20 files changed, 396 insertions, 0 deletions
diff --git a/2762/CH2/EX2.10.1/2_10_1.sce b/2762/CH2/EX2.10.1/2_10_1.sce
new file mode 100755
index 000000000..ad2c15e39
--- /dev/null
+++ b/2762/CH2/EX2.10.1/2_10_1.sce
@@ -0,0 +1,25 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.10-1
+//Principles of Momentum Transfer and Overall Balances
+//given data
+h=0.0655;//pressure drop reading in m
+rhow=996;//density of water in kg/m3
+g=9.80665;//gravity force
+dP=h*rhow*g;//pressure drop
+//dP=(32*mu*v*(l2-l1/(D*D))) this implies---> v= dP*(D*D)/(32*mu*(l2-l1)
+D=2.22/1000;//capillary internal diameter
+mu=1.13/1000;//viscosity of liquid
+dl=0.317;//l2-l1= length of capillary being used in m
+v= dP*(D*D)/(32*mu*dl);//velocity in m/s
+V=(v*3.14*D*D)/4;//volumetric flow rate D=2.22/1000;//capillary internal diameter
+mu=1.13/1000;//viscosity of liquid
+rhol=875;//density of liquid in kg/m3
+Re=(D*v*rhol)/mu;
+if(Re<2100) then
+    disp("the flow is laminar")
+else
+    disp("the flow is turbulent")
+end
+mprintf("volumetric flow rate= %f m3/s",V)
+//end
diff --git a/2762/CH2/EX2.10.2/2_10_2.sce b/2762/CH2/EX2.10.2/2_10_2.sce
new file mode 100755
index 000000000..5bde53067
--- /dev/null
+++ b/2762/CH2/EX2.10.2/2_10_2.sce
@@ -0,0 +1,21 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.10-2
+//Principles of Momentum Transfer and Overall Balances
+//given data
+D=2.22/1000;//capillary internal diameter
+mu=1.13/1000;//viscosity of liquid
+D=2.22/1000;//capillary internal diameter
+rhol=875;//density of liquid in kg/m3
+dl=0.317;//l2-l1= length of capillary being used in m
+v=0.275;//velcity of liq in m/s
+Re=(D*v*rhol)/mu;//reynolds number
+if(Re<2100) then
+    disp("the flow is laminar")
+    f=16/Re;//fannings friction factor
+else
+    disp("the flow is turbulent")
+end
+dP=(4*f*rhol*dl*v*v)/(2*D);//pressure drop in Pa (Hagen Poiseulle equation)
+mprintf("pressure drop= %f Pa",dP)
+//end
diff --git a/2762/CH2/EX2.10.3/2_10_3.sce b/2762/CH2/EX2.10.3/2_10_3.sce
new file mode 100755
index 000000000..363a46c90
--- /dev/null
+++ b/2762/CH2/EX2.10.3/2_10_3.sce
@@ -0,0 +1,23 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.10-3
+//Principles of Momentum Transfer and Overall Balances
+//given data
+D=0.0525;//diameter of the pipe in m
+v=4.57;//vel of fluid in m/s
+rhol=801;//density of fluid in kg/m3
+mu=4.46/1000;//viscosity in kg/m.s
+Re=(D*v*rhol)/mu;//reynolds number
+E=4.6*(10^-5)
+if(Re<2100) then
+    disp("the flow is laminar")
+    f=16/Re;//fannings friction factor
+else
+    disp("the flow is turbulent")
+    k=E/D;
+end
+dl=36.6;//l2-l1= length of pipe being used in m
+f=0.0060;//for given Re
+Ff=(4*f*dl*v*v)/(2*D);//mechanical energy friction loss
+mprintf("mechanical energy friction loss= %f J/kg",Ff)
+//end
diff --git a/2762/CH2/EX2.10.5/2_10_5.sce b/2762/CH2/EX2.10.5/2_10_5.sce
new file mode 100755
index 000000000..0006e330f
--- /dev/null
+++ b/2762/CH2/EX2.10.5/2_10_5.sce
@@ -0,0 +1,18 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.10-5
+//Principles of Momentum Transfer and Overall Balances
+//given data
+D=0.01;//diameter of tube in m
+G=9;// rate of flow of N through tube in kg/s.m2
+mu=1.77/100000;//viscosity of gas
+Re=D*G/mu;//reynolds number
