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-rw-r--r--1328/CH13/EX13.1/13_1.sce207
-rw-r--r--1328/CH13/EX13.2/13_2.sce59
-rw-r--r--1328/CH13/EX13.3/13_3.sce195
-rw-r--r--1328/CH13/EX13.4/13_4.sce11
-rw-r--r--1328/CH13/EX13.5/13_5.sce121
-rw-r--r--1328/CH13/EX13.6a/13_6a.sce265
-rw-r--r--1328/CH13/EX13.6b/13_6b.sce91
7 files changed, 949 insertions, 0 deletions
diff --git a/1328/CH13/EX13.1/13_1.sce b/1328/CH13/EX13.1/13_1.sce
new file mode 100644
index 000000000..18e1019e8
--- /dev/null
+++ b/1328/CH13/EX13.1/13_1.sce
@@ -0,0 +1,207 @@
+printf("\t example 13.1 \n");
+// at atmospheric pressure,Pt=760 mm Hg
+printf("\t approximate values are mentioned in the book \n");
+x(1)=0.077; // mole fraction of C4
+x(2)=0.613; // mole fraction of C5
+x(3)=0.310; // mole fraction of C6
+printf("\t for T 100 F \n");
+Pp(1)=3170; // vapour pressure of C4, from fig 13.3
+Pp(2)=790; // vapour pressure of C5,from fig 13.3
+Pp(3)=250; // vapour pressure of C6,from fig 13.3
+i=1;
+while(i<4)
+ p(i)=(Pp(i)*x(i));
+ printf(" \n x(i) Pp(i) p(i) \n "+string(x(i))+" "+string(Pp(i))+" "+string(p(i))+" \n");
+i=i+1;
+end
+pt=p(1)+p(2)+p(3);
+printf("\t total pressure is : %.1f mm Hg \n",pt);
+printf("\t pressure is too high \n");
+printf("\t for T 96 F \n");
+Pp(1)=2990; // vapour pressure of C4, from fig 13.3
+Pp(2)=725; // vapour pressure of C5,from fig 13.3
+Pp(3)=229; // vapour pressure of C6,from fig 13.3
+i=1;
+while(i<4)
+ p(i)=(Pp(i)*x(i));
+ printf(" \n x(i) Pp(i) p(i) \n "+string(x(i))+" "+string(Pp(i))+" "+string(p(i))+" \n");
+i=i+1;
+end
+pt=p(1)+p(2)+p(3);
+printf("\t total pressure is : %.1f mm Hg \n",pt);
+printf("\t pressure is too low \n");
+printf("\t for T 97 F \n");
+Pp(1)=3040; // vapour pressure of C4, from fig 13.3
+Pp(2)=740; // vapour pressure of C5,from fig 13.3
+Pp(3)=234; // vapour pressure of C6,from fig 13.3
+i=1;
+while(i<4)
+ p(i)=(Pp(i)*x(i));
+ printf(" \n x(i) Pp(i) p(i) \n "+string(x(i))+" "+string(Pp(i))+" "+string(p(i))+" \n");
+i=i+1;
+end
+pt=p(1)+p(2)+p(3);
+printf("\t total pressure is : %.1f mm Hg \n",pt);
+i=1;
+while(i<4)
+ y(i)=(Pp(i)*x(i)/pt);
+ printf("\n x(i) y(i) \n "+string(x(i))+" "+string(y(i))+" \n");
+ i=i+1;
+end
+printf("\t solution for b \n");
+// Similarly at what temperature will the mixture start to boil if the system is under a pressure of 35 psia
+printf("\t for T 150 F \n");
+Pp(1)=6100; // vapour pressure of C4, from fig 13.3
+Pp(2)=1880; // vapour pressure of C5,from fig 13.3
+Pp(3)=680; // vapour pressure of C6,from fig 13.3
+i=1;
+while(i<4)
+ p(i)=(Pp(i)*x(i));
+ printf(" \n x(i) Pp(i) p(i) \n "+string(x(i))+" "+string(Pp(i))+" "+string(p(i))+" \n");
+i=i+1;
+end
+pt=p(1)+p(2)+p(3);
+printf("\t total pressure is : %.0f mm Hg \n",pt);
+printf("\t pressure is too high \n");
+printf("\t for T 149F \n");
+Pp(1)=6050; // vapour pressure of C4, from fig 13.3
+Pp(2)=1850; // vapour pressure of C5,from fig 13.3
+Pp(3)=670; // vapour pressure of C6,from fig 13.3
+i=1;
+while(i<4)
+ p(i)=(Pp(i)*x(i));
+ printf(" \n x(i) Pp(i) p(i) \n "+string(x(i))+" "+string(Pp(i))+" "+string(p(i))+" \n");
+i=i+1;
+end
+pt=p(1)+p(2)+p(3);
+printf("\t total pressure is : %.0f mm Hg \n",pt);
+i=1;
+while(i<4)
+ y(i)=(Pp(i)*x(i)/pt);
+ printf("\n x(i) y(i) \n "+string(x(i))+" "+string(y(i))+" \n");
+ i=i+1;
+end
+printf("\t solution for c \n");
+printf("\t for T 95F \n");
+K(1)=3.13; // fig 7
+K(2)=0.92; // fig 7
+K(3)=0.30; // fig 7
+i=1;
+while(i<4)
+ y(i)=(K(i)*x(i));
+ printf("\n x(i) K(i) y(i) \n "+string(x(i))+" "+string(K(i))+" "+string(y(i))+" \n");
+ i=i+1;
+end
+yt=y(1)+y(2)+y(3);
+printf("\t yt is : %.3f \n",yt);
+printf("\t yt is too low \n");
+printf("\t for T 100F \n");
+K(1)=3.35; // fig 7
+K(2)=1; // fig 7
+K(3)=0.335; // fig 7
+i=1;
+while(i<4)
+ y(i)=(K(i)*x(i));
+ printf("\n x(i) K(i) y(i) \n "+string(x(i))+" "+string(K(i))+" "+string(y(i))+" \n");
+ i=i+1;
+end
+yt=y(1)+y(2)+y(3);
+printf("\t yt is : %.3f \n",yt);
+printf("\t yt is too low \n");
+printf("\t for T 102F \n");
+K(1)=3.45; // fig 7
+K(2)=1.02; // fig 7
+K(3)=0.35; // fig 7
+i=1;
+while(i<4)
