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-rwxr-xr-x167/CH3/EX3.1/ex1.sce9
-rwxr-xr-x167/CH3/EX3.10/ex10.sce13
-rwxr-xr-x167/CH3/EX3.11/ex11.sce22
-rwxr-xr-x167/CH3/EX3.12/ex12.sce23
-rwxr-xr-x167/CH3/EX3.13/ex13.sce29
-rwxr-xr-x167/CH3/EX3.14/ex14.sce12
-rwxr-xr-x167/CH3/EX3.2/ex2.sce9
-rwxr-xr-x167/CH3/EX3.3/ex3.sce14
-rwxr-xr-x167/CH3/EX3.4/ex4.sce16
-rwxr-xr-x167/CH3/EX3.5/ex5.sce23
-rwxr-xr-x167/CH3/EX3.7/ex7.sce11
-rwxr-xr-x167/CH3/EX3.8/ex8.sce9
12 files changed, 190 insertions, 0 deletions
diff --git a/167/CH3/EX3.1/ex1.sce b/167/CH3/EX3.1/ex1.sce
new file mode 100755
index 000000000..0d3b3ea61
--- /dev/null
+++ b/167/CH3/EX3.1/ex1.sce
@@ -0,0 +1,9 @@
+//ex1
+//Pressure of Saturated Liquid in a Tank
+clc
+Psat=70.183;//saturated pressure @90C using steam table A-4 in kPa
+printf('From steam table Psat @ 90 C = %.3f kPa',Psat);
+vsat=0.001036;//saturated specific volume @90C in m^3/Kg
+m=50;//mass in kg
+V=m*vsat;//Volume of tank in m^3
+printf('\n Total Volume of Tank = %.4f m^3',V);
diff --git a/167/CH3/EX3.10/ex10.sce b/167/CH3/EX3.10/ex10.sce
new file mode 100755
index 000000000..85e05d470
--- /dev/null
+++ b/167/CH3/EX3.10/ex10.sce
@@ -0,0 +1,13 @@
+//ques10
+//Mass of Air in a Room
+clc
+l=4;//length in metres
+b=5;//breadth in metres
+h=6;//height in metres
+V=l*b*h;//volume in m^3
+P=100;//Pressure in kPa
+R=0.287;//Gas constant for a given gas in kPa.m^3/Kg.k
+T=298;//Temp in K
+m=P*V/(R*T);//mass in Kg
+printf('Mass =P*V/(R*T)= %.1f kg',m);
+
diff --git a/167/CH3/EX3.11/ex11.sce b/167/CH3/EX3.11/ex11.sce
new file mode 100755
index 000000000..186fdce72
--- /dev/null
+++ b/167/CH3/EX3.11/ex11.sce
@@ -0,0 +1,22 @@
+//ques11
+//The Use of Generalized Charts
+clear
+clc
+//(a)specific volume using ideal gas equation of state
+R=0.0815;//gas constant for given substance in kPa.m^3/Kg.K
+Pcr=4.059;//Critical Pressure in MPa
+Tcr=374.2;//Critical Temp in K
+T=323;//Temp in K
+P=1000;//Pressure in kPa
+v=R*T/P;//Specific Volume in m^3/Kg
+printf('\n(a) Specific Volume = %.6f m^3/kg ',v);
+er=(v-0.021796)/0.021796;//error
+printf('\n Error = %.3f',er);
+//(b) specific volume using chart
+Pr=P/Pcr;//reduced pressure
+Tr=T/Tcr;//reduced Temperature
+Z=0.84;//from compressibility chart
+Videal=Z*v;//Ideal Volume in m^3/kg
+printf('\n(b) Ideal volume = %.6f m^3/kg ',Videal);
+er=(Videal-0.021796)/0.021796;//error
+printf('\n Error = %.3f',er); \ No newline at end of file
diff --git a/167/CH3/EX3.12/ex12.sce b/167/CH3/EX3.12/ex12.sce
new file mode 100755
index 000000000..fee809129
--- /dev/null
+++ b/167/CH3/EX3.12/ex12.sce
@@ -0,0 +1,23 @@
+//ques12
+//Using Generalized Charts to Determine Pressure
+clc
+//(a)
+R=0.5956;//Gas constant for a given substance in psia.ft^3/lbm.R
+Pcr=3200;//Critical Pressure in psia
+Tcr=1164.8;//Critical Temp in R
+v=0.51431;//specific volume in ft^3/lbm
+T=600;//Temperature in F
+//so
+P=1000;//Pressure in psia from Table A-6E
+printf('\n(a) Pressure at a specified state = %.0f psia',P);
+//(b)
+T=1060;//Temperature in F
+P=R*T/v;//Pressure in psia
+printf('\n(b)Pressure of the steam under specified condition = %.0f psia',P);
+//(c)using generalised compressibility chart
+Vr=v*Pcr/(R*Tcr/Pcr);//reduced volume
+Tr=T/Tcr;//reduced temperature
+//so
+Pr=0.33;//from compressibility chart
+P=Pr*Pcr;//final Pressure in psia
+printf('\n(c) Pressure(using generalised compressibility chart) = %.0f psia ',P);
diff --git a/167/CH3/EX3.13/ex13.sce b/167/CH3/EX3.13/ex13.sce
new file mode 100755
index 000000000..3ae3140f6
