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12 files changed, 278 insertions, 0 deletions

diff --git a/2510/CH18/EX18.10/Ex18_10.sce b/2510/CH18/EX18.10/Ex18_10.sce
new file mode 100755
index 000000000..f4302600a
--- /dev/null
+++ b/2510/CH18/EX18.10/Ex18_10.sce
@@ -0,0 +1,23 @@
+//Variable declaration:
+T1 = 2000                       //Hot gas temperature ( F)
+T2 = 550                        //Cool gas temperature ( F)
+T3 = 330                        //Steam temperature ( F)
+T4 = 140                        //Water temperature ( F)
+m = 30000                       //Mass flow rate of steam (lb/h)
+cp = 0.279                      //Average heat capacity of gas (Btu/lb. F)
+N = 800                         //Number of boiler tubes
+
+//Calculation:
+DT = (T1-T3)/(T2-T3)            //Temperature difference ratio
+Tav = (T1+T2)/2                 //Average gas temperature ( F)
+//From steam tables (Appendix):
+hs = 1187.7                     //Steam enthalpy (Btu/lb)
+hw = 107.89                     //Water enthalpy (Btu/lb)
+Q = m*(hs-hw)                   //Heat duty (Btu/h)
+mh = Q/cp*(T1-T2)               //Mass flow rate of gas (lb/h)
+x = mh/N                        //Gas mass flow rate per tube (lb/h)
+//From figure 18.5:
+L = 15                          //Length of boiler tubes (ft)
+
+//Result:
+printf("The length of boiler tubes is : %f ft .",L)
diff --git a/2510/CH18/EX18.12/Ex18_12.sce b/2510/CH18/EX18.12/Ex18_12.sce
new file mode 100755
index 000000000..e93d703e2
--- /dev/null
+++ b/2510/CH18/EX18.12/Ex18_12.sce
@@ -0,0 +1,30 @@
+
+//Variable declaration:
+T1 = 1800                       //Hot gas temperature ( F)
+T2 = 500                        //Cool gas temperature ( F)
+//From steam tables:
+Tw = 312                        //Boiling point of water at 80 psia ( F)
+m1 = 120000                     //Mass flow rate of flue gas (lb/h)
+D = 2/12                        //Inside diameter of tube (ft)
+cp = 0.26                       //Average heat capacity of flue gas (Btu/lb. F)
+
+//Calculation:
+DT = (T1-Tw)/(T2-Tw)            //Temperature difference ratio
+Tav = (T1+T2)/2                 //Average gas temperature ( F)
+//From figure 18.4:
+x = 150                         //Gas mass flow rate per tube (m/N) (lb/h)
+N = m1/x                        //Number of tubes
+L = 21.5                        //Length of tubes (ft)
+A = N*L*D                       //Total heat transfer area (ft^2)
+Q = m1*cp*(T1-T2)               //Heat duty (Btu/h)
+//From steam tables (Appendix):
+hs = 1183.1                     //Steam enthalpy at 80 psia (Btu/lb)
+hw = 168.1                      //Water enthalpy at 200 F (Btu/lb)
+m2 = Q/(hs-hw)                  //Mass flow rate of water (lb/h)
+m2 = round(m2*10**-4)/10**-4
+
+//Result:
+printf("The required heat transfer area is : %.0f ft^2 .",A)
+printf("The tube length is : %f ft .",L)
+printf("The heat duty is : %.2f x 10^7 .",Q/10**7)
+printf("The water mass flow rate is : %f lb/h .",m2)
diff --git a/2510/CH18/EX18.18/Ex18_18.sce b/2510/CH18/EX18.18/Ex18_18.sce
new file mode 100755
index 000000000..3ba48e148
--- /dev/null
+++ b/2510/CH18/EX18.18/Ex18_18.sce
@@ -0,0 +1,24 @@
+//Variable declaration:
+m1 = 144206                     //Mass flow rate of flue gas (lb/h)
