From b1f5c3f8d6671b4331cef1dcebdf63b7a43a3a2b Mon Sep 17 00:00:00 2001
From: priyanka
Date: Wed, 24 Jun 2015 15:03:17 +0530
Subject: initial commit / add all books

---
 389/CH6/EX6.1/Example6_1.sce |  55 ++++++++++++++
 389/CH6/EX6.2/Example6_2.sce |  86 ++++++++++++++++++++++
 389/CH6/EX6.3/Example6_3.sce | 169 +++++++++++++++++++++++++++++++++++++++++++
 389/CH6/EX6.4/Example6_4.sce |  53 ++++++++++++++
 389/CH6/EX6.5/Example6_5.sce |  65 +++++++++++++++++
 389/CH6/EX6.6/Example6_6.sce |  72 ++++++++++++++++++
 389/CH6/EX6.7/Example6_7.sce |  64 ++++++++++++++++
 7 files changed, 564 insertions(+)
 create mode 100755 389/CH6/EX6.1/Example6_1.sce
 create mode 100755 389/CH6/EX6.2/Example6_2.sce
 create mode 100755 389/CH6/EX6.3/Example6_3.sce
 create mode 100755 389/CH6/EX6.4/Example6_4.sce
 create mode 100755 389/CH6/EX6.5/Example6_5.sce
 create mode 100755 389/CH6/EX6.6/Example6_6.sce
 create mode 100755 389/CH6/EX6.7/Example6_7.sce

(limited to '389/CH6')

diff --git a/389/CH6/EX6.1/Example6_1.sce b/389/CH6/EX6.1/Example6_1.sce
new file mode 100755
index 000000000..515045c6b
--- /dev/null
+++ b/389/CH6/EX6.1/Example6_1.sce
@@ -0,0 +1,55 @@
+clear;
+clc;
+
+// Illustration 6.1
+// Page: 145
+
+printf('Illustration 6.1 - Page: 145\n\n');
+
+// solution
+
+//****Data****//
+// w = Gas flow rate per orifice
+w = 0.055/50;// [kg/s]
+L = 8*10^(-4);// [liquid flow rate, cubic m/s]
+d = 0.003;// [diameter of the orifice,m]
+viscocity_gas = 1.8*10^(-5);// [kg/m.s]
+//******//
+
+Re = 4*w/(%pi*d*viscocity_gas);
+Dp = 0.0071*Re^(-0.05);// [m]
+h = 3;// [height of vessel,m]
+P_atm = 101.3;// [kN/square m]
+Density_water = 1000;// [kg/cubic m]
+g = 9.81;// [m/s^2]
+Temp = 273+25;// [K]
+P_orifice = P_atm+(h*Density_water*g/1000);// [kN/square m]
+P_avg = P_atm+((h/2)*Density_water*g/1000);// [kN/square m]
+Density_gas = (29/22.41)*(273/Temp)*(P_avg/P_atm);// [kg/cubic m]
+D = 1;// [dia of vessel,m]
+Area = (%pi*D^2)/4;// [square m]
+Vg = 0.055/(Area*Density_gas);// [m/s]
+Vl = L/Area;// [m/s]
+sigma = 0.072;// [N/m]
+// From fig. 6.2 (Pg 143)
+abscissa = 0.0516;// [m/s]
+Vg_by_Vs = 0.11;
+Vs = Vg/Vg_by_Vs;// [m/s]
+deff('[y] = f6(shi_g)','y = Vs-(Vg/shi_g)+(Vl/(1-shi_g))');
+shi_g = fsolve(0.5,f6);
+dp = ((Dp^3)*(P_orifice/P_avg))^(1/3);// [bubble diameter,m]
+// From eqn. 6.9
+a = 6*shi_g/dp;// [specific interfacial area,square m]
+printf("The Specific Interfacial Area is %f square m/cubic m\n",a);
+
+// For diffsion of Cl2 in H20
+Dl = 1.44*10^(-9);// [square m/s]
+viscocity_water = 8.937*10^(-4);// [kg/m.s]
+Reg = dp*Vs*Density_water/viscocity_water;
+Scl = viscocity_water/(Density_water*Dl);
+// From Eqn.6.11
+Shl = 2+(0.0187*(Reg^0.779)*(Scl^0.546)*(dp*(g^(1/3))/(Dl^(2/3)))^0.116);
+// For dilute soln. of Cl2 in H20
+c = 1000/18.02;// [kmol/cubic m]
