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+clear;
+clc;
+// Example 19.3
+printf('Example 19.3\n\n');
+//Page No.576
+// Solution 
+
+P_atm =  1 ;//[atm]
+P =  760 ;//[mm of Hg]
+x_1 = 4/100 ;// Mole fraction of hexane in liquid phase
+// Constant A,B and C for Antoine eqn. of n_hexane 
+A1 = 15.8366;
+B1 = 2697.55 ;
+C1 = -48.784;
+// Constant A,B and C for Antoine eqn. of n_octane
+A2 = 15.9798;
+B2 = 3127.60 ;
+C2 = -63.633;
+
+// Solve for bubble point temperature by eqn. obtained by using Antoine equation
+deff('[y] = f(T)','y = exp(A1-(B1/(C1+T)))*x_1 +exp(A2-(B2/(C2+T)))*(1-x_1)  - P');
+T = fsolve(390,f) ;// Bubble point temperature 
+funcprot(0);
+printf('Bubble point temperature is %.1f K\n',T);
+
+// Composition of first vapour
+// Get vapour pressure of hexane and octane from Perry, it is
+vp_1 =  3114 ;//  vapour pressure of hexane-[mm of Hg]
+vp_2 = 661 ;//  vapour pressure of octane-[mm of Hg]
+y_1 = vp_1*x_1/P ;// Mole fraction of hexane in vapour phase
+y_2 =  1- y_1 ;//Mole fraction of octane in vapour phase
+printf('\n Composition of first vapour.\n ');
+printf('Component            Mole fraction.\n ');
+printf('n_hexane             %.3f\n',y_1);
+printf(' n_octane             %.3f\n',y_2);
+\ No newline at end of file