initial commit / add all books

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diff --git a/839/CH18/EX18.1/Example_18_1.sce b/839/CH18/EX18.1/Example_18_1.sce
new file mode 100755
index 000000000..9a438281a
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+++ b/839/CH18/EX18.1/Example_18_1.sce
@@ -0,0 +1,23 @@
+//clear//

+clear;

+clc;

+

+//Example 18.1

+//Given

+xF = 0.50;

+P = 1; //[atm]

+f =0.0001:0.2:1.2;

+A = -(1./f-1);

+x = [0.01:0.01:1];

+for i =1:length(f)

+  y(i,:) =-A(i)*x+xF/f(i)  

+end 

+//From Fig. 18.2

+xB = [0.50,0.455,0.41,0.365,0.325,0.29];

+yD = [0.71,0.67,0.63,0.585,0.54,0.5];

+//From Fig 18.3

+T = [92.2,93.7,95.0,96.5,97.7,99];

+plot(f,T./100,f,xB,f,yD)

+xlabel('f-moles vaporized per mole of feed')

+ylabel('Concentration, mole fraction Benzene')

+legend('Temperature(C)*100','Con. of Bnzene in liquid','Con. of Bnzene in vapor')

diff --git a/839/CH18/EX18.2/Example_18_2.sce b/839/CH18/EX18.2/Example_18_2.sce
new file mode 100755
index 000000000..b47fe7128
--- /dev/null
+++ b/839/CH18/EX18.2/Example_18_2.sce
@@ -0,0 +1,83 @@
+//clear//

+clear;

+clc;

+

+//Example 18.2

+//Given

+mdot = 30000; //[kg/h]

+wF_b = 40;

+wD = 97;

+wB = 2;

+R = 3.5;

+lambda_b = 7360; //[cal/g mol]

+lambda_t = 7960; //[cal/g mol]

+alpha = 2.5;

+TB = 95; //[C]

+TF = 20; //[C]

+P = 1; //[atm]

+Mb = 78;

+Mt = 92;

+Cp = 0.44; //[cal/g-C]

+//(a)

+//The concentrations of feed, overhead and bottoms in mole fraction of benzene are

+xF = (wF_b/Mb)/(wF_b/Mb+((100-wF_b)/Mt));

+xD = (wD/Mb)/(wD/Mb+((100-wD)/Mt));

+xB = (wB/Mb)/(wB/Mb+((100-wB)/Mt));

+//The average molecular weight of the feed is

+Mavg = 100/(wF_b/Mb+(100-wF_b)/Mt);

+//the average heat of vaporization

+lambda_avg = xF*lambda_b+(1-xF)*lambda_t; //[cal/g mol]

+//Feed rate

+F = mdot/Mavg; //[kg mol/h]

+//Using Eq.(18.5), by overall benzene balance

+D = F*(xF-xB)/(xD-xB); //[kg mol/h]

+B = F-D; //[kg mol/h]

+disp('respectively','kg mol/h',B,'kg mol/h',F,'the mole of overhead and bottom products are')

+

+

+//(b)Detemination of number of ideal plates and position of feed plate

+//(i)

+//Using Fig.18.16

+//Drawing the feed line with f = 0 on equilibrium diagram,

+//Plotting the operating lines with intercept from Eq.(18.19)is 0.216 

+//By counting the rectangular steps it is found that, besides the reboiler, 

+//11 ideal plates are neded and feed should be introduced on the 7th plate from

+//the top.

+

+//(ii)

+//The latent heat of vaporization of the feed 

+lambda = lambda_avg/Mavg; //[cal/g]

+//Using Eq.(18.24)

+q = 1+Cp*(TB-TF)/lambda;

+//From Eq.(18.31)

+slope = -q/(1-q);

+//From Fig. 18.17

+//It is found that a reboiler and 10 ideal plates are needed and feed is to be introduced 

+//on the fifth plate

+

+//(iii)

+q = 1/3;

+slope = -q/(1-q);

+//From Fig. 18.18

+//It calls for a reboiler and 12 plates, with the feed entering on the 7th plate

+

+//(c)

+//vapor flow in the rectifying section is

+V = 4.5*D; //[kg mol/h]

+lambda_s = 522; //[cal/g], From Appendix 7

+q = [1, 1.37, 0.333]

+//Using Eq.(18.27)

+Vbar = V-F*(1-q) 

+//Using Eq.(18.32), steam required

+ms_dot = lambda_t/lambda_s*Vbar; //[kg/h]

+disp('respectively','kg/h',ms_dot(3),'kg/h',ms_dot(2),'kg/h',ms_dot(1),'the steam consumption in the above three cases is')

+

+

+//(d)

+Tw1 = 25; //[C]

+Tw2 = 40; //[C]

+//The cooling water needed is same in all cases, Using Eq.(18.33)

+mw_dot = V*lambda_t/(Tw2-Tw1); //[kg/h]

+rho_25 = 62.24*16.018; //[kg/m^3]

+vw_dot = mw_dot/rho_25; //[m^3/h]