+cp = 0.3                        //Average flue gas heat capacity (Btu/lb. F)
+T1 = 2050                       //Initial temperature of gas ( F)
+T2 = 560                        //Final temperature of gas ( F)
+T3 = 70                         //Ambient air temperature ( F)
+
+//Calculation:
+Q = m1*cp*(T1-T2)               //Duty rate (Btu/h)
+//From appendix:
+cpa = 0.243                     //Average ambient air heat capacity 70 F (Btu/lb. F)
+MW = 29                         //Molecular weight of air at 70 F
+Q5 = round(Q*10**-5)/10**-5
+ma = Q5/(cpa*(T2-T3))  //Mass of air required (lb/h)
+m2 = round(ma)/MW               //Moles of air required (lb mol/h)
+m3 = round(ma)*13.32            //Volume of air required (ft^3/h)
+ma = round(ma*10**-2)/10**-2
+m2 = round(m2*10**-1)/10**-1
+m3 = round(m3*10**-3)/10**-3
+
+//Result:
+printf("The mass of air required is : %f lb/h .",ma)
+printf("The moles of air required is : %f lb mol/h .",m2)
+printf("The volume of air required is : %f ft^3/h .",m3)
diff --git a/2510/CH18/EX18.19/Ex18_19.sce b/2510/CH18/EX18.19/Ex18_19.sce
new file mode 100755
index 000000000..5664a05fb
--- /dev/null
+++ b/2510/CH18/EX18.19/Ex18_19.sce
@@ -0,0 +1,20 @@
+//Variable declaration:
+//From example 18.19:
+m1 = 144200                     //Mass flow rate of flue gas (lb/h)
+m2 = 541700                     //Mass flow rate of air (lb/h)
+R = 0.73                        //Universal gas constant (psia.ft^3/lbmol. R)
+P = 1                           //Absolute pressure (psia)
+T = 1020                        //Absolute temperature ( R)
+MW = 29                         //Molecular weight of air
+t = 1.5                         //Residence time (s)
+
+//Calculation:
+m = m1+m2                       //Total mass flow rate of the gas (lb/h)
+q = m*R*T/(P*MW)                //Volumetric flow at 560 F (ft^3/h)
+V = q*t/3600                    //Volume of tank (ft^3)
+m = round(m*10**-2)/10**-2
+
+//Result:
+printf("The total mass flow rate of the gas is : %f lb/h .",m)
+printf("The volumetric flow at 560 F is : %.2f  x 10^7 ft^3/h",q/10**7)
+printf("The volume of tank is : %.0f ft^3 .",V)
diff --git a/2510/CH18/EX18.2/Ex18_2.sce b/2510/CH18/EX18.2/Ex18_2.sce
new file mode 100755
index 000000000..298ac5bd3
--- /dev/null
+++ b/2510/CH18/EX18.2/Ex18_2.sce
@@ -0,0 +1,19 @@
+//Variable declaration:
+T1 = 25                      //Temperature of H2SO4 ( C)
+m = 50+200                   //Mass of H2SO4 (lb)
+//From figure 18.2:
+W1 = 50+100                  //Weight of H2SO4 (lb)
+W2 = 100                     //Weight of H2O (lb)
+
+//Calculation:
+m = W1/(W1+W2)*100          //Percent weight of H2SO4 (%)
+m2 = W1+W2                  //Mass of mixture (lb)
+//From fgure 18.2:
+T2 = 140                    //Final temperature between the 50% solution and pure H2SO4 at  25 C ( F)
+h1 = -86                    //Specific heat capacity of H2O (Btu/lb)
+h2 = -121.5                 //Specific heat capacity of H2SO4 (Btu/lb)
+Q = m2*(h2-h1)              //Heat transferred (Btu)
+
+//Result:
+printf("The final temperature between the 50%% solution and pure H2SO4 at  25 C is : %.0f F .",T2)
+printf("The heat transferred is : %.0f Btu .",Q)
diff --git a/2510/CH18/EX18.20/Ex18_20.sce b/2510/CH18/EX18.20/Ex18_20.sce