+Fl = (c*Dl*Shl)/dp;// [kmol/square m.s]
+printf("Mass Transfer coeffecient is %f kmol/square m.s\n",Fl);
\ No newline at end of file
diff --git a/389/CH6/EX6.2/Example6_2.sce b/389/CH6/EX6.2/Example6_2.sce
new file mode 100755
index 000000000..70e02ecd3
--- /dev/null
+++ b/389/CH6/EX6.2/Example6_2.sce
@@ -0,0 +1,86 @@
+clear;
+clc;
+
+// Illustration 6.2
+// Page: 157
+
+printf('Illustration 6.2 - Page: 157\n\n');
+
+// solution
+
+//****Data****//
+// a = N2 b = H2O
+L = 9.5*10^(-4);// [cubic m/s]
+G = 0.061;// [kg/s]
+Temp = 273+25;// [K]
+//*****//
+
+printf("Construction Arrangement\n");
+printf("Use 4 vertical wall baffles, 100 mm wide at 90 degree intervals.\n");
+printf("Use a 305 mm dameter, a six bladed disk flat blade turbine impeller, arranged axially, 300 mm from the bottom of vessel\n");
+printf("The sparger underneath the impeller will be in the form of a 240 mm dameter ring made of 12.7 mm tubing drilled in the top with 3.18 mm dia holes\n");
+Di = 0.305;// [m]
+Do = 0.00316;// [m]
+viscocity_a = 1.8*10^(-5);// [kg/m.s]
+Re_g = 35000;
+Ma = 28.02;// [kg/kmol]
+Mb = 18.02;// [kg/kmol]
+// w = Gas flow rate per orifice
+w = Re_g*%pi*Do*viscocity_a/4;// [kg/s]
+N_holes = G/w;
+Interval = %pi*240/round(N_holes);
+printf("The number of holes is %d at approx %d mm interval around the sparger ring\n",round(N_holes),round(Interval));
+
+viscocity_b = 8.9*10^(-4);// [kg/m.s]
+Sigma = 0.072;// [N/m]
+Density_b = 1000;// [kg/cubic m]
+D = 1;// [dia of vessel,m]
+g = 9.81;// [m/s^2]
+// From Eqn. 6.18
+deff('[y] = f7(N)','y = (N*Di/(Sigma*g/Density_b)^0.25)-1.22-(1.25*D/Di)');
+N_min = fsolve(2,f7);// [r/s]
+N = 5;// [r/s]
+Re_l = ((Di^2)*N*Density_b/viscocity_b);
+// From fig 6.5 (Pg 152)
+Po = 5;
+P = Po*Density_b*(N^3)*(Di^5);
+h = 0.7;// [m]
+P_atm = 101.33;// [kN/square m]
+P_gas = P_atm+(h*Density_b*g/1000);// [kN/square m]
+Qg = (G/Ma)*22.41*(Temp/273)*(P_atm/P_gas);// [cubic m/s]
+// From Fig.6.7 (Pg 155)
+abcissa = Qg/(N*(Di^3));
+// abcissa is off scale
+Pg_by_P = 0.43;
+Pg = 0.43*P;// [W]
+Vg = Qg/(%pi*(D^2)/4);// [superficial gas velocity,m/s]
+check_value = (Re_l^0.7)*((N*Di/Vg)^0.3);
+vl = %pi*(D^2)/4;// [cubic m]
+// Since value<30000
+// From Eqn. 6.21, Eqn.6.23 & Eqn. 6.24
+K = 2.25;
+m = 0.4;
+Vt = 0.250;// [m/s]
+shi = 1;
+err = 1;
+while (err>10^(-3))
+    a = 1.44*((Pg/vl)^0.4)*((Density_b/(Sigma^3))^0.2)*((Vg/Vt)^0.5);// [square m/cubic m]
+    shin = (0.24*K*((viscocity_a/viscocity_b)^0.25)*((Vg/Vt)^0.5))^(1/(1-m));
+    Dp = K*((vl/Pg)^0.4)*((Sigma^3/Density_b)^0.2)*(shin^m)*((viscocity_a/viscocity_b)^0.25);// [m]
+    err = abs(shi-shin);
+    Vt = Vt-0.002;// [m/s]
+    shi = shin;
+end
+
+// For N2 in H2
+Dl = 1.9*10^(-9);// [square m/s]
+Ra = 1.514*10^(6);
+// By Eqn. 6.25
+Shl = 2.0+(0.31*(Ra^(1/3)));
+// For dilute soln.