+ y(i)=(K(i)*x(i));
+ printf("\n x(i) K(i) y(i) \n "+string(x(i))+" "+string(K(i))+" "+string(y(i))+" \n");
+ i=i+1;
+end
+yt=y(1)+y(2)+y(3);
+printf("\t yt is : %.3f \n",yt);
+printf("\t solution for d \n");
+// The use of K values gives y, directly and permits use of the total mol fraction of yt = 1.00 as the criterion for equilibrium
+printf("\t for T 150F \n");
+K(1)=2.8; // fig 7
+K(2)=1.01; // fig 7
+K(3)=0.4; // fig 7
+i=1;
+while(i<4)
+ y(i)=(K(i)*x(i));
+ printf("\n x(i) K(i) y(i) \n "+string(x(i))+" "+string(K(i))+" "+string(y(i))+" \n");
+ i=i+1;
+end
+yt=y(1)+y(2)+y(3);
+printf("\t yt is : %.3f \n",yt);
+printf("\t yt is too low \n");
+printf("\t for T 153F \n");
+K(1)=2.90; // fig 7
+K(2)=1.06; // fig 7
+K(3)=0.415; // fig 7
+i=1;
+while(i<4)
+ y(i)=(K(i)*x(i));
+ printf("\n x(i) K(i) y(i) \n "+string(x(i))+" "+string(K(i))+" "+string(y(i))+" \n");
+ i=i+1;
+end
+yt=y(1)+y(2)+y(3);
+printf("\t yt is : %.3f \n",yt);
+printf("\t solution for e at pt=760mm Hg \n");
+y(1)=0.077; // mole fraction of C4
+y(2)=0.613; // mole fraction of C5
+y(3)=0.310; // mole fraction of C6
+printf("\t for T 130F \n");
+K(1)=5; // fig 7
+K(2)=1.65; // fig 7
+K(3)=0.62; // fig 7
+i=1;
+while(i<4)
+ x(i)=(y(i)/K(i));
+ printf("\n y(i) K(i) x(i) \n "+string(y(i))+" "+string(K(i))+" "+string(x(i))+" \n");
+ i=i+1;
+end
+xt=x(1)+x(2)+x(3);
+printf("\t xt is : %.3f \n",xt);
+printf("\t xt is too low \n");
+printf("\t for T 120F \n");
+K(1)=4.4; // fig 7
+K(2)=1.4; // fig 7
+K(3)=0.51; // fig 7
+i=1;
+while(i<4)
+ x(i)=(y(i)/K(i));
+ printf("\n y(i) K(i) x(i) \n "+string(y(i))+" "+string(K(i))+" "+string(x(i))+" \n");
+ i=i+1;
+end
+xt=x(1)+x(2)+x(3);
+printf("\t xt is : %.3f \n",xt);
+printf("\t xt is high \n");
+printf("\t for T 123F \n");
+K(1)=4.6; // fig 7
+K(2)=1.49; // fig 7
+K(3)=0.545; // fig 7
+i=1;
+while(i<4)
+ x(i)=(y(i)/K(i));
+ printf("\n y(i) K(i) x(i) \n "+string(y(i))+" "+string(K(i))+" "+string(x(i))+" \n");
+ i=i+1;
+end
+xt=x(1)+x(2)+x(3);
+printf("\t xt is : %.3f \n",xt);
+printf("\t dew point at 760mm is 123F \n");
+printf("\t dew point at 35psia \n");
+printf("\t for T 174F \n");
+K(1)=3.7; // fig 7
+K(2)=1.38; // fig 7
+K(3)=0.58; // fig 7
+i=1;
+while(i<4)
+ x(i)=(y(i)/K(i));
+ printf("\n y(i) K(i) x(i) \n "+string(y(i))+" "+string(K(i))+" "+string(x(i))+" \n");
+ i=i+1;
+end
+xt=x(1)+x(2)+x(3);
+printf("\t xt is : %.3f \n",xt);
+printf("\t dew point is 174F \n");
+// end
diff --git a/1328/CH13/EX13.2/13_2.sce b/1328/CH13/EX13.2/13_2.sce
new file mode 100644
index 000000000..387a23df0
--- /dev/null
+++ b/1328/CH13/EX13.2/13_2.sce
@@ -0,0 +1,59 @@
+printf("\t example 13.2 \n");
+printf("\t approximate values are mentioned in the book \n");
+printf("\t bubble point at 95F and 14.7psia \n");
+x(1)=0.077; // mole fraction of C4
+x(2)=0.613; // mole fraction of C5
+x(3)=0.310; // mole fraction of C6
+K(1)=3.13; // fig 7
+K(2)=0.92; // fig 7
+K(3)=0.3; // fig 7
+a(1)=3.4; // a= alpha
+a(2)=1;
+a(3)=0.326;
+i=1;
+while(i<4)
+ Z(i)=(a(i)*x(i));
+ i=i+1;
+end
+Zt=Z(1)+Z(2)+Z(3);
+printf("\t Zt is : %.3f \n",Zt);
+i=1;
+while(i<4)
+ y(i)=(a(i)*x(i)/(Zt));
+ printf(" \n x(i) K(i) a(i) Z(i) y(i) \n "+string(x(i))+" "+string(K(i))+" "+string(a(i))+" "+string(Z(i))+" "+string(y(i))+" \n");
+ i=i+1;
+end
+yt=y(1)+y(2)+y(3);
+printf("\t yt is : %.3f \n",yt);
+K2=(y(2)/x(2));
+printf("\t K2 is : %.3f \n",K2);
+printf("\t bubble point is 102 \n"); // from fig 7 , comparing K2 value
+printf("\t dew point at 130F and 14.7psia \n");
+y(1)=0.077; // mole fraction of C4
+y(2)=0.613; // mole fraction of C5
+y(3)=0.310; // mole fraction of C6
+K(1)=5; // fig 7
+K(2)=1.65; // fig 7
+K(3)=0.62; // fig 7
+a(1)=3.03; // a= alpha
+a(2)=1;
+a(3)=0.376;
+i=1;
+while(i<4)
+ Z(i)=(y(i)/a(i));
+ i=i+1;
+end
+Zt=Z(1)+Z(2)+Z(3);
+printf("\t Zt is : %.3f \n",Zt);
+i=1;
+while(i<4)
+ x(i)=(Z(i)/Zt);
+ printf(" \n y(i) K(i) a(i) Z(i) x(i) \n "+string(y(i))+" "+string(K(i))+" "+string(a(i))+" "+string(Z(i))+" "+string(x(i))+" \n");
+ i=i+1;
+end
+xt=x(1)+x(2)+x(3);
+printf("\t xt is : %.0f \n",xt);
+K2=(y(2)/x(2));
+printf("\t K2 is : %.2f \n",K2);
