initial commit / add all books

1 files changed, 195 insertions, 0 deletions

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