2 files changed, 156 insertions, 155 deletions
diff --git a/839/CH22/EX22.5/Example_22_5.sce b/839/CH22/EX22.5/Example_22_5.sce
index 76d8d4dfa..685e0f917 100755
--- a/839/CH22/EX22.5/Example_22_5.sce
+++ b/839/CH22/EX22.5/Example_22_5.sce
@@ -1,99 +1,99 @@
-//clear//
-clear;
-clc;
-
-//Example 22.5
-//Solution
-//Equlibrium data are shown in Fig.22.22
-//By a heat balance similar to that of Eample 22.3
-//The temperature rise of the liqui was estimated
-//to be
-delta_T = 12.5; //[C]
-//Basis:
-dry_gas_in = 100; //[mol]
-sol_in = 140; //[mol]
-N2_in = 87; //[mol]
-CO2_in = 10; //[mol]
-EO_in = 3; //[mol]
-N2_out = 87; //[mol]
-CO2_out = 10; //[mol]
-EO_out = 3*0.02; //[mol]
-IN = N2_in+CO2_in+EO_in; //[mol]
-OUT = N2_out+CO2_out+EO_out; //[mol]
-//Assuming negligible CO2 absorption and neglect effect of H2O on
-//gas composition.
-//At top:
-xt = 0.004;
-yt = EO_out/OUT;
-//Moles of EO absorbed
-EO_abs = 3*0.98; //[mol]
-//Moles of EO absorbed in water
-EO_H2O = 140*0.0004; //[mol]
-//At bottom:
-xb = (EO_abs+EO_H2O)/(140+EO_abs);
-yb = 0.03;
-//From Fig 22.22
-y = [0.03,0.015,0.005,0.0006]';
-delta_y1 = [0.008,0.0006,0.0024,0.0003]';
-
-for i = 1:length(y)-1
-  delta_y = y(i)-y(i+1);
-  delta_yL = (delta_y1(i)-delta_y1(i+1))/log(delta_y1(i)/delta_y1(i+1));
-  Noy1(i) = delta_y/delta_yL;
-end
-Noy = sum(Noy1);
-
-//Column diameter:
-//Using generalize pressure-drop correlation, Fig.22.6
-//Based on the inlet gas,
-Mbar = 0.87*28+0.1*44+0.03*44;
-//At 40C,
-rho_y = 30.1/359*20*273/313 //[lb/ft^3]
-rho_x = 62.2; //[lb/ft^3]
-//Let A = Gx/Gy*sqrt(rho_y/(rho_x-rho_y))
-A = 1.4*18/(1*30.1)*sqrt(rho_y/(rho_x-rho_y));
-//From Fig. 22.6, for
-delta_P = 0.5; //[in.H2O/ft]
-//Let B = Gy^2*Fp*mux^0.1/(rho_y*(rho_x-rho_y)*gc)
-B = 0.045;
-//From Table 22.1,
-Fp = 40;
-mu = 0.656; //[cP]
-//so 
-Gy = sqrt(B*(rho_y)*(rho_x-rho_y)*32.2/(Fp*mu^0.1)); //[lb/ft^2-h]
-//or 
-Gy = Gy*3600; //[lb/ft^2-s]
-Gx = 1.4*18/(1*Mbar)*Gy; //[lb/f^2-s]
-//For a feed rate 
-F = 10000*Mbar; //[lb/h]
-S = F/Gx; //[ft^2]
-D = sqrt(S*4/%pi); //[ft]
-//Column heigth:
-//From Fig. 22.20 at Gy = 500 and Gx = 1500
-Hy_NH3 = 1.4; //[ft]
-mu_40 =0.0181*10^-2; //[P], Appendix 8
-Dv = 7.01*10^-3; //[cm^2/s], from Eq.(21.25)
-rho = 2.34*10^-2; //[lb/ft^3]
-Nsc = mu_40/(rho*Dv);