+printf("\t dew point is 122F \n"); // from fig 7, comparing K2 value
+// end
diff --git a/1328/CH13/EX13.3/13_3.sce b/1328/CH13/EX13.3/13_3.sce
new file mode 100644
index 000000000..50166d3e7
--- /dev/null
+++ b/1328/CH13/EX13.3/13_3.sce
@@ -0,0 +1,195 @@
+printf("\t example 13.3 \n");
+printf("\t approximate values are mentioned in the book \n");
+printf("\t for condensing range \n");
+V(1)=170.5; // volume of C3,Mol/hr
+V(2)=284; // volume of C4,Mol/hr
+V(3)=56.8; // volume of C6,Mol/hr
+V(4)=341.1; // volume of C7,Mol/hr
+V(5)=284; // volume of C8,Mol/hr
+Tw=283; // dew point assumption
+Tb=120; // bubble point assumption
+K(1)=13.75 // at 283F
+K(2)=6.18 // at 283F
+K(3)=1.60 // at 283F
+K(4)=0.825 // at 283F
+K(5)=0.452 // at 283F
+i=1;
+while(i<6)
+ Z(i)=(V(i)/K(i));
+ i=i+1;
+end
+Vt=V(1)+V(2)+V(3)+V(4)+V(5);
+Zt=Z(1)+Z(2)+Z(3)+Z(4)+Z(5);
+L(1)=170.5; // volume of C3,Mol/hr
+L(2)=284; // volume of C4,Mol/hr
+L(3)=56.8; // volume of C6,Mol/hr
+L(4)=341.1; // volume of C7,Mol/hr
+L(5)=284; // volume of C8,Mol/hr
+Kl(1)=4.1 // at 283F
+Kl(2)=1.39 // at 283F
+Kl(3)=0.17 // at 283F
+Kl(4)=0.06 // at 283F
+Kl(5)=0.023 // at 283F
+i=1;
+while(i<6)
+ Zl(i)=(L(i)*Kl(i));
+ printf(" \n V(i) K(i) Z(i) L(i) Kl(i) Zl(i) \n "+string(V(i))+" "+string(K(i))+" "+string(Z(i))+" "+string(L(i))+" "+string(Kl(i))+" "+string(Zl(i))+" \n");
+ i=i+1;
+end
+Lt=L(1)+L(2)+L(3)+L(4)+L(5);
+Zlt=Zl(1)+Zl(2)+Zl(3)+Zl(4)+Zl(5);
+printf("\t total volume in vapour phase : %.1f \n",Vt);
+printf("\t total Zt in vapour phase : %.1f \n",Zt);
+printf("\t total volume in liquid phase : %.1f \n",Lt);
+printf("\t total Zlt in liquid phase : %.1f \n",Zlt);
+// Range: 283 to 270°F
+// Trial: Assume V /L = 4.00.
+R=4; // R=(V/L), assumption
+K(1)=12.75 // at 270F
+K(2)=5.61 // at 270F
+K(3)=1.40 // at 270F
+K(4)=0.705 // at 270F
+K(5)=0.375 // at 270F
+i=1;
+Y(i)=V(i);
+while(i<6)
+ P(i)=(K(i)*R);
+ L1(i)=(V(i)/(1+P(i))); // V(i)=Y(i)
+ printf(" \n Y(i) K(i) P(i) L1(i) \n "+string(V(i))+" "+string(K(i))+" "+string(P(i))+" "+string(L1(i))+" \n");
+ i=i+1;
+end
+L1t=L1(1)+L1(2)+L1(3)+L1(4)+L1(5);
+V1t=(Vt-L1t);
+R1=(V1t/L1t);
+printf("\t total liquid at 270F : %.0f \n",L1t);
+printf("\t total vapour at 270F : %.0f \n",V1t);
+printf("\t R1 is : %.0f \n",R1);
+// If the assumed and calculated values of V /L had not checked, a new value would have been assumed.
+printf("\t for condensing curve \n");
+R270=4; // V/L at 270, from table 13.2
+R270=1.567; // V/L at 250, from table 13.2
+R270=0.916; // V/L at 230, from table 13.2
+R270=0.520; // V/L at 200, from table 13.2
+R270=0.226; // V/L at 160, from table 13.2
+H270=30835500; // 4th table in solution ,enthalpies calculated from fig 10
+printf("\t heat load at 270F is : %.0f Btu/hr \n",H270);
+H250=27042400; // 5th table in solution ,enthalpies calculated from fig 10
+printf("\t heat load at 250F is : %.0f Btu/hr \n",H250);
+Q=H270-H250;
+printf("\t heat load for interval 270-250F : %.0f Btu/hr \n",Q);
+qt=21203000; // 6th table in solution, calculated from fig 10
+printf("\t heat load for entire range is : %.0f Btu/hr \n",qt);
+M=210410; // M=sum(U*A), 6th table in solution, calculated from fig 10
+w=(qt/(120-80));
+printf("\t water flow rate : %.1e lb/hr \n",w);
+W=95450; // flow rate of feed,lb/hr
+delt=(qt/M);
+printf("\t weighted delt is : %.1f F \n",delt);
+q1=[0 3.4765 7.2696 10.109 13.468 17.399 21.203];
+T1=[283 270 250 230 200 160 120];
+plot2d(q1,T1,style=3,rect=[0,0,25,300]);
+q2=[0 21.203];
+T2=[283 120];
+plot2d(q2,T2,style=5,rect=[0,0,25,300]);
+xtitle("condensing curve","heat load,Btu/hr","temperature,F");
+legend("green-differential vapour","red-vapour");
+printf("\t calculation of the exchanger \n");
+T1=283; // inlet hot fluid,F
+T2=120; // outlet hot fluid,F
+t1=80; // inlet cold fluid,F
+t2=120; // outlet cold fluid,F
+L=16;
+Nt=774;
+n=4;
+row=62.5;
+Qs=21203000; // Btu/hr
+Qw=(w*1*(120-80));
+printf("\t heat absorbed by water : %.4e Btu/hr \n",Qw);
+Mavg=84; // This corresponds very closely to hexane (mol. Wt. = 86.2) whose properties will be used throughout.