+p1=2.0265*100000;//entrance pressure
+f=0.009;//friction factor for given Re
+dl=200;//section of tube used in m
+R=8314.3;//gas constant
+T=298.15;//std temp given
+M=28.02;//molecular weight of N2
+p2=((p1^2)-((4*f*dl*G*G*R*T)/(M*D)))^0.5;//outlet pressure
+mprintf("outlet pressure= %f Pa",p2)
+//end
diff --git a/2762/CH2/EX2.2.1/2_2_1.sce b/2762/CH2/EX2.2.1/2_2_1.sce
new file mode 100755
index 000000000..6b3b19e62
--- /dev/null
+++ b/2762/CH2/EX2.2.1/2_2_1.sce
@@ -0,0 +1,15 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.2-1
+//Principles of Momentum Transfer and Overall Balances
+//given data
+//a)
+Fl=3*32.174*(1/32.174);// lbm*(ft/s^2)*(1/(ft/s^2))=m*g/gc
+//b)
+Fdyne=3*453.59*980.665;//lbm*(g/lbm)8(cm/s^2)
+//c)
+Fnewt=3*(1/2.2046)*9.80665;//(lbm*(kg/lbm)*(m/s^2))
+mprintf("the force in lb is %f lb force ",Fl)
+mprintf("the force in dynes is %f dyn ",Fdyne)
+mprintf("the force in Newtons is %f N ",Fnewt)
+//end
diff --git a/2762/CH2/EX2.2.2/2_2_2.sce b/2762/CH2/EX2.2.2/2_2_2.sce
new file mode 100755
index 000000000..c20cb5885
--- /dev/null
+++ b/2762/CH2/EX2.2.2/2_2_2.sce
@@ -0,0 +1,24 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.2-2
+//Principles of Momentum Transfer and Overall Balances
+//given data
+//P(total pressure)=h(height of the column)*rho(density of fluid)*g(gravity force)+P(absolute pressure)
+h1=10 ;//ht of oil layer in ft
+rhooil=917;//density of oil in kg/m3
+g=9.8;//gravity force in m/s2
+Patmsi=1.01325*10^5;//atm pressure in si units
+Patm=14.696;//lbf/in2
+Ptot1=h1*(rhooil*62.43/1000)*1*(1/144)+Patm;//ft*(lbm/ft3)*(1/(in2/ft2));
+Ptot1si=(h1*0.3048)*rhooil*g+Patmsi;//total pressure of oil in si units
+h2=2;//ht in ft
+rhowater=1000;//density of water in kg/m3
+Ptot2=h2*(rhowater*62.43/1000)*1*(1/144)+Ptot1;//ft*(lbm/ft3)*(1/(in2/ft2))
+Ptot2si=(h2*0.3048)*rhowater*g+Ptot1si;//total pressure of water in si units
+Pgage=Ptot2-Patm
+mprintf("the pressure on oil layer is %f psia",Ptot1)
+mprintf("the pressure on oil layer is %f pa",Ptot1si)
+mprintf("the pressure on bottom layer is %f psia",Ptot2)
+mprintf("the pressure on oil layer is %f pa",Ptot2si)
+mprintf("the gage pressure %f psia",Pgage)
+//end
diff --git a/2762/CH2/EX2.2.3/2_2_3.sce b/2762/CH2/EX2.2.3/2_2_3.sce
new file mode 100755
index 000000000..8e1f055c3
--- /dev/null
+++ b/2762/CH2/EX2.2.3/2_2_3.sce
@@ -0,0 +1,15 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.2-3
+//Principles of Momentum Transfer and Overall Balances
+//given data
+//a) si units
+rhow=1000;
+g=9.80665;
+P=101325;
+hw=P/(rhow*g);//water head 
+mprintf("a) head= %f m of water 4 deg C",hw)
+//b) for Hg
+rhom=13595.5;
+hm=(rhow/rhom)*hw;
+mprintf(" b) head= %f m of Mercury",hm)
diff --git a/2762/CH2/EX2.2.4/2_2_4.sce b/2762/CH2/EX2.2.4/2_2_4.sce
new file mode 100755
index 000000000..1f8acf7a6
--- /dev/null
+++ b/2762/CH2/EX2.2.4/2_2_4.sce
@@ -0,0 +1,12 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.2-4
+//Principles of Momentum Transfer and Overall Balances
+//given data: 
+R=32.7;//manometer reading in cm
+rhom=13.6;//density of mercury in g/cc
+rhow=1;//density of water in g/cc
+g=9.81//gravity force in m/s2
+Pdiff=(R/100)*(rhom-rhow)*1000*g;//Pressure diff in N/m2