+disp('m^3/h',vw_dot,'cooling water needed is')

diff --git a/839/CH18/EX18.3/Example_18_3.sce b/839/CH18/EX18.3/Example_18_3.sce
new file mode 100755
index 000000000..cd43921a9
--- /dev/null
+++ b/839/CH18/EX18.3/Example_18_3.sce
@@ -0,0 +1,47 @@
+//clear//

+clear;

+clc;

+

+//Example 18.3

+//Given

+mdot = 30000; //[kg/h]

+wF_b = 40;

+wD = 97;

+wB = 2;

+R = 3.5;

+lambda_b = 7360; //[cal/g mol]

+lambda_t = 7960; //[cal/g mol]

+alpha = 2.5;

+TB = 95; //[C]

+TF = 20; //[C]

+P = 1; //[atm]

+Mb = 78;

+Mt = 92;

+Cp = 0.44; //[cal/g-C]

+//Solution

+xF = (wF_b/Mb)/(wF_b/Mb+((100-wF_b)/Mt));

+xD = (wD/Mb)/(wD/Mb+((100-wD)/Mt));

+xB = (wB/Mb)/(wB/Mb+((100-wB)/Mt));

+//The average molecular weight of the feed is

+Mavg = 100/(wF_b/Mb+(100-wF_b)/Mt);

+//the average heat of vaporization

+lambda_avg = xF*lambda_b+(1-xF)*lambda_t; //[cal/g mol]

+//Feed rate

+F = mdot/Mavg; //[kg mol/h]

+//Using Eq.(18.5), by overall benzene balance

+D = F*(xF-xB)/(xD-xB); //[kg mol/h]

+B = F-D; //[kg mol/h]

+//Using Table 18.3, in all three cases respectively

+xprime = [0.44,0.521,0.3];

+yprime = [0.658,0.730,0.513];

+

+//(a)

+//Using Eq.(18.43)

+RDm = (xD-yprime)./(yprime-xprime)

+disp('respectively',RDm(3),RDm(2),RDm(1),'Minimum Reflux Ratio for three cases is')

+

+//(b)

+//For minimum umber of plates the, the reflux ratio is infinite, the operating lines

+//coincides with the diagonal, and there are no differences between the three cases.

+//The plot is given by Fig 18.22. A reboiler and eight plates are needed.

+ 

diff --git a/839/CH18/EX18.4/Example_18_4.sce b/839/CH18/EX18.4/Example_18_4.sce
new file mode 100755
index 000000000..61c99d153
--- /dev/null
+++ b/839/CH18/EX18.4/Example_18_4.sce
@@ -0,0 +1,26 @@
+//clear//

+clear;

+clc;

+

+//Example 18.4

+//Given

+xa = 0.02;

+Vbar = 0.2; //[mol/mol of Feed]

+xb = 0.0001;

+yb = 0;

+xe = 0:0.01:1;

+m = 9

+ye = m*xe;

+//Let

+F = 1; //[mol]

+Lbar = F; //[mol]

+

+//Solution

+ya_star = m*xa;

+yb_star = m*xb;

+//By overall ethonal balance

+ya = Lbar/Vbar*(xa-xb)+ yb

+//Using Eq.(17.27), As both operting lines and equilibrium lines are straight

+N = log((ya-ya_star)/(yb-yb_star))/log((yb_star-ya_star)/(yb-ya));

+

+disp(N,'Ideal plates needed are' )

diff --git a/839/CH18/EX18.6/Example_18_6.sce b/839/CH18/EX18.6/Example_18_6.sce
new file mode 100755
index 000000000..df9872730
--- /dev/null
+++ b/839/CH18/EX18.6/Example_18_6.sce
@@ -0,0 +1,79 @@
+//clear//

+clear;

+clc;

+

+//Example 18.6

+//Given

+xF = 0.40;

+P = 1; //[atm]

+D = 5800; //[kg/h]

+R = 3.5;

+LbyV = R/(1+R);

+//Solution

+//Physical properties of methanol

+M = 32;

+Tnb = 65; //[C]

+rho_v = M*273/(22.4*338); //[kg/^3]

+rho_l_0 = 810; //[kg/m^3], At 0C, from Perry, Chemical Engineers' Handbook 

+rho_l_20 = 792; //[kg/m^3], At 20C, from Perry, Chemical Engineers' Handbook 

+rho_l = 750; //[kg/m^3], At 65C

+sigma = 19; //[dyn/cm], from Lange's Handbook of Chemistry

+//(a)

+//Vapor velocity and column diameter

+//Using Fig. 18.28, the abscissa is

+abscissa = LbyV*(rho_v/rho_l)^(1/2);

+//for 18-in. plate spacing

+Kv = 0.29;

+//Allowable vapor velocity

+uc = Kv*((rho_l-rho_v)/rho_v)^(1/2)*(sigma/20)^(0.2); //[ft/s]

+//Vapor flow rate

+V = D*(R+1)/(3600*rho_v); //[m^3/s]

+//Cross setional area of the column

+Bubbling_area = V/2.23; //[m^2]

+//If the bubble area is 0.7 of the total column area

+Column_area = Bubbling_area/0.7; //[m^2]

+//Column diameter

+Dc = sqrt(4*Column_area/%pi); //[m]

+disp('respectively','m',Dc,'and','ft/s',uc,'the allowable velocity and colmn diameter are')

+

+//(b)

+//Pressure drop:

+//Area of one unit of three holes on a trangular 3/4-in. pitch is

+//1/2*3/4*(3/4*sqrt(3/2)) in.^2. The hole area in this section (half a hole)is

+//1/2*%pi/4*(1/4)^2 in.^2. Thus the hole area is %pi/128*64/9*sqrt(3), or 10.08 percent

+//of the bubbling area.