+Qc=W*(0.6/2)*(283-120);
+printf("\t condensate sensible heat load: %.2e Btu/hr \n",Qc);
+S=(Qc*(100/Qs));
+printf("\t submergence : %.0f \n",S);
+Tc=((T1+T2)/2); // caloric temperature of hot fluid,F
+printf("\t caloric temperature of hot fluid is : %.0f F \n",Tc);
+tc=((t1+t2)/2); // caloric temperature of cold fluid,F
+printf("\t caloric temperature of cold fluid is : %.0f F \n",tc);
+printf("\t hot fluid:shellside,vapour \n");
+Nts=(774*(1-.22)); // as submergence is 22%
+printf("\t unmerged tubes : %.0f \n",Nts);
+Gs=(W/(L*(Nts^(2/3)))); // eq 12.43
+printf("\t Gs is : %.1f \n",Gs);
+Ho=200; // assumption
+printf("\t cold fluid:inner tube side,water \n");
+at1=0.302; // flow area, in^2
+at=((Nt*at1)/(144*n)); // total area,ft^2,from eq.7.48
+printf("\t flow area is : %.3f ft^2 \n",at);
+Gt=(w/(at)); // mass velocity,lb/(hr)*(ft^2)
+printf("\t mass velocity is : %.1e lb/(hr)*(ft^2) \n",Gt);
+V=(Gt/(3600*row));
+printf("\t V is : %.2f fps \n",V);
+hi=1355; // fig 25
+ID=0.62;
+OD=0.75;
+hio=((hi)*(ID/OD)); //Hio=(hio/phyp), using eq.6.5
+printf("\t Correct hio to the surface at the OD is : %.2e Btu/(hr)*(ft^2)*(F) \n",hio);
+tw=(tc)+(((Ho)/(hio+Ho))*(Tc-tc)); // from eq.5.31
+printf("\t tw is : %.0f F \n",tw);
+tf=(Tc+tw)/(2); // from eq 12.19
+printf("\t tf is : %.0f F \n",tf);
+kf=0.077; //table 4, Btu/(hr)*(ft^2)*(F/ft)
+sf=0.60; // from table 6
+muf=0.21; // cp, from fig 14
+ho=206; // Btu/(hr)*(ft^2)*(F), from fig 12.9
+printf("\t Correct ho to the surface at the OD is : %.0f Btu/(hr)*(ft^2)*(F) \n",ho);
+Uc=((hio)*(ho)/(hio+ho)); // clean overall coefficient,Btu/(hr)*(ft^2)*(F)
+printf("\t clean overall coefficient is : %.0f Btu/(hr)*(ft^2)*(F) \n",Uc);
+Ac=(Qw/(174*delt));
+printf("\t clean surface required for condensation : %.2e ft^2 \n",Ac);
+As=1210*0.22;
+printf("\t clean surface required for subcooling : %.0f ft^2 \n",As);
+AG=As+Ac;
+printf("\t total clean surface : %.0f ft^2 \n",AG);
+UC=(Qw/(AG*delt));
+printf("\t weighted clean overall coefficient : %.0f Btu/(hr)*(ft^2)*(F) \n",UC);
+A2=0.1963; // actual surface supplied for each tube,ft^2,from table 10
+A=(Nt*L*A2); // ft^2
+printf("\t total surface area is : %.2e ft^2 \n",A);
+UD=((Qw)/((A)*(delt)));
+printf("\t actual design overall coefficient is : %.1f Btu/(hr)*(ft^2)*(F) \n",UD);
+Rd=((UC-UD)/((UD)*(UC))); // (hr)*(ft^2)*(F)/Btu
+printf("\t actual Rd is : %.5f (hr)*(ft^2)*(F)/Btu \n",Rd);
+printf("\t pressure drop for annulus \n");
+B=30;
+as=33*0.25*(30/144)*1; // eq 7.1
+printf("\t as is : %.2f ft^2 \n",as);
+Gs=(W/as);
+printf("\t Gs is : %.2e lb/(hr)*(ft^2) \n",Gs); // eq 7.2
+mu1=0.0218; // at 283F
+De=0.0608; // ft, from fig 15
+Res=(De*Gs)/(mu1);
+printf("\t reynolds number is : %.2e \n",Res);
+f=0.00125; // fig 29
+N=(12*L/B); // eq 7.43
+printf("\t number crosses : %.0f \n",N);
+row1=0.527; //lb/ft^3
+s=0.00844;
+Ds=2.75; // ft
+delPs=((f*(Gs^2)*(Ds)*(N))/(5.22*(10^10)*(De)*(s)*(1)))/(2); // using eq 12.47,psi
+printf("\t delPs is : %.1f psi \n",delPs);
+printf("\t pressure drop for inner pipe \n");
+mu2=1.74; // fig 14
+D=0.0517; // ft
+s=1;
+Ret=(D*Gt/mu2);
+printf("\t reynolds number : %.2e \n",Ret);
+f=0.00019; // ft^2/in^2
+delPt=((f*(Gt^2)*(L)*(n))/(5.22*(10^10)*(D)*(1)*(1))); // using eq.7.45,psi
+printf("\t delPt is : %.1f psi \n",delPt);
+X1=0.23; // X1=((V^2)/(2*g)),using fig.27
+delPr=((4*n*X1)/(s)); // using eq.7.46,psi
+printf("\t delPr is : %.1f psi \n",delPr);
+delPT=delPt+delPr; // using eq.7.47,psi
+printf("\t delPT is : %.1f psi \n",delPT);
+printf("\t allowable delPa is 10 psi \n");
+// end
diff --git a/1328/CH13/EX13.4/13_4.sce b/1328/CH13/EX13.4/13_4.sce
new file mode 100644
index 000000000..03e5d39b0
--- /dev/null
+++ b/1328/CH13/EX13.4/13_4.sce
@@ -0,0 +1,11 @@
+printf("\t example 13.4 \n");
+printf("\t approximate values are mentioned in the book \n");
+vA=2*3.7+(7.4); // for steam
+vB=14.8+(2*7.4); // for CO2
+MA=18;
+MB=44;
+T=403; // K
+Pt=3.04; // atm
+kd=(0.0166)*(((403^(3/2))/(3.04*(14.8^(1/3)+29.6^(1/3))^(2)))*((1/18)+(1/44))^(1/2)); // eq 13.31