new file mode 100755
index 000000000..4ca382903
--- /dev/null
+++ b/2510/CH18/EX18.20/Ex18_20.sce
@@ -0,0 +1,11 @@
+//Variable declaration:
+//Fro example 18.20:
+V = 7335                    //Volume of tank (ft^3)
+
+//Calculation:
+D = (4*V/%pi)**(1/3)         //Diameter of tank (ft)
+H = D                       //Height of tube (ft)
+
+//Result:
+printf("The diameter of tank is : %.2f ft .",H)
+printf("The height of tube is : %.2f ft .",D)
diff --git a/2510/CH18/EX18.21/Ex18_21.sce b/2510/CH18/EX18.21/Ex18_21.sce
new file mode 100755
index 000000000..392267b1d
--- /dev/null
+++ b/2510/CH18/EX18.21/Ex18_21.sce
@@ -0,0 +1,17 @@
+//Variable declaration:
+m1 = 144206                     //Mass flow rate of flue gas (lb/h)
+cp1 = 0.3                       //Average heat capacities of the flue gas (Btu/lb F)
+cp2 = 0.88                      //Average heat capacities of the solid (Btu/lb F)
+//From example 18.18:
+T1 = 550                        //Initial temperature of gas ( F)
+T2 = 2050                       //Final temperature of gas ( F)
+T3 = 70                         //Initial temperature of solid ( F)
+T4 = 550-40                     //Final temperature of solid ( F)
+
+//Calculation:
+Dhf = m1*cp1*(T2-T1)            //For the flue gas, the enthalpy change for one hour of operation (Btu)
+Dhs = round(Dhf*10**-4)/10**-4  //For the solids, the enthalpy change for one hour of operation (Btu)
+m2 = Dhs/(cp2*(T4-T3))          //Mass of solid (lb)
+
+//Result:
+printf("The mass of solid is : %.0f lb .",m2)
diff --git a/2510/CH18/EX18.22/Ex18_22.sce b/2510/CH18/EX18.22/Ex18_22.sce
new file mode 100755
index 000000000..f2a0c1083
--- /dev/null
+++ b/2510/CH18/EX18.22/Ex18_22.sce
@@ -0,0 +1,26 @@
+//Variable declaration:
+//From example 18.21:
+m = 144206                      //Mass flow rate of flue gas (lb/h)
+cp = 0.3                        //Average heat capacities of the flue gas (Btu/lb F)
+T1 = 2050                       //Initial temperature of gas ( F)
+T2 = 180                        //Final temperature of gas ( F)
+T3 = 60                         //Ambient air temperature ( F)
+U = 1.5                         //Overall heat transfer coefficient for cooler (Btu/h.ft^2. F)
+MW = 28.27                      //Molecular weight of gas
+R = 379                         //Universal gas constant (psia.ft^3/lbmol. R)
+v = 60                          //Duct or pipe velcity at inlet (2050 F) (ft/s)
+pi = %pi
+
+//Calculation:
+Q = m*cp*(T1-T2)                //Heat duty (Btu/h)
+DTlm = ((T1-T3)-(T2-T3))/log((T1-T3)/(T2-T3))   //Log-mean temperature difference ( F)
+A1 = round(Q * 10**-5)/10**-5/(U*round(DTlm))                 //Radiative surface area (ft^2)
+q = m*R*(T1+460)/(T3+460)/MW    //Volumetric flow at inlet (ft^3/h)
+A2 = q/(v*3600)                 //Duct area (ft^2)
+D = sqrt(A2*4/pi)               //Duct diameter (ft)
+L = A1/(pi*D)                   //Length of required heat exchange ducting (ft)
+A1 = round(A1*10**-1)/10**-1
+
+//Result:
+printf(" The radiative surface area required is : %f ft^2 .",A1)
+printf(" The length of required heat exchange ducting is : %.0f ft .",L)
diff --git a/2510/CH18/EX18.3/Ex18_3.sce b/2510/CH18/EX18.3/Ex18_3.sce
new file mode 100755
index 000000000..4f40560d0
--- /dev/null
