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 --- 3516/CH13/EX13.1/Ex13_1.sce | 207 +++++++++++++++++++++++++ 3516/CH13/EX13.2/Ex13_2.sce | 59 ++++++++ 3516/CH13/EX13.3/Ex13_3.sce | 195 ++++++++++++++++++++++++ 3516/CH13/EX13.4/Ex13_4.sce | 11 ++ 3516/CH13/EX13.5/Ex13_5.sce | 121 +++++++++++++++ 3516/CH13/EX13.6/Ex13_6.sce | 357 ++++++++++++++++++++++++++++++++++++++++++++ 6 files changed, 950 insertions(+) create mode 100644 3516/CH13/EX13.1/Ex13_1.sce create mode 100644 3516/CH13/EX13.2/Ex13_2.sce create mode 100644 3516/CH13/EX13.3/Ex13_3.sce create mode 100644 3516/CH13/EX13.4/Ex13_4.sce create mode 100644 3516/CH13/EX13.5/Ex13_5.sce create mode 100644 3516/CH13/EX13.6/Ex13_6.sce (limited to '3516/CH13') diff --git a/3516/CH13/EX13.1/Ex13_1.sce b/3516/CH13/EX13.1/Ex13_1.sce new file mode 100644 index 000000000..18e1019e8 --- /dev/null +++ b/3516/CH13/EX13.1/Ex13_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/3516/CH13/EX13.2/Ex13_2.sce b/3516/CH13/EX13.2/Ex13_2.sce new file mode 100644 index 000000000..387a23df0 --- /dev/null +++ b/3516/CH13/EX13.2/Ex13_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/3516/CH13/EX13.3/Ex13_3.sce b/3516/CH13/EX13.3/Ex13_3.sce new file mode 100644 index 000000000..50166d3e7 --- /dev/null +++ b/3516/CH13/EX13.3/Ex13_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/3516/CH13/EX13.4/Ex13_4.sce b/3516/CH13/EX13.4/Ex13_4.sce new file mode 100644 index 000000000..03e5d39b0 --- /dev/null +++ b/3516/CH13/EX13.4/Ex13_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/3516/CH13/EX13.5/Ex13_5.sce b/3516/CH13/EX13.5/Ex13_5.sce new file mode 100644 index 000000000..308dd8fa4 --- /dev/null +++ b/3516/CH13/EX13.5/Ex13_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/3516/CH13/EX13.6/Ex13_6.sce b/3516/CH13/EX13.6/Ex13_6.sce new file mode 100644 index 000000000..221b17a55 --- /dev/null +++ b/3516/CH13/EX13.6/Ex13_6.sce @@ -0,0 +1,357 @@ +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 + + +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 -- cgit