-//Form Table 22.1,
-fp = 1.36;
-Hy_EO = 1.4*(1.1/0.66)^0.5*1/1.36*(Gy/500)^0.3*(1500/Gx)^0.4; //[ft]
-//Form Fig. 22.19,
-Hx_O2 = 0.9; //[ft]
-Gx1 = 1500;
-mu1 = 0.00656; //[P]
-rho1 = 1; //[lb/ft^3]
-//Using Eq.(21.28)
-Dv1 = 2.15*10^-5; //[cm^2/s]
-Nsc1 = mu1/(rho1*Dv1);
-//Using Eq.(22.35), with the correction factor fp and Nsc = 381, 
-//for O2 in water at 25 C
-Hx_EO = Hx_O2*(Gx/(mu1*100)/(Gx1/0.894))^0.3*(Nsc1/381)^0.5/1.36; //[ft]
-//From Fig 22.22, the average value of m
-m = 1.0;
-//From Eq.(22.30)
-HOy = 1.71+(1*0.96)/1.4; //[ft] 
-
-disp(NOy,'number of transfer units required')
-disp('ft',D,'diameter of the column')
-disp('ft',HOy,'packing height')
+//clear//
+clear;
+clc;
+
+//Example 22.5
+//Solution
+//Equlibrium data are shown in Fig.22.22
+//By a heat balance similar to that of Eample 22.3
+//The temperature rise of the liqui was estimated
+//to be
+delta_T = 12.5; //[C]
+//Basis:
+dry_gas_in = 100; //[mol]
+sol_in = 140; //[mol]
+N2_in = 87; //[mol]
+CO2_in = 10; //[mol]
+EO_in = 3; //[mol]
+N2_out = 87; //[mol]
+CO2_out = 10; //[mol]
+EO_out = 3*0.02; //[mol]
+IN = N2_in+CO2_in+EO_in; //[mol]
+OUT = N2_out+CO2_out+EO_out; //[mol]
+//Assuming negligible CO2 absorption and neglect effect of H2O on
+//gas composition.
+//At top:
+xt = 0.004;
+yt = EO_out/OUT;
+//Moles of EO absorbed
+EO_abs = 3*0.98; //[mol]
+//Moles of EO absorbed in water
+EO_H2O = 140*0.0004; //[mol]
+//At bottom:
+xb = (EO_abs+EO_H2O)/(140+EO_abs);
+yb = 0.03;
+//From Fig 22.22
+y = [0.03,0.015,0.005,0.0006]';
+delta_y1 = [0.008,0.0006,0.0024,0.0003]';
+
+for i = 1:length(y)-1
+  delta_y = y(i)-y(i+1);
+  delta_yL = (delta_y1(i)-delta_y1(i+1))/log(delta_y1(i)/delta_y1(i+1));
+  Noy1(i) = delta_y/delta_yL;
+end
+Noy = sum(Noy1);
+
+//Column diameter:
+//Using generalize pressure-drop correlation, Fig.22.6
+//Based on the inlet gas,
+Mbar = 0.87*28+0.1*44+0.03*44;
+//At 40C,
+rho_y = 30.1/359*20*273/313 //[lb/ft^3]
+rho_x = 62.2; //[lb/ft^3]
+//Let A = Gx/Gy*sqrt(rho_y/(rho_x-rho_y))
+A = 1.4*18/(1*30.1)*sqrt(rho_y/(rho_x-rho_y));
+//From Fig. 22.6, for
+delta_P = 0.5; //[in.H2O/ft]
+//Let B = Gy^2*Fp*mux^0.1/(rho_y*(rho_x-rho_y)*gc)
+B = 0.045;
+//From Table 22.1,
+Fp = 40;
+mu = 0.656; //[cP]
+//so 
+Gy = sqrt(B*(rho_y)*(rho_x-rho_y)*32.2/(Fp*mu^0.1)); //[lb/ft^2-h]