+++ b/2510/CH18/EX18.3/Ex18_3.sce
@@ -0,0 +1,22 @@
+//Variable declaration:
+F = 10000                       //Mass flow rate of NaOH (lb/h)
+C1 = 10                         //Old concentration of NaOH solution (%)
+C2 = 75                         //New concentration of NaOH solution (%)
+h1 = 1150                       //Enthalpy of saturated steam at 14.7 psia (Btu/lb)
+U = 500                         //Overall heat transfer coefficient (Btu/h.ft^2. F)
+T1 = 212                        //Absolute temperature of evaporator ( F)
+T2 = 340                        //Saturated steam temperature ( F)
+
+//Calculation:
+L = F*(C1/100)/(C2/100)         //Flow rate of steam leaving the evaporator (lb/h)
+V = F-L                         //Overall material balance (lb/h)
+//From figure 18.3:
+hF = 81                         //Enthalpy of solution entering the unit (Btu/lb)
+hL = 395                        //Enthalpy of the 75% NaOH solution (Btu/lb)
+Q = round(V)*h1+round(L)*hL-F*hF    //Evaporator heat required (Btu/h)
+A = Q/(U*(T2-T1))               //Area of the evaporaor (ft^2)
+Q = round(Q*10**-2)/10**-2
+
+//Result:
+printf("The heat transfer rate required for the evaporator is : %f Btu/h ",Q)
+printf("The area requirement in the evaporator is : %.1f ft^2 .",A)
diff --git a/2510/CH18/EX18.4/Ex18_4.sce b/2510/CH18/EX18.4/Ex18_4.sce
new file mode 100755
index 000000000..c4dcf90f5
--- /dev/null
+++ b/2510/CH18/EX18.4/Ex18_4.sce
@@ -0,0 +1,19 @@
+//Variable declaration:
+U1 = 240                    //Overall heat transfer coefficient for first effect (Btu/h.ft^2. F)
+U2 = 200                    //Overall heat transfer coefficient for second effect (Btu/h.ft^2. F)
+U3 = 125                    //Overall heat transfer coefficient for third effect (Btu/h.ft^2. F)
+A1 = 125                    //Heating surface area in first effect (ft^3)
+A2 = 150                    //Heating surface area in second effect (ft^3)
+A3 = 160                    //Heating surface area in third effect (ft^3)
+T1 = 400                    //Condensation stream temperature in the first effect ( F)
+T2 = 120                    //Vapor leaving temperature in the first effect ( F)
+
+//Calculation:
+R1 = 1/(U1*A1)              //Resistance across first effect
+R2 = 1/(U2*A2)              //Resistance across second effect
+R3 = 1/(U3*A3)              //Resistance across third effect
+R = R1+R2+R3                //Total resistance
+DT1 = (R1/R)*(T1-T2)        //Temperature drop across the heating surface in the first effect ( F)
+
+//Result:
+printf("The temperature drop across the heating surface in the first effect is : %.0f F .",DT1)
diff --git a/2510/CH18/EX18.6/Ex18_6.sce b/2510/CH18/EX18.6/Ex18_6.sce
new file mode 100755
index 000000000..60d79b610
--- /dev/null
+++ b/2510/CH18/EX18.6/Ex18_6.sce
@@ -0,0 +1,32 @@
+//Variable declaration:
+F = 5000                        //Mass of soltuion fed in the evaporator (lb)
+xF = 2/100                      //Concentration of feed
+xL = 5/100                      //Concentration of liquor
+U = 280                         //Overall heat transfer coefficient (Btu/h.ft^2. F)
+//From figure 18.1 & 18.3:
+TF = 100                        //Feed temperature ( F)
+TS = 227                        //Steam temperature ( F)
