\n",
+ "C=sT-OD\n",
+ "\n",
+ "import math\n",
+ "At=(Nt*math.pi*ID**2)/(4*Np)\n",
+ "As=(Ds*C*B)/sT\n",
+ "\n",
+ "De=4*((sT/2.0)*(0.86*sT)-(math.pi*OD**2/8.0))/(math.pi*OD/2.0)\n",
+ "\n",
+ "Re_s=(m_1/3600.0)*(De)/(v_1*rou_1*As)\n",
+ "Re_t=(m_2/3600.0)*(ID)/(v_2*rou_2*At)\n",
+ "\n",
+ "Nu_t=0.023*(Re_t)**(0.8)*(Pr_2)**0.4\n",
+ "Nu_s=0.36*(Re_s)**(0.55)*(Pr_1)**(1/3.0)\n",
+ "h_ti=Nu_t*kf_2/ID\n",
+ "h_to=h_ti*ID/OD\n",
+ "h_s=Nu_s*kf_1/De\n",
+ "\n",
+ "Uo=1/((1/h_to)+(1/h_s))\n",
+ "R=(m_2*cp_2)/(m_1*cp_1)\n",
+ "L=16\n",
+ "Ao=Nt*math.pi*OD*L\n",
+ "UoAo_mccp=(Uo*Ao)/(m_2*cp_2)\n",
+ "S=0.58 #value of S from fig. 9.13 Ten Broeck graph corresponding to the value of (UoAo)/(McCpc)\n",
+ "t2=S*(T1-t1)+t1\n",
+ "T2=T1-R*(t2-t1)\n",
+ "ft=0.029 #friction factor for raw water fom figure 6.14 corresponding to Reynolds Number calculated above\n",
+ "fs=0.281 #friction factor for distilled water fom figure 6.14 corresponding to Reynolds Number calculated above\n",
+ "\n",
+ "V_t=(m_2/3600.0)/(rou_2*At)\n",
+ "V_s=(m_1/3600.0)/(rou_1*As)\n",
+ "\n",
+ "gc=32.2\n",
+ "dP_t=(rou_2*V_t**2)*((ft*L*Np/ID)+4*Np)/(2*gc)\n",
+ "dP_s=((rou_1*V_s**2)*(fs*Ds*(Nb+1)))/(2*gc*De)\n",
+ "\n",
+ "print\"Outlet Temperatures of raw water is \",round(t2,1),\"F\"\n",
+ "print\"Outlet Temperatures of distilled water is \",round(T2,1),\"F\"\n",
+ "print\"\\nThe pressure drop for tube side is\",round(dP_t/147,1),\"psi\"\n",
+ "print\"The pressure drop for shell side is\",round(dP_s/147,1),\"psi\"\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": []
+ },
+ {
+ "cell_type": "heading",
+ "level": 3,
+ "metadata": {},
+ "source": [
+ "Example 9.6 Page No.492"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "\n",
+ "m_1=170000 \t\t# mass flow rate in lbm/hr\n",
+ "T1=110 \t\t\t# temperature in degree F\n",
+ "cp_1=0.998\t\t # specific heat BTU/(lbm-degree Rankine) \n",
+ "m_2=150000 \t\t# mass flow rate in lbm/hr\n",
+ "t1=65 \t\t\t# temperature in degree F\n",
+ "cp_2=0.9988\t # specific heat BTU/(lbm-degree Rankine) \n",
+ "Uo=350 \t\t\t# exchanger coefficient\n",
+ "Ao=703.7\n",
+ "mcp_raw=m_2*cp_2\n",
+ "mcp_distilled=m_1*cp_1\n",
+ "\n",
+ "mcp_min_max=mcp_raw/mcp_distilled\n",
+ "UA_mcpmin=(Uo*Ao)/(mcp_raw)\n",
+ "effectiveness=0.58 \t\t#value of effectiveness from figure 9.15 corresponding to the above calculated values of capacitance ratio and (UoAo/mcp_min)\n",
+ "qmax=mcp_raw*(T1-t1)\n",
+ "q=effectiveness*qmax \t# actual heat transfer\n",
+ "t2=(q/mcp_raw)+t1\n",
+ "T2=T1-(q/mcp_distilled)\n",
+ "\n",
+ "print\"The Outlet temperature is Raw Water is\",round(t2,1),\"F\"\n",
+ "print\"The Outlet temperature is disilled Water is\",round(T2,1),\"F\"\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "The Outlet temperature is Raw Water is 91.1 F\n",
