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

---
 839/CH18/EX18.1/Example_18_1.sce | 23 +++++++++++
 839/CH18/EX18.2/Example_18_2.sce | 83 ++++++++++++++++++++++++++++++++++++++++
 839/CH18/EX18.3/Example_18_3.sce | 47 +++++++++++++++++++++++
 839/CH18/EX18.4/Example_18_4.sce | 26 +++++++++++++
 839/CH18/EX18.6/Example_18_6.sce | 79 ++++++++++++++++++++++++++++++++++++++
 839/CH18/EX18.7/Example_18_7.sce | 32 ++++++++++++++++
 839/CH18/EX18.8/Example_18_8.sce | 28 ++++++++++++++
 7 files changed, 318 insertions(+)
 create mode 100755 839/CH18/EX18.1/Example_18_1.sce
 create mode 100755 839/CH18/EX18.2/Example_18_2.sce
 create mode 100755 839/CH18/EX18.3/Example_18_3.sce
 create mode 100755 839/CH18/EX18.4/Example_18_4.sce
 create mode 100755 839/CH18/EX18.6/Example_18_6.sce
 create mode 100755 839/CH18/EX18.7/Example_18_7.sce
 create mode 100755 839/CH18/EX18.8/Example_18_8.sce

(limited to '839/CH18')

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
--- /dev/null
+++ 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
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+++ 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')
-- 
cgit