+c = 1000/Mb;// [kmol/cubic m]
+Fl = Shl*c*Dl/Dp;// [kmol/square m.s]
+printf("The average gas-bubble diameter is %e m\n",Dp);
+printf("Gas Holdup:%f\n",shi);
+printf("Interfacial area:%e square m/cubic m \n",a);
+printf("Mass transfer coeffecient:%e kmol/square m.s\n",Fl);
\ No newline at end of file
diff --git a/389/CH6/EX6.3/Example6_3.sce b/389/CH6/EX6.3/Example6_3.sce
new file mode 100755
index 000000000..f18c23bdf
--- /dev/null
+++ b/389/CH6/EX6.3/Example6_3.sce
@@ -0,0 +1,169 @@
+clear;
+clc;
+
+// Illustration 6.3
+// Page: 174
+
+printf('Illustration 6.3 - Page: 174\n\n');
+
+// solution
+
+//****Data****//
+// a = methanol b = water
+G = 0.100;// [kmol/s]
+L = 0.25;// [kmol/s]
+Temp = 273+95;// [K]
+XaG = 0.18;// [mol % in gas phase]
+MaL = 0.15;// [mass % in liquid phase]
+//*****//
+
+Ma = 32;// [kg/kmol]
+Mb = 18;// [kg/kmol]
+Mavg_G = XaG*Ma+((1-XaG)*Mb);// [kg/kmol]
+Density_G = (Mavg_G/22.41)*(273/Temp);// [kg/cubic cm]
+Q = G*22.41*(Temp/273);// [cubic cm/s]
+Density_L = 961;// [kg/cubic cm]
+Mavg_L = 1/((MaL/Ma)+(1-MaL)/Mb);// [kg/kmol]
+q = L*Mavg_L/Density_L;
+
+// Perforations
+printf("Perforations\n");
+printf("Do = 4.5mm on an equilateral triangle pitch 12 mm between the hole centres, punched in sheet metal 2 mm thick\n");
+Do = 0.0045;// [m]
+pitch = 0.012;// [m]
+// By Eqn.6.31
+Ao_by_Aa = 0.907*(Do/pitch)^2;
+printf("The ratio of Hole Area By Active Area is:%f\n",Ao_by_Aa);
+printf("\n");
+
+// Tower Diameter
+printf("Tower Diameter\n");
+t = 0.50;// [tray spacing,m]
+printf("Tower Spacing:%f m\n",t);
+// abcissa = (L/G)*(Density_G/Density_L)^0.5 = (q/Q)*(Density_L/Density_G)^0.5
+abcissa = (q/Q)*(Density_L/Density_G)^0.5;
+// From Table 6.2 (Pg 169)
+alpha = (0.0744*t)+0.01173;
+beeta = (0.0304*t)+0.015;
+if (abcissa<0.1) 
+    abcissa = 0.1;
+end
+sigma = 0.040;// [N/m]
+// From Eqn.6.30
+Cf = ((alpha*log10(1/abcissa))+beeta)*(sigma/0.02)^0.2;
+// From Eqn. 6.29
+Vf = Cf*((Density_L-Density_G)/Density_G)^(1/2);// [m/s]
+// Using 80% of flooding velocity
+V = 0.8*Vf;// [m/s]
+An = Q/V;// [square m]
+// The tray area used by one downspout = 8.8%
+At = An/(1-0.088);// [square m]
+D = (4*At/%pi)^(1/2);// [m]
+// Take D = 1.25 m
+D = 1.25; //[m]
+At = %pi*(D^2)/4;// [corrected At, square m]
+W = 0.7*D;// [weir length,m]
+Ad = 0.088*At;// [square m]