+printf("\t diffusivity is : %.2f ft^2/hr \n",kd);
+// end
diff --git a/1328/CH13/EX13.5/13_5.sce b/1328/CH13/EX13.5/13_5.sce
new file mode 100644
index 000000000..308dd8fa4
--- /dev/null
+++ b/1328/CH13/EX13.5/13_5.sce
@@ -0,0 +1,121 @@
+printf("\t example 13.5 \n");
+// for a Basis of one Hour
+printf("\t approximate values are mentioned in the book \n");
+c(1)=1544; // Flow rate of CO2, Lb/hr
+h(1)=4500; // Flow rate of H20, Lb/hr
+
+c(2)=35; //Flow rate of CO2, Mol/hr
+h(2)=250;//Flow rate of H20, Mol/hr
+
+t(1)=c(1)+h(1); //Total flow rate , Lb/hr
+t(2)=c(2)+h(2); //Total flow rate, Mol/hr
+
+Pt = (30+14.7)/(14.7); //Total Pressure in atm
+printf("\t Pt is %.2f\n",Pt);
+Pw = ( h(2)/t(2) )*Pt; //Partial pressure of Water in atm
+
+printf("\t Partial Pressure of Water: %.2f atm \n",Pw);
+
+Tw = 267; // from table 7 at 2.68atm
+Mm = (t(1)/t(2));
+
+printf("\t mean molecular weight : %.1f \n",Mm);
+// weighted temperature difference
+// overall balance
+//for Inlet
+Pv=2.68; // water vapour pressure, atm
+Pg=Pt-Pv; // Inert pressure
+//for Exit
+Pw1 = 0.1152 // Partial pressure of water at 120 F
+Pv1 = 0.115; // Water vapor pressure
+Pg1 = 2.935; // Inert pressure
+
+w1 = 250; //Pound mols steam inlet
+w2 = c(2)*(Pv1/Pg1);
+printf("\tPound mols steam exit:%.2f\n",w2);
+w3 = w1 - w2;
+printf("\tPound mols steam condessed:%.2f\n",w3);
+//Assume points at 267, 262, 255,225,150,120 deg F
+//For the interval from 267 to 262 F
+
+Pv2 = 2.49; // From table 7 at 262 F
+Pg2 = Pt - Pv2; //Inert pressure
+printf("\tPg is %.2f",Pg2);
+
+w4 = c(2) * (Pv2/Pg2); //Mol steam remaining
+w5 = h(2) - w4; //Mol steam condensed
+
+printf("\tMol steam remaining:%.0f\n",w4);
+printf("\tMol steam condensed:%.0f\n",w5);
+
+h1 = (w5*18*937.3) + (0.46*(267-262) * w5 * 18); //Heat of condensation
+h2 = (w4 * 18 * 0.46*(267-262)); //Heat from uncondensed steam
+h3 = c(1)*0.22*5.0; //Heat from noncondensable
+
+printf("\tHeat of condensation:%.2e\n",h1);
+printf("\tHeat from uncondensed steam:%.2e\n",h2);
+printf("\tHeat from noncondensable:%.1e\n",h3);
+
+ht = h1+h2+h3;//Total heat
+printf("\tTotal heat:%.0f\n",ht);
+
+//Similarily calculating the Heat balance for other intervals
+printf("\tInterval,F\tTotal Heat\n\t267-262\t1,598,000\n\t262-255\t1,104,000\n\t255-225\t1,172,000\n\t225-150\t751,000\n\t150-120\t177,000\n\tTotal\t4,802,000\n");
+
+w=4802000/(115-80); //Total water
+printf("\tTotal water: %.2e\n",w);
+//Water coefficient
+Nt = 246;
+at1 = 0.302;
+n = 4;
+
+at = Nt * (at1/(144*n)); // From eq 7.48
+printf("\tat is %.3f ft^2\n",at);
+Gt = w/at;
+printf("\tGt is %.2e lb/(hr)(ft^2)\n",Gt);
+ro = 62.5;
+V = Gt/(3600*ro);
+printf("\tV is %.2f fps\n",V);
+hi = 1120; // From fig. 25
+ID = 0.62;
+OD = 0.75;
+hi0= hi *(ID/OD); //From eq 6.5
+printf("\thi0 is %.0f\n",hi0);
+//Mean properties at 267 F
+c = ((c(1)*0.22)+(h(1)*0.46))/t(1); // Calculation mistake in Book
+printf("\tMean c:%.3f Btu/(lb)(F)\n",c);
+
+k = ((c(1)*0.0128)+(h(1)*0.015))/t(1); // Calculation mistake in Book
+printf("\tMean k:%.4f Btu/(hr)(ft^2)(F/ft)\n",k);
+
+mu = (((c(1)*0.019)+(h(1)*0.0136))/t(1))* 2.42; // Calculation mistake in Book
+printf("\tMean mu:%.4f lb/(hr)(ft)\n",mu);
+
+ID1 = 21.25;
+C = 0.25;
+B = 12;
+PT = 1.0;
+
+as = ID1 * C * (B/(144*PT)); //From eq 7.1
+printf("\tas is %.3f ft^2\n",as);
+Gs = t(1)/as //From eq 7.2
+printf("\tGs is %.3e lb/(hr)(ft^2)\n",Gs);
+Ds = 0.0792; // From Fig 28
+Res = Ds * (Gs/0.0363); // From eq 7.3
+printf("\tRes is %.2e\n",Res);
+jH = 102; // From Fig 28
+x = ((c*mu)/k)^(1/3);
+printf("\t(c.mu/k)^1/3 is %.0f\n",x);
+h0 = jH * 0.0146 * (x/Ds); //From eq 6.15b
+printf("\th0 is %.0f\n",h0);
+y = 0.62 // y = (mu/ro * kd)^(2/3)
+z = 1.01; // z = ((c*mu)/k)^(2/3)
+
+K = (h0*z)/(0.407*Mm*y); //KG = K/p0f
+printf("\tK is %.2f\n",K);
+//at point 1
+Tg = 244; // F
+tW = 115;
+delt=(Tg-tW);
+printf("\t delt is %.0f F \n",delt);
+
diff --git a/1328/CH13/EX13.6a/13_6a.sce b/1328/CH13/EX13.6a/13_6a.sce
new file mode 100644
index 000000000..1dde88f6f