+mprintf("the pressure diff is %f N/m2",Pdiff)
+//end
diff --git a/2762/CH2/EX2.3.1/2_3_1.sce b/2762/CH2/EX2.3.1/2_3_1.sce
new file mode 100755
index 000000000..5aa486b81
--- /dev/null
+++ b/2762/CH2/EX2.3.1/2_3_1.sce
@@ -0,0 +1,19 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.3-1
+//Principles of Momentum Transfer and Overall Balances
+//given data
+//a)
+del=0.013;//diffusivity
+T1=1.37e-2;//concn at pt1 amt of prop/m3
+T2=0.72e-2;//concn at pt2
+z2=0.4;
+z1=0;
+shi1=(del*(T1-T2))/(z2-z1);
+mprintf("%f amt of property/s m2",shi1)
+//b
+disp('T=T1+(shi1/del)*(z1-z)')
+//c)
+z=0.2;//point where concn is being found
+T=T1+(shi1/del)*(z1-z);//concentration at mid point
+mprintf("%f amt of property/s m3",T)
diff --git a/2762/CH2/EX2.4.1/2_4_1.sce b/2762/CH2/EX2.4.1/2_4_1.sce
new file mode 100755
index 000000000..74c3e2129
--- /dev/null
+++ b/2762/CH2/EX2.4.1/2_4_1.sce
@@ -0,0 +1,24 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.4-1
+//Principles of Momentum Transfer and Overall Balances
+//given data
+dely=0.5;//dist between 2 plates in cm
+delv=10;//vel diff along z in cm/s
+mu=0.0177//viscosity in CP
+//a) after integrating shear stress(tao)= mu*(delv)/dely
+tao=mu*(delv/dely);//g/(s2*cm)
+//shear rate= delv/dely as the vel change is linear with y
+SR=delv/dely;
+mprintf("shear stress in cgs = %f dyn/cm2",tao)
+mprintf(" shear rate in cgs = %f s-1",SR)
+//b) in lb force
+mulb=mu*(6.7197/100);//viscosity changes to lbm/(ft*s)
+taolb=(mulb*delv)/(dely*32.174);//lbf/ft2
+mprintf(" shear stress in english units = %f lbf/ft2",taolb)
+mprintf(" shear rate in english units = %f s-1",SR)
+//c)
+taosi=(mu*0.1*delv)/(dely);
+mprintf(" shear stress in si = %f N/m2",taosi)
+mprintf(" shear rate in si = %f s-1",SR)
+//end
diff --git a/2762/CH2/EX2.5.1/2_5_1.sce b/2762/CH2/EX2.5.1/2_5_1.sce
new file mode 100755
index 000000000..3d3b3a4fe
--- /dev/null
+++ b/2762/CH2/EX2.5.1/2_5_1.sce
@@ -0,0 +1,21 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.5-1
+//Principles of Momentum Transfer and Overall Balances
+//given data
+f=10*(1/7.481)*(1/60);//flow rate(ft3/s)=10(gal/min)*(1ft3/7.481 gal)(1min/60s)
+D=2.067/12;//diameter in ft
+A=(3.14*D*D)/4;//cross sectional area in ft2
+v=f/A;//velocity in ft/s
+rhoeng=0.996*62.43;//lbm/ft3
+mueng=0.8007*6.7197/10000;//viscosity in lbm/ft*s
+Nreeng= (D*v*rhoeng)/(mueng);//reynolds number in english units
+//in SI units
+rhosi=0.996*1000;//density in kg/m3
+Dsi=2.067*1/3.2808;//in*(ft/12in)*(m/ft)
+vsi=v*(1/3.2808)*(1/12);//velocity in m/s
+musi=0.8007/1000;//viscosity in SI units
+Nresi=(Dsi*rhosi*vsi)/musi;
+mprintf("the reynolds number in si units is %f",Nresi)
+mprintf("the reynolds number in english units is %f",Nreeng)
+//end
diff --git a/2762/CH2/EX2.6.1/2_6_1.sce b/2762/CH2/EX2.6.1/2_6_1.sce
new file mode 100755
index 000000000..49b62ebbd
--- /dev/null
+++ b/2762/CH2/EX2.6.1/2_6_1.sce
@@ -0,0 +1,20 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.6-1
+//Principles of Momentum Transfer and Overall Balances
+//given data
+//oil density=892 kg/m3 , volumetric flow rate= (1.388*10^-3) m3/s, schedule 40 pipes are being used
+//a) 
+A1=0.02330*0.0929;//cross sectional area in m2
+A3=0.01414*0.0929;//cross sectional area in m2
