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