--- /dev/null
+++ b/1328/CH13/EX13.6a/13_6a.sce
@@ -0,0 +1,265 @@
+printf("\t example 13.6a \n");
+printf("\t approximate values are mentioned in the book \n");
+
+ds=[0 10 20 30 40 50 60 70 80 90 100];
+tmp=[90 145 180 208 234 260 286 312 338 367 400];
+clf();
+subplot(3,2,1);
+plot2d(ds,tmp,style=2,rect=[0,80,100,400]);
+xtitle("Plot of ASTM curve",boxed=1);
+xlabel("Per cent distilled off");
+ylabel("Temperature °F");
+
+//From the plotted ASTM curve and reference line
+s = (312-145)/60; // (70% - 10%)/60%
+printf("\tSlope of ASTm = %.2f °F\n",s);
+ap = (180+260+338)/3; // (20% +50% +80%)/3
+printf("\tAverage 50prcnt point = %.1f °F\n",ap);
+
+fc = 38; //°F, from Fig.13.8
+printf("\t50prcnt point ASTM = 50prcnt point flash curve = %.0f °F\n",fc);
+fc1 = ap - fc; //°F, fixing first point on EFC
+printf("\t50prcnt on EFC = %.0f °F\n",fc1);
+
+s1 = 1.65; // (°F/%) from fig 13.10, upper curve
+ten = 221 - 40*s1; //
+printf("\t10prcnt on EFC = 50prcnt - 40prcnt = %.0f °F\n",ten);
+sty = 221 + 20*s1; //
+printf("\t70prcnt on EFC = 50prcnt + 20prcnt %.0f °F\n",sty);
+
+//Draw this line as a reference through the 50% point. Calculate the flash curve for different percentages off
+
+//0% off
+printf("\n\t0 prcnt off:\n");
+dela = 90 - 117; // Step (8)
+printf("\t\tDelT ASTM = %.0f °F\n",dela);
+delE = dela * 0.50; // Step (9)
+printf("\t\tDelT EFC = %.1f °F\n",delE);
+FE = 139 - delE; // Step (10)
+printf("\t\t°F EFC = %.1f\n",FE);
+//end
+ov=13300; //lb/hr
+ng=90;//lb/hr
+mng=50;// mol. wt
+st=370;//lb/hr
+avG=50;//°F API
+//For 80%
+ouc=ov*0.80;//lb/hr
+printf("\toil uncondensed = %.0f lb/hr\n",ouc);
+avB=269;//°F,from Fig. 13.13
+printf("\tAverage boiling point from the EFC at 1 atm = %.0f°F\n",avB);
+avB1=avB+17;//°F,from Fig. 13.13
+printf("\tAverage boiling point from the EFC at 19.7 psia = %.0f°F\n",avB1);
+mwt=113;//mol. wt
+mtoc=ouc/mwt;
+printf("\tThe moles of oil still to be condensed = %.1f\n",mtoc);
+mg1=ng/mng;
+ms1=st/18;
+tm=mg1+ms1+mtoc;
+printf("\t\tMols gas = %.2f\n\t\tMols steam = %.1f\n",mg1,ms1);
+printf("\t\t\t -----\n\t\tMols total = %.1f\n",tm);
+tp=19.7;//psia
+poil=(mtoc/tm)*tp;//psia
+printf("\tPartial pressure of oil = %.1f psia\n",poil);
+pgas=(mg1/tm)*tp;//psia
+printf("\tPartial pressure of NC gas = %.3f psia\n",pgas);
+tm(1)=95;//°F
+tm(2)=127;//°F
+tm(3)=163;//°F
+tm(4)=205;//°F
+tm(5)=240;//°F
+pp(1)=6.73;
+pp(2)=9.40;
+pp(3)=12.25;
+pp(4)=14.64;
+pp(5)=15.65;
+psat(1)=0.815;//From steam table
+psat(2)=2.050;//From steam table
+psat(3)=5.09;//From steam table
+psat(4)=12.77;//From steam table
+psat(5)=24.97;//From steam table
+printf("\n\t\tCALCULATION OF DEW POINT OF THE STEAM\n");
+printf("\tT,°F\t[pt - (poil+pNC)] = psteam\tpsat(steam tables)\n");
+i=1;
+while(i<6)
+ ps=tp-pp(i);
+ printf("\t"+string(tm(i))+"\t%.1f\t %.2f\t\t%.2f\t%.3f\n",tp,pp(i),ps,psat(i));
+ i=i+1;
+end
+subplot(3,2,2);
+plot2d(psat,tm,style=3,rect=[0,25,90,250]);
+xtitle("Computed pressure of steam",boxed=1);
+xlabel("Pressure of steam, psi");
+ylabel("Temperature °F");
+
+ds=6.417;//psia,at 173°F,
+printf("\tAt 173°F, the dew point of steam, psat = %.3f psia\n",ds);
+pd1=tp-ds;//psia
+printf("\tpoil + pNC = %.2f psia\n",pd1);
+x=((tp*ms1)/ds)-(ms1+mg1);// mols oil
+printf("\tOil = %.2f mols oil\n",x);
+mw=85;//From fig. 13.14
+printf("\tThe molecular weight of the vapors is %.0f\n",mw);
+lv=x*mw;//lb
+printf("\tLb/hr vapor = %.0f\n",lv);
+prc=((ov-lv)*100)/ov;//%
+printf("\tpercent Condensed = %.0f\n",prc);
+printf("\n\t\t\tOIL CONDENSING CURVE\n");
+printf("\tprcnt\tCondensables\t\tAv BP on EFC\t\t50° API\t\tMol oil\t\tMol NC gas\tMol steam\tMol total\tTotal pressure\tPartial pressure\tPartial pressure\tCond temp,°F\n\t\tlb.hr\t\t14.7 psia °F\t19.7 psia,°F\tmol.wt\t\t\t\t\t\t\t\t\t\tpsia\t\toil,psia\t\tNC gas, psia\n");
+mo(1)=107.5;
+mo(2)=94.3;
+mo(3)=77.7;
+mo(4)=57.4;
+mo(5)=31.8;
+mo(6)=17.1;
+mo(7)=8.9;
+i=1;
+while(i<8)
+ mt(i)=mo(i)+mg1+ms1;
+ ppo(i)=(mo(i)/mt(i))*tp;
+ ppg(i)=(mg1/mt(i))*tp;
+ i=i+1;
+end