+// For a design similar to Fig 6.14 (Pg 168)
+// A 40 mm wide supporting ring, beams between downspouts and a 50 mm wide disengaging & distributing zones these areas total 0.222 square m
+Aa = At-(2*Ad)-0.222;
+printf("Weir Length:%f\n",W);
+printf("Area for perforated sheet: %f square m\n",Aa);
+printf("\n");
+
+// Weir crest h1 & Weir height hw
+printf("Weir crest h1 & Weir height hw\n")
+h1 = 0.025;// [m]
+h1_by_D = h1/D;
+D_by_W = D/W;
+// From Eqn. 6.34
+Weff_by_W = sqrt(((D_by_W)^2)-((((D_by_W)^2-1)^0.5)+(2*h1_by_D*D_by_W))^2);
+// Set hw to 50 mm
+hw = 0.05;// [m]
+printf("Weir crest: %f m\n",h1);
+printf("Weir height: %f m\n",hw);
+printf("\n");
+
+// Dry Pressure Drop
+printf("Dry Pressure Drop\n");
+l = 0.002;// [m]
+// From Eqn. 6.37
+Co = 1.09*(Do/l)^0.25;
+Ao = 0.1275*Aa;// [square m]
+Vo = Q/Ao;// [m/sec]
+viscocity_G = 1.25*10^(-5);// [kg/m.s]
+Re = Do*Vo*Density_G/viscocity_G;
+// From "The Chemical Engineers Handbook," 5th Edition fig 5.26
+fr = 0.008;
+g = 9.81;// [m/s^2]
+// From Eqn. 6.36
+deff('[y] = f(hd)','y = (2*hd*g*Density_L/(Vo^2*Density_G))-(Co*(0.40*(1.25-(Ao/An))+(4*l*fr/Do)+(1-(Ao/An))^2))');
+hd = fsolve(1,f);
+printf("Dry Pressure Drop:%f m\n",hd);
+printf("\n");
+
+// Hydraulic head hl
+printf("Hydraulic head hl");
+Va = Q/Aa;// [m/s]
+z = (D+W)/2;// [m]
+// From Eqn. 6.38
+hl = 6.10*10^(-3)+(0.725*hw)-(0.238*hw*Va*(Density_G)^0.5)+(1.225*q/z);// [m]
+printf("Hydraulic head: %f m\n",hl);
+printf("\n");
+
+//Residual Pressure drop hr
+printf("Residual Pressure drop hr\n");
+// From Eqn. 6.42
+hr = 6*sigma/(Density_L*Do*g);// m
+printf("Residual Pressure Drop:%e m\n",hr);
+printf("\n");
+
+// Total Gas pressure Drop hg
+printf("Total Gas pressure Drop hg\n")
+// From Eqn. 6.35
+hg = hd+hl+hr;// [m]
+printf("Total gas pressure Drop: %f m\n",hg);
+printf("\n");
+
+// Pressure loss at liquid entrance h2
+printf("Pressure loss at liquid entrance h2\n");
+// Al: Area for the liquid flow under the apron
+Al = 0.025*W;// [square m]
+Ada = min(Al,Ad);
+// From Eqn. 6.43
+h2 = (3/(2*g))*(q/Ada)^2;
+printf("Pressure loss at liquid entrance:%e m\n",h2);
+printf("\n");
+
+// Backup in Downspout h3
+printf("Backup in Downspout h3\n");
+// From Eqn.6.44
+h3 = hg+h2;
+printf("Backup in Downspout:%f m\n",h3);
+printf("\n");
+
+// Check on Flooding
+printf("Check on Flooding\n");