+TV = 212                        //Vapour temperature ( F)
+TL = 212                        //Liquor temperature ( F)
+TC = 227                        //Condensate temperature ( F)
+
+//Calculation:
+//From steam tables:
+hF = 68                         //Enthalpy of feed (Btu/lb)
+hL = 180                        //Enthalpy of liquor (Btu/lb)
+hV = 1150                       //Enthalpy of vapour (Btu/lb)
+hS = 1156                       //Enthalpy of steam (Btu/lb)
+hC = 195                        //Enthalpy of condensate (Btu/lb)
+s1 = F*xF                       //Total solids in feed (lb)
+w = F-s1                        //Total water in feed (lb)
+s2 = F*xF                       //Total solids in liquor (lb)
+L = s2/xL                       //Total water in liquor (lb)
+V = F-L                         //Overall balance (lb)
+S = (V*hV+L*hL-F*hF)/(hS-hC)    //Mass of steam (lb)
+Q = S*(hS-hC)                   //Total heat requirement (Btu)
+A = Q/(U*(TS-TL))               //Required surface aea (ft^2)
+
+//Result:
+printf("The mass of vapor produced is : %.0f lb .",V)
+printf("The total mass of steam required is : %.0f lb .",S)
+printf("The surface area required is : %.0f ft^2 .",A)
diff --git a/2510/CH18/EX18.7/Ex18_7.sce b/2510/CH18/EX18.7/Ex18_7.sce
new file mode 100755
index 000000000..68b181326
--- /dev/null
+++ b/2510/CH18/EX18.7/Ex18_7.sce
@@ -0,0 +1,35 @@
+
+//Variable declaration:
+F = 5000                        //Mass flow rate of NaOH (lb/h)
+xF = 20/100                     //Old concentration of NaOH solution
+TF = 100                        //Feed temperature ( F)
+xL = 40/100                     //New concentration of NaOH solution
+xv = 0                          //Vapour concentration at x
+yv = 0                          //Vapour concentration at y
+T1 = 198                        //Boiling temperature of solution in the evaporator ( F)
+T2 = 125                        //Saturated steam temperature ( F)
+U = 400                         //Overall heat transfer coefficient (Btu/h.ft^2. F)
+Ts = 228                        //Steam temperature ( F)
+
+//Calculation:
+//From steam tables at 228 F and 5 psig:
+hS = 1156                       //Enthalpy of steam (Btu/lb)
+hC = 196                        //Enthalpy of condensate (Btu/lb)
+hV = hS-hC                      //Enthalpy of vapour (Btu/lb)
+Tw = 125.4                      //Boiling point of water at 4 in Hg absolute ( F)
+hS2 = 1116                      //Enthalpy of saturated steam at 125 F (Btu/lb)
+hs = 0.46                       //Heat capacity of superheated steam (Btu/lb. F)
+//From figure 18.3:
+hF = 55                         //Enthalpy of feed (Btu/lb)
+hL = 177                        //Enthalpy of liquor (Btu/lb)
+L = F*xF/xL                     //Mass of liquor (lb)
+V = L                           //Mass of vapour (lb)
+hV = hS2+hs*(T1-T2)             //Enthalpy of vapour leaving the solution (Btu/lb)
+S = (V*hV+L*hL-F*hF)/(hS-hC)    //Mass flow rate of steam (lb/h)
+Q = S*(hS-hC)                   //Total heat requirement (Btu)
+A = Q/(U*(Ts-T1))               //Required heat transfer area (ft^2)
+S = round(S*10**-1)/10**-1
+
+//Result:
+printf("The steam flow rate is : %f lb/h .",S)
+printf("The required heat transfer area is : %.0f ft^2 .",A)