+printf("\t---------------------------------------------------------------------------------------------------------------------------------------------------------------------------------------------------------------------\n");
+printf("\t100\t13330\t\t300\t\t317\t\t124\t\t%.1f\t\t1.8\t\t20.6\t\t%.1f\t\t19.7\t\t%.1f\t\t\t%.3f\t\t\t305\n",mo(1),mt(1),ppo(1),ppg(1));
+printf("\t80\t10664\t\t269\t\t286\t\t113\t\t%.1f\t\t1.8\t\t20.6\t\t%.1f\t\t19.7\t\t%.1f\t\t\t%.3f\t\t\t277\n",mo(2),mt(2),ppo(2),ppg(2));
+printf("\t60\t7998\t\t239\t\t256\t\t103\t\t%.1f\t\t1.8\t\t20.6\t\t%.1f\t\t19.7\t\t%.1f\t\t\t%.3f\t\t\t240\n",mo(3),mt(3),ppo(3),ppg(3));
+printf("\t40\t5332\t\t207\t\t224\t\t93\t\t%.1f\t\t1.8\t\t20.6\t\t%.1f\t\t19.7\t\t%.1f\t\t\t%.3f\t\t\t205\n",mo(4),mt(4),ppo(4),ppg(4));
+printf("\t20\t2666\t\t178\t\t195\t\t84\t\t%.1f\t\t1.8\t\t20.6\t\t%.1f\t\t19.7\t\t%.1f\t\t\t%.3f\t\t\t163\n",mo(5),mt(5),ppo(5),ppg(5));
+printf("\t10\t1333\t\t155\t\t172\t\t78\t\t%.1f\t\t1.8\t\t20.6\t\t%.1f\t\t19.7\t\t%.1f\t\t\t%.3f\t\t\t127\n",mo(6),mt(6),ppo(6),ppg(6));
+printf("\t5\t667\t\t141\t\t158\t\t75\t\t%.1f\t\t1.8\t\t20.6\t\t%.1f\t\t19.7\t\t%.1f\t\t\t%.3f\t\t\t95\n",mo(7),mt(7),ppo(7),ppg(7));
+
+//Trail 1:
+m=78;//50° API mol. wt. for condesables 1333
+vap=(ov*0.10)/78;//Mol/hr
+printf("\n\t\t\t\tMol/hr\n\tOil vapor\t\t%.1f\n\tNC gas\t\t\t%.1f\n\tSteam\t\t\tX\n\tTotal\t\t\t18.9+X\n",vap,mg1);
+vap1=vap+mg1;//Mol/hr
+psteam=5.09;//psia, For 163°F
+x1=(psteam*vap1)/(tp-psteam);//mols steam
+printf("\tX = %.2f mols steam\n",x1);
+tv=vap1+x1;
+printf("\n\t\t\tMol/hr\tmf\tmf*pt = p-partial\n");
+mf1=vap/(tv);
+ppar1=mf1*tp;
+printf("\tOil vapor\t%.1f\t%.3f\t%.2f\n",vap,mf1,ppar1);
+mf2=mg1/tv;
+ppar2=mf2*tp;
+printf("\tNC gas\t\t%.1f\t%.3f\t%.2f\n",mg1,mf2,ppar2);
+mf3=x1/tv;
+ppar3=mf3*tp;
+printf("\tSteam\t\t%.2f\t%.3f\t%.2f\n",x1,mf3,ppar3);
+tot1=vap+mg1+x1;
+tot2=mf1+mf2+mf3;
+tot3=ppar1+ppar2+ppar3;
+printf("\tTotal\t\t%.2f\t%.3f\t%.2f\n",tot1,tot2,tot3);
+//Error was found. So trail 2 is done in a similar way
+printf("\n\tSimilarly,\n\tT,°F\tOil cond, prcnt\tOil cond, lb\tSteam cond,lb\n");
+printf("\t173\t74\t\t9863\t\t0\n\t163\t85\t\t11350\t\t204\n\t127\t97.5\t\t13000\t\t357\n\t95\t100\t\t13330\t\t370\n");
+//Condensing curve
+printf("\n\t\t\tOil\t\t\t\tSteam\n\t-----------------------------------------------------------------\n\tTc,°F\tHv,vapor\tHl,liquid\tHg or Hv,\tHl,liquid\n\t\t\t\t\t\tgas or vapor\n");
+printf("\t-----------------------------------------------------------------\n")
+printf("\t305\t368\t\t242\t\t1197.0\t\tSuperheated\n\t277\t359\t\t225\t\t1184.1\t\tSuperheated\n\t240\t337\t\t204\t\t1167.0\t\tSuperheated\n\t205\t322\t\t185\t\t1150.6\t\tSuperheated\n\t173\t310\t\t168\t\t1135.4\t\t140.9\n");//From fig.11 in Appendix and steam tables
+//Heat load
+//305°F:
+hvv=368;
+hvg=1197.0;
+olv=ov*hvv;
+stm=st*hvg;
+ncg=ng*(0.46*273);
+thh=olv+stm+ncg;
+printf("\n\t\t\t\tH\t\tq\n");
+printf("\tOil vapor\t\t%.2e\n\tSteam\t\t\t%.2e\n\tNC gas\t\t\t%.2e\n\t\t\t\t--------\n\t\t\t\t%.4e\t0\n",olv,stm,ncg,thh);
+//Similarily at other temperatures
+ttp(1)=305;//°F
+ttp(2)=277;//°F
+ttp(3)=240//°F
+ttp(4)=205;//°F
+ttp(5)=173;//°F, Dew point of steam
+ttp(6)=163;//°F
+ttp(7)=127;//°F
+ttp(8)=95;//°F
+
+hld(1)=0;//million Btu
+hld(2)=0.55;//milllion Btu
+hld(3)=1.2;//million Btu
+hld(4)=1.75;//million Btu
+hld(5)=2.3;//million Btu
+hld(6)=2.73;//million Btu
+hld(7)=3.3;//million Btu
+hld(8)=3.66;//million Btu
+subplot(2,2,3);
+plot2d(hld,ttp,style=6,rect=[0,60,3.8,320]);
+xtitle("Condensation of mixed hydrocarbons with gas and steam",boxed=1);
+xlabel("Heat load, million Btu");
+ylabel("Temperature °F");
+//summary
+dp=3042800;//Btu/hr
+ttt=3638400;//Btu/hr
+i2s=thh-dp;//Btu/hr
+printf("\tInlet to steam dew point = %.4eBtu/hr\n",i2s);
+so=dp-1735900;//Btu/hr
+printf("\tSteam dew point to outlet = %.4e Btu/hr\n",so);
+totl=i2s+so;//Btu/hr
+printf("\tTotal\t\t\t= %.4e Btu/hr\n",totl);
+twa=ttt/(120-85);
+printf("\tTotal water = %.2e lb/hr\n",twa);
+wt=85+((1306900/ttt)*35);//°F