+if((hw+h1+h3)<(t/2))
+    printf("Choosen Tower spacing is satisfactory\n");
+else
+    printf("Choosen Tower spacing is  not satisfactory\n")
+end
+printf("\n");
+
+// Weeping Velocity
+printf("Weeping Velocity\n");
+printf("For W/D ratio %f weir is set at %f m from the center from the tower\n",W/D,0.3296*D);
+Z = 2*(0.3296*D);// [m]
+// From Eqn.6.46
+deff('[y] = f8(Vow)','y = (Vow*viscocity_G/(sigma))-(0.0229*((viscocity_G^2/(sigma*Density_G*Do))*(Density_L/Density_G))^0.379)*((l/Do)^0.293)*(2*Aa*Do/(sqrt(3)*(pitch^3)))^(2.8/((Z/Do)^0.724))');
+Vow = fsolve(0.1,f8);// [m/s]
+printf("The minimum gas velocity through the holes below which excessive weeping is likely: %f m/s\n",Vow);
+printf("\n");
+
+// Entrainment
+printf("Entrainment\n");
+V_by_Vf = V/Vf;
+// From Fig.6.17 (Pg 173), V/Vf = 0.8 & abcissa = 0.0622
+E = 0.05;
+printf("Entrainment:%f\n",E);
\ No newline at end of file
diff --git a/389/CH6/EX6.4/Example6_4.sce b/389/CH6/EX6.4/Example6_4.sce
new file mode 100755
index 000000000..e10305aca
--- /dev/null
+++ b/389/CH6/EX6.4/Example6_4.sce
@@ -0,0 +1,53 @@
+clear;
+clc;
+
+// Illustration 6.4
+// Page: 183
+
+printf('Illustration 6.4 - Page: 183\n\n');
+
+// solution
+
+//****Data****//
+//From Illustrtion 6.3:
+G = 0.100;// [kmol/s]
+Density_G = 0.679;// [kg/cubic m]
+q = 5*10^(-3);// [cubic m/s]
+Va = 3.827;// [m/s]
+z = 1.063;// [m]
+L = 0.25;// [kmol/s]
+hL = 0.0106;// [m]
+hW = 0.05;// [m]
+Z = 0.824;// [m]
+E = 0.05;
+ya = 0.18;// [mole fraction methanol]
+
+// a:CH3OH b:H2O
+Ma = 32;// [kg/kmol]
+Mb = 18;// [kg/kmol]
+// From Chapter 2:
+ScG = 0.865;
+Dl = 5.94*10^(-9);// [square m/s]
+// From Eqn. 6.61:
+NtG = (0.776+(4.57*hW)-(0.238*Va*Density_G^0.5)+(104.6*q/Z))/ScG^0.5;
+DE = ((3.93*10^(-3))+(0.0171*Va)+(3.67*q/Z)+(0.1800*hW))^2;// [square m/s]
+thethaL = hL*z*Z/q;// [s]
+NtL = 40000*Dl^0.5*((0.213*Va*Density_G^0.5)+0.15)*thethaL;
+// For 15 mass% methanol:
+xa = (15/Ma)/((15/Ma)+(85/Mb));
+// From Fig 6.23 (Pg 184)
+mAC = -(NtL*L)/(NtG*G);// [Slope of AC line]
+meqb = 2.50;// [slope of equilibrium line]
+// From Eqn. 6.52:
+NtoG = 1/((1/NtG)+(meqb*G/L)*(1/NtL));
+// From Eqn. 6.51:
+EOG = 1-exp(-NtoG);
+// From Eqn. 6.59:
+Pe = Z^2/(DE*thethaL);
+// From Eqn. 6.58:
+eta = (Pe/2)*((1+(4*meqb*G*EOG/(L*Pe)))^0.5-1);
+// From Eqn. 6.57:
+EMG = EOG*(((1-exp(-(eta+Pe)))/((eta+Pe)*(1+(eta+Pe)/eta)))+(exp(eta)-1)/(eta*(1+eta/(eta+Pe))));
+// From Eqn. 6.60:
+EMGE = EMG/(1+(EMG*E/(1-E)));
+printf("Effeciency of Sieve trays: %f",EMGE);
\ No newline at end of file
diff --git a/389/CH6/EX6.5/Example6_5.sce b/389/CH6/EX6.5/Example6_5.sce
new file mode 100755
index 000000000..d10ecdec1
--- /dev/null
+++ b/389/CH6/EX6.5/Example6_5.sce
@@ -0,0 +1,65 @@
+clear;
+clc;
+
+// Illustration 6.5
+// Page: 200
+
+printf('Illustration 6.5 - Page: 200\n\n');
+
+// solution
+
+// ****Data****//
+G = 0.80;// [cubic m/s]
+P = 10^2;// [kN/square m]
+XaG = 0.07;
+Temp = 273+30;// [K]
+L = 3.8;// [kg/s]
+Density_L = 1235;// [kg/cubic m]
+viscocity_L = 2.5*10^(-3);// [kg/m.s]
+//******//
+
+// a = SO2 b = air
+
+// Solution (a) 
+
+// Since the larger flow quantities are at the bottom for an absorber, the diameter will be choosen to accomodate the bottom condition
+Mavg_G = XaG*64+((1-XaG)*29);// [kg/kmol]
+G1 = G*(273/Temp)*(P/101.33)*(1/22.41);// [kmol/s]
+G2 = G1*Mavg_G;// [kg/s]
+Density_G = G2/G;// [kg/cubic m]
+// Assuming Complete absorption of SO2
+sulphur_removed = G1*XaG*64;// [kg/s]
+abcissa = (L/G)*((Density_G/Density_L)^0.5);
+//From Fig. 6.24, using gas pressure drop of 400 (N/square m)/m
+ordinate = 0.061;
+// For 25 mm ceramic Intalox Saddle:
+Cf = 98;// [Table 6.3 Pg 196]
+J = 1;
+G_prime = (ordinate*Density_G*(Density_L-Density_G)/(Cf*viscocity_L^0.1*J))^0.5;// [kg/square m.s]
+A = G2/G_prime;// [square m]
+D = (4*A/%pi)^0.5;// [m]
+printf("The Tower Diameter is %f m\n",D);
+
+// Solution (b)
+
+// Let
+D = 1;// [m]
+A = %pi*D^2/4;// [square m]
+// The pressure drop for 8 m of irrigated packing
+delta_p = 400*8;// [N/square m]
+// For dry packing
+G_prime = (G2-sulphur_removed)/A;// [kg/square m.s]
+P = P-(delta_p/1000);// [kN/square m]
+Density_G = (29/22.41)*(273/Temp)*(P/101.33);// [kg/cubic m]
+// From Table 6.3 (Pg 196)
+Cd = 241.5;
+// From Eqn. 6.68
+delta_p_by_z = Cd*G_prime^2/Density_G;// [N/square m for 1m of packing]
+pressure_drop = delta_p+delta_p_by_z;// [N/square m]
+V = 7.5;// [m/s]
+head_loss = 1.5*V^2/2;// [N.m/kg]
+head_loss = head_loss*Density_G;// [N/square m]
+Power = (pressure_drop+head_loss)*(G2-sulphur_removed)/(Density_G*1000);// [kW]
+eta = 0.6;
+Power = Power/eta;// [kW]
+printf("The Power for the fan motor is %f kW\n",Power);