+ "The Outlet temperature is disilled Water is 87.0 F\n"
+ ]
+ }
+ ],
+ "prompt_number": 39
+ },
+ {
+ "cell_type": "heading",
+ "level": 3,
+ "metadata": {},
+ "source": [
+ "Example 9.7 Page No. 499"
+ ]
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [
+ "rou_1= 0.852*62.4\t\t # density in lbm/ft**3 \n",
+ "cp_1=0.509\t\t # specific heat BTU/(lbm-degree Rankine) \n",
+ "v_1=0.404e-3 \t\t# viscosity in ft**2/s \n",
+ "kf_1=0.08 \t\t# thermal conductivity in BTU/(hr.ft.degree Rankine) \n",
+ "a_1=2.98e-3 \t# diffusivity in ft**2/hr \n",
+ "Pr_1=490.0 \t\t# Prandtl Number \n",
+ "m_1=39.8 \t\t # mass flow rate in lbm/min\n",
+ "T1=190.0\n",
+ "T2=158.0\n",
+ "rou_2= 0.0653\t\t # density in lbm/ft**3 \n",
+ "cp_2=0.241\t\t # specific heat BTU/(lbm-degree Rankine) \n",
+ "v_2= 20.98e-5 \t\t# viscosity in ft**2/s \n",
+ "kf_2 = 0.01677 \t\t # thermal conductivity in BTU/(hr.ft.degree Rankine) \n",
+ "a_2 = 1.066 \t\t# diffusivity in ft**2/hr \n",
+ "Pr_2 = 0.706 \t\t# Prandtl Number \n",
+ "m_2=67.0 \t\t\t# mass flow rate in lbm/min\n",
+ "t1=126.0\n",
+ "t2=166.0\n",
+ "q_air=m_2*cp_2*60*(t2-t1)\n",
+ "q_oil=m_1*cp_1*60*(T1-T2)\n",
+ "\n",
+ "import math\n",
+ "LMTD=((T1-t2)-(T2-t1))/(math.log((T1-t2)/(T2-t1)))\n",
+ "Area_air=(9.82*8)/144.0\n",
+ "Area_oil=(3.25*9.82)/144.0\n",
+ "\n",
+ "S=(t2-t1)/(T1-t1)\n",
+ "R=(T1-T2)/(t2-t1)\n",
+ "F=0.87 #value of correction factor from figure 9.21a corresponding to above calculated values of S and R\n",
+ "UA=q_air/(F*LMTD)\n",
+ "mcp_air=m_2*cp_2*60\n",
+ "mcp_oil=m_1*cp_1*60\n",
+ "\n",
+ "mcp_min_max=mcp_air/mcp_oil\n",
+ "NTU=(UA/mcp_air)\n",
+ "effectiveness=0.62 \t\t#effectiveness from fig 9.21b corresponding to the values of capacitance ratio \n",
+ "t2_c=(T1-t1)*effectiveness+t1\n",
+ "T2_c=T1-(mcp_air)*(t2_c-t1)/(mcp_oil)\n",
+ "\n",
+ "print\"The Overall Coefficient is \",round(UA,0),\" BTU/(hr. degree R)\"\n",
+ "print\"Calculated outlet temprature are:\"\n",
+ "print\"Outlet temprature for air\",round(t2_c,1),\"F\"\n",
+ "print\"Outlet temprature for Engine Oil\",round(T2_c,0),\"F\"\n",
+ "\n"
+ ],
+ "language": "python",
+ "metadata": {},
+ "outputs": [
+ {
+ "output_type": "stream",
+ "stream": "stdout",
+ "text": [
+ "The Overall Coefficient is 1602.0 BTU/(hr. degree R)\n",
+ "Calculated outlet temprature are:\n",
+ "Outlet temprature for air 165.7 F\n",
+ "Outlet temprature for Engine Oil 158.0 F\n"
+ ]
+ }
+ ],
+ "prompt_number": 21
+ },
+ {
+ "cell_type": "code",
+ "collapsed": false,
+ "input": [],
+ "language": "python",
+ "metadata": {},
+ "outputs": []
+ }
+ ],
+ "metadata": {}
+ }
+ ]
+}
\ No newline at end of file |