+//or 
+Gy = Gy*3600; //[lb/ft^2-s]
+Gx = 1.4*18/(1*Mbar)*Gy; //[lb/f^2-s]
+//For a feed rate 
+F = 10000*Mbar; //[lb/h]
+S = F/Gx; //[ft^2]
+D = sqrt(S*4/%pi); //[ft]
+//Column heigth:
+//From Fig. 22.20 at Gy = 500 and Gx = 1500
+Hy_NH3 = 1.4; //[ft]
+mu_40 =0.0181*10^-2; //[P], Appendix 8
+Dv = 7.01*10^-3; //[cm^2/s], from Eq.(21.25)
+rho = 2.34*10^-2; //[lb/ft^3]
+Nsc = mu_40/(rho*Dv);
+//Form Table 22.1,
+fp = 1.36;
+Hy_EO = 1.4*(1.1/0.66)^0.5*1/1.36*(Gy/500)^0.3*(1500/Gx)^0.4; //[ft]
+//Form Fig. 22.19,
+Hx_O2 = 0.9; //[ft]
+Gx1 = 1500;
+mu1 = 0.00656; //[P]
+rho1 = 1; //[lb/ft^3]
+//Using Eq.(21.28)
+Dv1 = 2.15*10^-5; //[cm^2/s]
+Nsc1 = mu1/(rho1*Dv1);
+//Using Eq.(22.35), with the correction factor fp and Nsc = 381, 
+//for O2 in water at 25 C
+Hx_EO = Hx_O2*(Gx/(mu1*100)/(Gx1/0.894))^0.3*(Nsc1/381)^0.5/1.36; //[ft]
+//From Fig 22.22, the average value of m
+m = 1.0;
+//From Eq.(22.30)
+HOy = 1.71+(1*0.96)/1.4; //[ft] 
+
+disp(Noy,'number of transfer units required')
+disp('ft',D,'diameter of the column')
+disp('ft',HOy,'packing height')
+\ No newline at end of file
diff --git a/839/CH22/EX22.6/Example_22_6.sce b/839/CH22/EX22.6/Example_22_6.sce
index 326e3f8e9..bea069cab 100755
--- a/839/CH22/EX22.6/Example_22_6.sce
+++ b/839/CH22/EX22.6/Example_22_6.sce
@@ -1,56 +1,57 @@
-//clear//
-clear;
-clc;
-
-//Example 22.6
-//Solution
-rho_m = 62.2/18; //[mol/ft^3]
-//kya = 0.025*Gy^0.7*Gx^0.25
-H2ObySO2 = 2*0.98964/0.01036; 
-//and
-xb = 1/(H2ObySO2+1);
-//The molal mass velocity of the feed gas Gm is
-Gm_in = 200/29*(1/0.8); //[mol/ft^2-h]
-SO2_in = Gm_in*0.2; //[mol/ft^2-h]
-Air_in = Gm_in*0.8; //[mol/ft^2-h]
-Air_out = Air_in; //[mol/ft^2-h]
-SO2_out = Air_out*(0.005/(1-0.005)); //[mol/ft^2-h]
-SO2_abs = SO2_in-SO2_out; //[mol/ft^2-h]
-H2O_in = H2ObySO2*SO2_abs; //[mol/ft^2-h]
-//Operating line
-x = 0:6;
-x = x/10^3;
-A = x./(1-x);
-B = H2O_in/Air_in*A+(0.005/0.995);
-y = B./(B+1);
-plot(x,y)
-xgrid();
-xlabel('x');
-ylabel('y');
-//legend('20C','30C','40C');
-title('x vs y');
-Gxbar = H2O_in*18.02+SO2_abs*64.1/2; //[lb/ft^2-h]
-kxa = 0.131*Gxbar^0.82; //[mol/ft^3-h]
-//The gas film coefficients are calculated for the bottom
-//and the top of the tower:
-//At bottom:
-Gy_B = (Air_in*29)+(SO2_in*64.1); //[lb/ft^2-h]