\ No newline at end of file
diff --git a/389/CH6/EX6.6/Example6_6.sce b/389/CH6/EX6.6/Example6_6.sce
new file mode 100755
index 000000000..0e38ff926
--- /dev/null
+++ b/389/CH6/EX6.6/Example6_6.sce
@@ -0,0 +1,72 @@
+clear;
+clc;
+
+// Illustration 6.6
+// Page: 204
+
+printf('Illustration 6.6 - Page: 204\n\n');
+
+// solution
+
+//****Data****//
+// Gas
+Mavg_G = 11;// [kg/kmol]
+viscocity_G = 10^(-5);// [kg/m.s]
+Pt = 107;// [kN/square m]
+Dg = 1.30*10^(-5);// [square m/s]
+Temp = 273+27;// [K]
+G_prime = 0.716;// [kg/square m.s]
+
+// Liquid:
+Mavg_L = 260;
+viscocity_L = 2*10^(-3);// [kg/m.s]
+Density_L = 840;// [kg/cubic m]
+sigma = 3*10^(-2);// [N/m]
+Dl = 4.71*10^(-10);// [square m/s]
+//******//
+
+//Gas:
+Density_G = (Mavg_G/22.41)*(Pt/101.33)*(273/Temp);// [kg/cubic m]
+ScG = viscocity_G/(Density_G*Dg);
+G = G_prime/Mavg_G;// [kmol/square m.s]
+
+// Liquid:
+L_prime = 2.71;// [kg/square m.s]
+ScL = viscocity_L/(Density_L*Dl);
+
+// Holdup:
+// From Table 6.5 (Pg 206), L_prime = 2.71 kg/square m.s
+Ds = 0.0472;// [m]
+beeta = 1.508*Ds^0.376;
+shiLsW = 5.014*10^(-5)/Ds^1.56;// [square m/cubic m]
+shiLtW = (2.32*10^(-6))*(737.5*L_prime)^beeta/(Ds^2);// [square m/cubic m]
+shiLoW = shiLtW-shiLsW;// [square m/cubic m]
+H = (1404*(L_prime^0.57)*(viscocity_L^0.13)/((Density_L^0.84)*((3.24*L_prime^0.413)-1)))*(sigma/0.073)^(0.2817-0.262*log10(L_prime));
+shiLo = shiLoW*H;// [square m/cubic m]
+shiLs = 4.23*10^(-3)*(viscocity_L^0.04)*(sigma^0.55)/((Ds^1.56)*(Density_L^0.37));// [square m/cubic m]
+shiLt = shiLo+shiLs;// [square m/cubic m]
+
+// Interfacial Area:
+// From Table 6.4 (Pg 205)
+m = 62.4;
+n = (0.0240*L_prime)-0.0996;
+p = -0.1355;
+aAW = m*((808*G_prime/(Density_G^0.5))^n)*(L_prime^p);// [square m/cubic m]
+// From Eqn. 6.73
+aA = aAW*shiLo/shiLoW;// [square m/cubic m]
+// From Table 6.3 (Pg 196)
+e = 0.75;
+// From Eqn. 6.71
+eLo = e-shiLt;
+// From Eqn. 6.70
+deff('[y] = f9(Fg)','y = ((Fg*ScG^(2/3))/G)-1.195*((Ds*G_prime)/(viscocity_G*(1-eLo)))^(-0.36)');
+Fg = fsolve(1,f9);// [kmol/square m.s]
+// From Eqn. 6.72:
+deff('[y] = f10(Kl)','y = (Kl*Ds/Dl)-(25.1*(Ds*L_prime/viscocity_L)^0.45)*ScL^0.5');
+Kl = fsolve(1,f10);// [(kmol/square m.s).(kmol/cubic m)]
+// Since the value of Kl is taken at low conc., it can be converted into Fl
+c = (Density_L/Mavg_L);// [kmol/cubic m]