+rho=892;//oil density=892 kg/m3
+m1=(1.388/1000)*rho;//mass flow rate in kg/s in pipes 1 and 2
+m3=m1/2;//mas flow rate divides eqully in 3 pipes
+v1=m1/(rho*A1);//velocity at 1 pipe'
+v3=m3/(rho*A3);//
+G1=(v1)*rho;
+mprintf("a) the total mass flow rate in pipe 1 is %f kg/s",m1)
+mprintf(" b) the velocity in pipe 1 is %f m/s",v1)
+mprintf(" the velocity in pipe 3 is %f m/s",v3)
+mprintf(" c) the mass velocity in pipe 1 is %f kg/s m2",G1)
+//end
diff --git a/2762/CH2/EX2.7.1/2_7_1.sce b/2762/CH2/EX2.7.1/2_7_1.sce
new file mode 100755
index 000000000..80c44fd45
--- /dev/null
+++ b/2762/CH2/EX2.7.1/2_7_1.sce
@@ -0,0 +1,22 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.7-1
+//Principles of Momentum Transfer and Overall Balances
+//given data
+//Q=(z2-z1)*g+(v2^2-v1^2)/2 + (H2-H1)
+//for KE terms
+v1=1.52;//velociy of inlet stream
+v2=9.14;//velocity of exit stream
+KE=((v1^2)-(v2^2))/2;
+//for PE terms 
+z1=0 ,// (z2-z1)*g
+z2=15.2;//ht of exit stream
+g=9.80665;// g force
+PE=(z2-z1)*g;
+//enthalpy change
+H2=2771.4*1000;//exit ,enthalpy data from appendix
+H1=76.97*1000;//inlet enthalpy
+H=H2-H1;
+Q=KE+PE+H;
+mprintf("the amount of heat to be added %f J/kg",Q)
+//end
diff --git a/2762/CH2/EX2.7.2/2_7_2.sce b/2762/CH2/EX2.7.2/2_7_2.sce
new file mode 100755
index 000000000..1a3ade16b
--- /dev/null
+++ b/2762/CH2/EX2.7.2/2_7_2.sce
@@ -0,0 +1,22 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.7-2
+//Principles of Momentum Transfer and Overall Balances
+//given data
+m=0.567;//inlet vol flow rate 
+rho1=968.5;//density of fluid
+m1=m*rho1/60;// mass flow rate in kg/s
+m2=m1;//steady state
+E1=7.45*1000;//energy supplied by the pump in J/s
+Ws=-E1/m1;//work done by shaft
+E2=-1408*1000;//energy given up in J/s
+Q=E2/m2;
+g=9.80665;
+z2=20;
+z1=0;
+//H2-H1+(z2-z1)g+(del v^2)/2= Ws+Q
+H1=355.9*1000;//enthalpy from tables
+H2=Q-Ws-(z2-z1)*g+H1;
+mprintf("the enthalpy is %f J/kg",H2)
+mprintf(" the temp as ssen from steam tables is 48.41 deg C")
+//end
diff --git a/2762/CH2/EX2.7.3/2_7_3.sce b/2762/CH2/EX2.7.3/2_7_3.sce
new file mode 100755
index 000000000..aa17d2ca3
--- /dev/null
+++ b/2762/CH2/EX2.7.3/2_7_3.sce
@@ -0,0 +1,13 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.7-2
+//Principles of Momentum Transfer and Overall Balances
+//given data
+//si units
+KE=0;PE=0;Ws=0;//steady state
+Power=19.63*1000;
+m1=0.3964/60;//mass flow rate in si units
+Q=Power/m1;//heat added
+H1=0;
+H2=H1+Q;//exit enthalpy
+mprintf("exit enthalpy= %f kJ/kg",H2/1000)
diff --git a/2762/CH2/EX2.7.4/2_7_4.sce b/2762/CH2/EX2.7.4/2_7_4.sce
new file mode 100755
index 000000000..a3b74406e
--- /dev/null
+++ b/2762/CH2/EX2.7.4/2_7_4.sce
@@ -0,0 +1,16 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.7-4
+//Principles of Momentum Transfer and Overall Balances
+//given data
+Ws=-155.4;
+z1=0;
+z2=3.05;
+g=9.806;
+PE=(z1-z2)*g;
+KE=0;//const dia pipe'
+rho=998;
+p1=68.9*1000;
+p2=137.8*1000;
+sumF=-Ws+PE+KE+(p1-p2)/rho
+mprintf("frictional loss= %f J/kg",sumF)
diff --git a/2762/CH2/EX2.7.5/2_7_5.sce b/2762/CH2/EX2.7.5/2_7_5.sce
new file mode 100755
index 000000000..ea4cf47e0
--- /dev/null
+++ b/2762/CH2/EX2.7.5/2_7_5.sce
@@ -0,0 +1,32 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.7-5
