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diff --git a/1328/CH15/EX15.7/15_7.sce b/1328/CH15/EX15.7/15_7.sce
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index 000000000..b0a41c96d
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+++ b/1328/CH15/EX15.7/15_7.sce
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+printf("\t example 15.7 \n");
+printf("\t approximate values are mentioned in the book \n");
+
+//Basis: One hour
+//20000=WD+WB , material balance
+//0.99*WD+(0.05*WB)=(20000*0.5) , Benzene balance
+// solving above two eq. we get WD and WB
+WD=9570; // lb/hr
+WB=10430; // lb/hr
+
+//Compositions and Boiling Points
+//Feed
+l1 = 10000; //Lb/hr , C6H4
+l2 = 10000; //Lb/hr , C7H8
+lb = l1+l2; //Lb/hr
+printf("\ttotal Lb/hr is %.0f\n",lb);
+mo1 = 78.1; //Mol. wt., C6H6
+mo2 = 93.1; //Mol. wt , C7H8
+mh1 = 128.0; //Mol/hr , C6H6
+mh2 = 107.5; //Mol/hr , C7H8
+mh = mh1 + mh2; // Mol/hr
+printf("\ttotal Mol/hr is %.1f\n",mh);
+x1 = mh1/mh;
+printf("\tx1 of C6H6 is %.3f\n",x1);
+x2 = mh2/mh;
+printf("\tx1 of C7H8 is %.3f\n",x2);
+x = x1+x2;
+printf("\tTotal x1 is %.3f\n",x);
+Pp1= 1380; // 214°F
+Pp2=575; // 214°F
+xp1 = x1*Pp1;
+printf("\tx1Pp1 of C6H6 is %.0f\n",xp1);
+xp2 = x2*Pp2;
+printf("\tx1Pp1 of C7H8 is %.0f\n",xp2);
+sxp = xp1 + xp2;
+printf("\tTotal x1Pp1 is %.0f\n",sxp);
+y1 = xp1/sxp;
+printf("\ty1 of C6H6 is %.3f\n",y1);
+y2 = xp2/sxp;
+printf("\ty1 of C7H8 is %.3f\n",y2);
+y = y1+y2;
+printf("\tTotal y1 is %.3f\n",y);
+
+
+w1 = 0.558; //from eq 15.42
+printf("\t(WR`/V =((xD - yF)/.(xD - xF))) = %.3fmol/mol\n",w1);
+wD=1;
+xD = 0.992;
+//V = WR' + WD
+// WR'/V = 0.558
+//Solving, WR' = (WR' * 0.558) + (0.558 * WD)
+Wr = 1.27; // mol reflux/mol distillate
+printf("\tWR` = %.2f (mol reflux)/(mol distillate)\n",Wr);
+Wr1 = Wr * 2; // mol/ mol distillate
+printf("\tAssumed 200 percent of the theoretical minimum reflux as economic\n\tWR = %.2f(mol)/(mil distillate)\n",Wr1);
+in = (wD * xD)/(Wr1 + 1); //intercept for the upper operating line
+printf("\tThe intercept for the upper operating line = %.3f\n",in);
+p = 13; // From fig. 15.23, connecting the corresponding lines
+printf("\tConnecting the corresponding line in Fig. 15.23, plates required: %.0f\n",p);
+fp = 7; // From fig. 15.23, connecting the corresponding lines
+printf("\tFeed plate is %.0fth(from top)\n",fp);
+d=122.5;
+tf = Wr1 * d;
+printf("\tTotal reflux is %.1f\n",tf);
+printf("\t\t\t\t\tHeat balances");
+
+//Heat Balances
+l1 = 33900;
+l2 = 9570;
+l3 = 24330;
+b1 = 253.8;
+b2 = 85.8;
+b3 = 85.8;
+bt1 = b1*l1;
+bt2 = b2*l2;
+bt3 = b3*l3;
+bt4 = 5688000;
+printf("\n\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,°F\tBtu/lb\tBtu/hr\n\t________________________________________________________________________\n\tHeat balance \n\taround condenser:\n");
+printf("\t  Heat in:\n\t  Top plate vapor.......433\t87.3\t%.0f\t195\t%.1f\t%.0f\n",l1,b1,bt1);
+printf("\t  Heat out:\n\t  Distillate............");
+printf("122.5\t78.3\t%.0f\t195\t%.1f\t%.0f\n",l2,b2,bt2);
+printf("\t  Reflux................");
+printf("310.5\t78.3\t%.0f\t195\t%.1f\t%.0f\n",l3,b3,bt3);
+printf("\t  Condenser duty, by\n\t  difference........... .....   ....    ......  ..");
+printf(".     .....   5688000\n");
+printf("\t\t\t\t\t\t\t\t\t_______\n\t\t\t\t\t\t\t\t\t8600000\n\n");
+
+lam = 153; // At 246 °F, Btu/hr
+rv = 5800000/153; //Lb/hr
+printf("\tReboiler vapor is %.2e lb/hr\n",rv);
+to = rv + 10430; //Lb/hr
+printf("\tTrapout is %.3e lb/hr\n",to);
+
+printf("\n\t\t\t\tMol/hr\tMol.wt.\tLb/hr\tTemp,°F\tBtu/lb\tBtu/hr\n\t________________________________________________________________________\n");
+printf("\tHeat in:\n\t  Trapout...............522\t92.8\t%.0f\t246\t108.0\t5230000\n",to);
+printf("\t  Reboiler duty, \n\t  by difference.......  ....    ....    .....   ...     .....   5800000\n");
+printf("\t\t\t\t\t\t\t\t\t_______\n\t\t\t\t\t\t\t\t\t11030000\n\n");
+printf("\n\tReboiler requirements are\n");
+printf("\t\tTotal liquid to reboiler\t48330 lb/hr\n\t\tVaporization\t\t\t37900 lb/hr\n\t\tTemperature(nearly isothermal)\t246°F\n\t\tPressure\t\t\t5 psig\n\t\tHeat load\t\t\t5800000 Btu/hr\n")
+//end