+Fl = Kl*c;// [kmol/cubic m]
+printf("The volumetric coeffecients are\n");
+printf("Based on Gas Phase %f kmol/cubic m.s\n",Fg*aA);
+printf("based on Liquid Phase %f kmol/cubic m.s\n",Fl*aA);
\ No newline at end of file
diff --git a/389/CH6/EX6.7/Example6_7.sce b/389/CH6/EX6.7/Example6_7.sce
new file mode 100755
index 000000000..e9e8ddfde
--- /dev/null
+++ b/389/CH6/EX6.7/Example6_7.sce
@@ -0,0 +1,64 @@
+clear;
+clc;
+
+// Illustration 6.7
+// Page: 207
+
+printf('Illustration 6.7 - Page: 207\n\n');
+
+// solution
+
+//****Data****//
+// Air
+G_prime = 1.10;// [kg/square m.s]
+viscocity_G = 1.8*10^(-5);// [kg/m.s]
+ScG = 0.6;// [for air water mixture]
+Temp1 = 273+20;// [K]
+
+// Water
+L_prime = 5.5;// [kg/square m.s]
+//*****//
+
+// Air:
+Ma = 29;// [kg/kmol]
+G = G_prime/Ma;// [kmol/square m.s]
+Density_G = (Ma/22.41)*(273/Temp1);
+Cpa = 1005;// [N.m/kg.K]
+PrG = 0.74;
+
+// Liquid:
+kth = 0.587;// [W/m.K]
+Cpb = 4187;// [N.m/kg.K]
+viscocity_L = 1.14*10^(-3);// [kg/m.s]
+
+// From Table 6.5 (Pg 206)
+Ds = 0.0725;// [m]
+beeta = 1.508*(Ds^0.376);
+shiLtW = (2.09*10^(-6))*(737.5*L_prime)^beeta/(Ds^2);// [square m/cubic m]
+shiLsW = 2.47*10^(-4)/(Ds^1.21);// [square m/cubic m]
+shiLoW = shiLtW-shiLsW;// [square m/cubic m]
+// From Table 6.4 (Pg 205)
+m = 34.03;
+n = 0;
+p = 0.362;
+aAW = m*(808*G_prime/Density_G^0.5)^(n)*L_prime^p;// [square m/cubic m]
+// From Eqn. 6.75
+aVW = 0.85*aAW*shiLtW/shiLoW;// [square m/cubic m]
+// From Table 6.3
+e = 0.74;
+eLo = e-shiLtW;
+// From Eqn. 6.70
+deff('[y] = f11(Fg)','y = ((Fg*ScG^(2/3))/G)-1.195*((Ds*G_prime)/(viscocity_G*(1-eLo)))^(-0.36)');
+Fg = fsolve(1,f11);// [kmol/square m.s]
+// Since the liquid is pure water. It has no mass trnsfer coeffecient.
+// For such process we need convective heat transfer coeffecient for both liquid & gas.
+// Asuming Jd = Jh
+// From Eqn. 6.70
+Jh = 1.195*((Ds*G_prime)/(viscocity_G*(1-eLo)))^(-0.36);
+Hg = Jh*Cpa*G_prime/(PrG^(2/3));// [W/square m.K]
+PrL = Cpb*viscocity_L/kth;
+// Heat transfer analog of Eqn. 6.72
+Hl = 25.1*(kth/Ds)*(Ds*L_prime/viscocity_L)^0.45*PrL^0.5;// [W/square m.K]
+printf("The volumetric coeffecients are\n");
+printf("Based on Gas Phase %f W/cubic m.K\n",Hg*aVW);
+printf("based on Liquid Phase %f W/cubic m.K\n",Hl*aVW);
\ No newline at end of file
-- 
cgit