+//Principles of Momentum Transfer and Overall Balances
+//given data
+//cgs units
+V=69.1;//volumetric flow rate in gallon/min
+fr1=V*(1/60)*(1/7.481);//converting flow rate in ft3/s
+A1=0.0233;//cross section area in ft2 of the pipe
+v2=fr1/A1;//vel in ft/s
+v1=0;//since the tank is very large
+p1=1;//atm pressure
+p2=p1;
+gc=32.174;
+z1=0;//datum
+g=32.174;
+z2=50;//length of discharge line in ft
+rho=114.8;//density of liq soln
+F1=10;//friction loss in ft-lb force/lb mass
+Ws=(z1*(g/gc))-(z2*(g/gc))+(v1*v1/(2*gc))-(v2*v2/(2*gc))+((p1-p2)/rho)-F1;//shaft work calculated by mechanical energy equation
+n=0.65;//efficiency
+Wp=(-Ws/n);
+m=fr1*rho;//mass flow rate in lbm/s
+P=m*Wp*(1/550);//pump horsepower
+A2=0.05134;//area of cross section
+v3=fr1/A2;
+v4=v2;
+F2=0;//friction losses in the second pipe is negligible
+Pdbyrho=(v3*v3/(2*gc))-(v4*v4/(2*gc))-Ws-F2;
+Pdiff=Pdbyrho*(rho/144);//pressure diff in lb force/in2
+mprintf("pressure developed by pump = %f psia",Pdiff)
+mprintf(" pump horsepower= %f hp",P)
diff --git a/2762/CH2/EX2.8.2/2_8_2.sce b/2762/CH2/EX2.8.2/2_8_2.sce
new file mode 100755
index 000000000..845bbc69f
--- /dev/null
+++ b/2762/CH2/EX2.8.2/2_8_2.sce
@@ -0,0 +1,21 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.8-2
+//Principles of Momentum Transfer and Overall Balances
+//given data
+V=0.03154;//vol flow rate in si units
+D1=0.0635;// upstream ID
+A1=(%pi/4)*D1*D1;//area of cross section
+D2=0.0286;// downstream ID
+A2=(%pi/4)*D2*D2;//area of cross section
+rho=1000;//density of water
+m=V*rho;//mass flow rate of water upstream
+m1=m;
+m2=m;
+v1=V/A1;//vel at pt 1
+v2=V/A2;//vel at pt 2
+p2=0;//gage pressure
+p1=(((v2*v2/2)-(v1*v1/2))+(p2/rho))*rho;
+//for x direction the momentum balance equation is used
+Rx=m*(v2-v1)-A1*p1;
+mprintf("the resultant force towards the negative x direction is %f N",-Rx)
diff --git a/2762/CH2/EX2.8.5/2_8_5.sce b/2762/CH2/EX2.8.5/2_8_5.sce
new file mode 100755
index 000000000..976265c45
--- /dev/null
+++ b/2762/CH2/EX2.8.5/2_8_5.sce
@@ -0,0 +1,17 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.8-5
+//Principles of Momentum Transfer and Overall Balances
+//given data
+v1=30.5;
+D1=2.54/100;
+alpha2=60;
+rho=1000;
+A1=(%pi*D1*D1)/4;
+m=v1*A1*rho;
+Rx=m*v1*(cos(%pi/3)-1);
+Ry=m*v1*sin(%pi/3);
+mprintf("the force on x direction =%f N",-Rx)
+mprintf("the force on y direction =%f N",-Ry)
+R=sqrt(Rx*Rx+Ry*Ry);
+mprintf("the resultant force =%f N",-R)
diff --git a/2762/CH2/EX2.9.1/2_9_1.sce b/2762/CH2/EX2.9.1/2_9_1.sce
new file mode 100755
index 000000000..818b38206
--- /dev/null
+++ b/2762/CH2/EX2.9.1/2_9_1.sce
@@ -0,0 +1,16 @@
+//Transport Processes and Seperation Process Principles
+//Chapter 2
+//Example 2.9-1
+//Principles of Momentum Transfer and Overall Balances
+//given data
+rho=820;//density in kg/m3
+del=1.7/1000;//film thikness in m
+g=9.806;//g force
+mu=0.2;//viscocity in Pa.s
+T=(rho^2)*(del^3)*g/(3*mu);//T= mass flow rate per unit width of wall
+Re=(4*T)/mu;//Reynolds Number
+v=(rho*g*(del^2))/(3*mu);//avg velocity
+mprintf("mass flow rate per unit width of wall= %f kg/(s.m)",T)
+mprintf(" Reynolds Number= %f",Re)
+mprintf(" avg velocity= %f m/s",v)
+//end