-kya_B = 0.025*Gy_B^0.7*Gx^0.25; //[mol/ft^3-h]
-//At top:
-Gy_T = (Air_out*29)+(SO2_out*64.1); //[lb/ft^2-h]
-kya_T = 0.025*Gy_T^0.7*Gx^0.25; //[mol/ft^3-h]  
-//Assuming 
-yLbar = 0.82
-C = kxa*yLbar/kya_B;
-//a line from (yb,xb) with a slope of -C, gives
-yi = 0.164;
-yLbar = 0.818;
-m = 20.1
-Kya_prime = 1/(yLbar/kya_B+m/kxa); //[mol/ft^3-h]
-//The fraction of the total resistance that is in the liquid is
-Rf = m/kxa/(1/Kya_prime);
-//For different values of y1
-y1 =[0.2,0.15,0.1,0.05,0.02,0.005]';
-delta_y1 = [0.103,0.084,0.062,0.034,0.015,0.005]';
-y1i = [0.164,0.118,0.074,0.034,0.012,0.002]';
-delta_yi = y1-y1i;
+//clear//
+clear;
+clc;
+
+
+//Example 22.6
+//Solution
+rho_m = 62.2/18; //[mol/ft^3]
+//kya = 0.025*Gy^0.7*Gx^0.25
+H2ObySO2 = 2*0.98964/0.01036; 
+//and
+xb = 1/(H2ObySO2+1);
+//The molal mass velocity of the feed gas Gm is
+Gm_in = 200/29*(1/0.8); //[mol/ft^2-h]
+SO2_in = Gm_in*0.2; //[mol/ft^2-h]
+Air_in = Gm_in*0.8; //[mol/ft^2-h]
+Air_out = Air_in; //[mol/ft^2-h]
+SO2_out = Air_out*(0.005/(1-0.005)); //[mol/ft^2-h]
+SO2_abs = SO2_in-SO2_out; //[mol/ft^2-h]
+H2O_in = H2ObySO2*SO2_abs; //[mol/ft^2-h]
+//Operating line
+x = 0:6;
+x = x/10^3;
+A = x./(1-x);
+B = H2O_in/Air_in*A+(0.005/0.995);
+y = B./(B+1);
+plot(x,y)
+xgrid();
+xlabel('x');
+ylabel('y');
+//legend('20C','30C','40C');
+title('x vs y');
+Gxbar = H2O_in*18.02+SO2_abs*64.1/2; //[lb/ft^2-h]
+kxa = 0.131*Gxbar^0.82; //[mol/ft^3-h]
+//The gas film coefficients are calculated for the bottom
+//and the top of the tower:
+//At bottom:
+Gy_B = (Air_in*29)+(SO2_in*64.1); //[lb/ft^2-h]
+kya_B = 0.025*Gy_B^0.7*Gxbar^0.25; //[mol/ft^3-h]
+//At top:
+Gy_T = (Air_out*29)+(SO2_out*64.1); //[lb/ft^2-h]
+kya_T = 0.025*Gy_T^0.7*Gxbar^0.25; //[mol/ft^3-h]  
+//Assuming 
+yLbar = 0.82
+C = kxa*yLbar/kya_B;
+//a line from (yb,xb) with a slope of -C, gives
+yi = 0.164;
+yLbar = 0.818;
+m = 20.1
+Kya_prime = 1/(yLbar/kya_B+m/kxa); //[mol/ft^3-h]
+//The fraction of the total resistance that is in the liquid is
+Rf = m/kxa/(1/Kya_prime);
+//For different values of y1
+y1 =[0.2,0.15,0.1,0.05,0.02,0.005]';
+delta_y1 = [0.103,0.084,0.062,0.034,0.015,0.005]';
+y1i = [0.164,0.118,0.074,0.034,0.012,0.002]';
+delta_yi = y1-y1i;
+\ No newline at end of file