+//Vapor velocity through holes:

+uo = 2.23/0.1008; //[m/s]

+//Using Eq.(18.58),

+//From Fig. 18.27

+Co = 0.73;

+hd = 51.0*uo^2*rho_v/(Co^2*rho_l); //[mm methanol]

+//Head of liquid on plate:

+//Weir height

+hw = 2*25.4; //[mm]

+//Height of the liquid above weir:

+//Assuming the downcomer area is 15 percent of the column 

+//area on each side of th column. From Perry, the chord

+//length for sucha segmental downcomer is 1.62 times the radius

+//of the colmn, so

+Lw = 1.62*2.23/2; //[m]

+//Liqiud Flow rate:

+qL = D*(R+1)/(rho_l*60); //[m^3/min]

+//From Eq.(18.60)

+how = 43.4*(qL/Lw)^(2/3) //[mm]

+//From Eq.(18.59), with 

+beeta = 0.6;

+hI = beeta*(hw+how); //[mm]

+//Total height of liquid, from Eq.(18.62)

+hT = hd+hI; //[mm]

+disp('mm methanol',hT,'pressure drop per plate is')

+

+//(c)

+//Froth height in th downcomer :

+//Using Eq.(18.62).,Estimating 

+hf_L = 10; //[mm methanol]

+//Then,

+Zc = (2*hI)+hd+hf_L; //[mm]

+//from Eq.(18.63)

+Z = Zc/0.5; //[mm]

+disp('mm methanol',Z,'Froth height in the downcomer is')

diff --git a/839/CH18/EX18.7/Example_18_7.sce b/839/CH18/EX18.7/Example_18_7.sce
new file mode 100755
index 000000000..60f38e239
--- /dev/null
+++ b/839/CH18/EX18.7/Example_18_7.sce
@@ -0,0 +1,32 @@
+//clear//

+clear;

+clc;

+

+//Example 18.7

+//Given

+xF = 0.40;

+P = 1; //[atm]

+D = 5800; //[kg/h]

+R = 3.5;

+LbyV = R/(1+R);

+//Solution

+//Physical properties of methanol

+M = 32;

+Tnb = 65; //[C]

+rho_v = M*273/(22.4*338); //[kg/^3]

+rho_l_0 = 810; //[kg/m^3], At 0C, from Perry, Chemical Engineers' Handbook 

+rho_l_20 = 792; //[kg/m^3], At 20C, from Perry, Chemical Engineers' Handbook 

+rho_l = 750; //[kg/m^3], At 65C

+sigma = 19; //[dyn/cm], from Lange's Handbook of Chemistry

+//(a)

+//Vapor velocity and column diameter

+//Using Fig. 18.28, the abscissa is

+abscissa = LbyV*(rho_v/rho_l)^(1/2);

+//for 18-in. plate spacing

+Kv = 0.29;

+//Allowable vapor velocity

+uc = Kv*((rho_l-rho_v)/rho_v)^(1/2)*(sigma/20)^(0.2)/(3.2825112); //[ft/s]

+//From Eq.(18.71), the F factor is

+F = uc*sqrt(rho_v);

+disp(F,'the value of F factor is')

+

diff --git a/839/CH18/EX18.8/Example_18_8.sce b/839/CH18/EX18.8/Example_18_8.sce
new file mode 100755
index 000000000..df622aee4
--- /dev/null
+++ b/839/CH18/EX18.8/Example_18_8.sce
@@ -0,0 +1,28 @@
+//clear//

+clear;

+clc;

+

+//Example 18.8

+//Given

+xOA = 0.15;

+xAi = 0.015;

+

+P = 1; //[atm]

+

+//Solution

+

+Pv = 3.4; //[atm]

+alpha_o = 3.4; //at 36 C

+Tbi = 27; //[C]

+alpha_i = 3.6

+alpha = (alpha_o+alpha_i)/2;

+//Basis 1 mol Feed

+nOA = 0.15; //[mol]

+nA = 0.015; //[mol]

+nOB = 0.85; //[mol]

+//Using Eq.(18.79)

+nB = nOB*(nA/nOA)^(1/alpha); //[mol]

+n = nA+nB; //[mol]

+xA = nA/n; 

+disp('mol',nB,'pentane removed is')

+disp((1-xA),'xB',xA,'xA','composition of the remaining liquid is')