+printf("\tWater temperature at dew point of steam = %.0f°F\n",wt);
+//Weighted true temperature difference, delT:
+ //Inlet to dew point of steam:
+delq=2331500;
+delt1=122.2;
+UA1=delq/delt1;
+printf("\tUA = %.0f\n",UA1);
+printf("\n\tDew point of steam to oulet\n");
+printf("\tq\tdelq\tTc\ttw\tdelTav\t(delq/delTav) = UA\n");
+printf("\t----------------------------------------------------------\n");
+q(1)=2331500;
+q(2)=2500000;
+q(3)=2750000;
+q(4)=3000000;
+q(5)=3250000;
+q(6)=3500000;
+q(7)=3638000;
+i=1;
+while(i<7)
+ dq(i)=q(i+1)-q(i);
+ i=i+1;
+end
+dpt(1)=173;
+dpt(2)=169;
+dpt(3)=161;
+dpt(4)=149;
+dpt(5)=134;
+dpt(6)=112;
+dpt(7)=95;
+dtw(1)=97.5;
+dtw(2)=96;
+dtw(3)=93;
+dtw(4)=91;
+dtw(5)=89;
+dtw(6)=86;
+dtw(7)=85;
+i=1;
+tua=0;
+while(i<7)
+ dpdelt(i)=((dpt(i+1)-dtw(i+1))+(dpt(i)-dtw(i)))/2;
+ UA(i)=dq(i)/dpdelt(i);
+ tua=tua+UA(i);
+ i=i+1;
+end
+printf("\t2331500\t......\t173\t173\t97.5\n");
+i=1;
+while(i<7)
+ printf("\t"+string(q(i+1))+"\t"+string(dq(i))+"\t"+string(dpt(i+1))+"\t"+string(dtw(i+1))+"\t"+string(dpdelt(i))+"\t%.0f\n",UA(i));//from Fig. 13.16
+i=i+1;
+end
+
+printf("\t\t\t\t\t\t%.0f\tUA = sigma{delq/delt}\n",tua);
+wdt=1306900/tua;//°F
+printf("\tWeighted delt = %.1f°F\n",wdt);
+owdt=ttt/(tua+UA1);//°F
+printf("\tOverall weighted temperature difference = %.1f °F\n",owdt);
+printf("\tThe uncorrected LMTD is 60.1°F\n");
+//end
+
diff --git a/1328/CH13/EX13.6b/13_6b.sce b/1328/CH13/EX13.6b/13_6b.sce
new file mode 100644
index 000000000..bb334647e
--- /dev/null
+++ b/1328/CH13/EX13.6b/13_6b.sce
@@ -0,0 +1,91 @@
+printf("\t example 13.6b \n");
+printf("\t approximate values are mentioned in the book \n");
+
+// EXCHANGER
+//Shell side
+Id = 27; // inches
+Bs = 16; // inches
+Ps = 1; // passes
+
+//Tube side
+N = 286; // number
+l = 12; // inches
+Od = 1; // inch
+BWG = 14; // bWG
+Ptc = 1.25; //inches
+Ps1 = 8; // passes
+
+//Clesan surface requirements
+
+//Head load inlet to dew point of steam
+st = 2331500; // Btu/hr
+delT = 122.2 // °F
+hio = 700; // Btu/((hr)(ft^2)(°F)) for water
+
+//From table 13.4 at inlet
+NC = 1.8; //NC gas, mol/hr
+sm = 20.6;// steam, mol/hr
+tt = NC + sm;// mol/hr
+printf("\tNC gas + steam is %.1f mol/hr\n",tt);
+pN = tt/129.9; // mol/hr
+printf("\tpercentage NC gas is %.4f\n",pN);
+
+//From Fig 13.17
+hn = 205; //Btu/((hr)(ft^2)(°F))
+//At dew point of steam
+No=40.75; // Mol/hr
+t1 = tt + No; // Mol/hr, total
+pN1 = tt/t1; // Mol/hr, %NC
+printf("\tpercentage NC is %.3f\n",pN1);
+
+//From fig 13.7
+hn1 = 140; //Btu/((hr)(ft^2)(°F))
+lm = 136.5; //Btu/((hr)(ft^2)(°F))
+delT = 122.2; // °F
+Ac1 = st/(lm * delT); // ft^2
+printf("\tAc1 = Q/(U * delT) is %.1f ft^2\n",Ac1);
+
+//At dew point of steam to oulet
+sm1 = 20.64; // Mol/hr , Steam
+t2 = NC + sm1; // total, Mol/hr
+printf("\tNC gas + steam is %.1f mol/hr\n",t2);
+pN1 = NC/t2; // % NC gas
+printf("\tpercentage NC gas is %.3f \n",pN1);
+
+Uc = 212; // From Fig 13.17, weighted for oil and steam
+
+//At outlet, steam = negligible
+
+Uc = 15;//From Fig 13.17
+
+//Log mean overall coefficient
+lm = 74.5; // Btu/((hr)(ft^2)(°F)) , From Fig 13.17
+delT = 44.8; // °F
+Ac2 = 1306900/(lm * delT);
+printf("\tAc2 is %.0f ft^2\n",Ac2);
+
+hl = 770000; // Btu/hr
+printf("\tHeat of Liquid(50°API) is %.1ef\n",hl);
+wr = (hl/3638400)*35; // °F
+printf("\tWater rise = %.1f °F\n",wr);
+
+LMTD = 66.3; //°F
+U1=50 //for free convection
+As = hl/(U1*LMTD);// ft^2
+printf("\tAs = %.1f ft^2\n",As);
+Ac = Ac1 + Ac2 + As; //ft^2
+printf("\tTotal clean surface %.0f ft^2\n",Ac);
+
+Uc = 3638400/(Ac * 75.5); // Btu/((hr)(ft^2)(°F))
+printf("\tClean overall coefficient Uc = %.1f Btu/((hr)(ft^2)(°F))\n",Uc);
+
+x = 0.2618; // ft, from table 10
+A = N * l * x; //ft^2
+Ud = 3638400/(A * 75.5);
+printf("\tDesign coefficient Ud is %.1f\n",Ud);
+Rd =(Uc - Ud)/(Uc * Ud); // ((hr)(ft^2)(°F))/Btu
+printf("\tDirt factor Rd is %.4f ((hr)(ft^2)(°F))/Btu\n",Rd);
+
+yo = (As/Ac)*A; // ft^2
+printf("\tSubmerge = %.0f ft^2 of surface\n",yo);
+//end
generated by cgit (git 2.34.1) at 2024-12-22 19:09:14 +0000