--- /dev/null
+++ b/167/CH3/EX3.13/ex13.sce
@@ -0,0 +1,29 @@
+//ex13
+//Different Methods of Evaluating Gas Pressure
+clear
+clc
+T=175//temp in K
+v=0.00375//specific volume in m^3/kg
+//(a)ideal gas equation of state
+// data from table A-1
+R=0.2968//gas constant for a given gas in kPa.m^3/kg.K
+P=R*T/v;//Pressure in kPa
+printf('\n(a) Pressure from Ideal gas equation = %.0f kPa \n',P);
+//(b)van der waals equation
+//a and b are van der waals constant
+a=0.175;//m^6.kPa/Kg^2
+b=0.00138;//m^3/Kg
+P=R*T/(v-b)-a/v^2;//pressure in kPa
+printf('(b) Pressure from van der waals equation = %.0f kPa \n',P);
+//(c)Beattie-Bridgeman equation
+A=102.29//constant
+B=0.05378//constant
+c=4.2*10^4;//constant
+Ru=8.314;//universal gas constant value
+MM=28.013//molecular Mass of substance
+v=0.00375//specific volume in Kg/m^3
+V=MM*v//Volume in m^3
+
+P=Ru*T/V^2*(1-c/(V*T^3))*(V+B)-A/V^2;//pressure in KPa
+printf('(c) Pressure from Beattie-Bridgeman equation = %.0f kPa \n',P);
+
diff --git a/167/CH3/EX3.14/ex14.sce b/167/CH3/EX3.14/ex14.sce
new file mode 100755
index 000000000..c2425a6ea
--- /dev/null
+++ b/167/CH3/EX3.14/ex14.sce
@@ -0,0 +1,12 @@
+//ques14
+//Temperature Drop of a Lake Due to Evaporation
+clear
+clc
+Psat=3.17//saturated pressure in kPa @ 25 C
+Pv1=0.1*Psat//pressure for 10% humidity in kPa
+Pv2=0.8*Psat//pressure for 80% humidity in kPa
+Pv3=1*Psat//pressure for 100% humidity in kPa
+T1=-8.0;//Temp in K
+T2=21.2;//Temp in K
+T3=25;//Temp in K
+printf( 'Corresponding Temperatures(in C) are(From table A-5) \n T1 = %.1f K \n T2 = %.1f K \n T3 = %.1f K ',T1,T2,T3 );
diff --git a/167/CH3/EX3.2/ex2.sce b/167/CH3/EX3.2/ex2.sce
new file mode 100755
index 000000000..0d79e4035
--- /dev/null
+++ b/167/CH3/EX3.2/ex2.sce
@@ -0,0 +1,9 @@
+//ques2
+//Temperature of Saturated Vapor in a Cylinder
+clc
+Tsat=280.99;//Saturated temperature in F @ 50psia from table A-5E
+printf("Saturated Temperature = %.2f F \n",Tsat);
+v=8.5175;//vg saturated volume of vapor in ft^3/lbm table A-5E
+V=2;//Total Volume in ft^3
+m=V/v;//mass in lbm
+printf('Mass of the sample is = %.3f lbm ',m);
diff --git a/167/CH3/EX3.3/ex3.sce b/167/CH3/EX3.3/ex3.sce
new file mode 100755
index 000000000..e19265773
--- /dev/null
+++ b/167/CH3/EX3.3/ex3.sce
@@ -0,0 +1,14 @@
+//ques3
+//Volume and Energy Change during Evaporation
+clc
+vg=1.6941; //saturated vapor specific volume from table A-5 @ 100kPa in m^3/Kg
+vf=0.001043;//saturated liquid specific volume from table A-5 @ 100kPa in m^3/Kg
+vfg=vg-vf;//in m^3/Kg
+m=0.2;//in kg
+//(a) Volume change
+dV=m*vfg;//Volume in m^3
+printf('(a) Volume change = %.4f m^3 \n',dV);
+//(b) Amount of energy Transfer to water
+hfg=2257.5;//change in enthalpy from table A-5 @ 100kPa in kJ/Kg
+E=m*hfg;//In kJ
+printf('(b) Energy Transferred = %.1f kJ',E);
diff --git a/167/CH3/EX3.4/ex4.sce b/167/CH3/EX3.4/ex4.sce
new file mode 100755
index 000000000..1ad0ec3fa
--- /dev/null
+++ b/167/CH3/EX3.4/ex4.sce
@@ -0,0 +1,16 @@
+//ques4
+//Pressure and Volume of a Saturated Mixture
+clc
+//(a) Pressure in the tank
+P=70.183;//Psat @ 90 C table A-4 in kPa
+printf("(a) Pressure in the tank = %.3f kPa ",P);
+//(b)volume of tank
+disp('(b)V = Vf+Vg = mf*vf+mg*vg');
+mf=8;//mass of liquid water in kg
+mg=2//mass of vapor water in kg
+vf=0.001036;//saturated specific volume of liquid water from table A-4 in m^3/Kg
+vg=2.3593;//saturated specific volume of vapor water from Table A-5 in m^3/Kg
+V=mf*vf+mg*vg;//Total Volume in m^3
+printf('Volume of tank = %.2f m^3',V);
+
+
diff --git a/167/CH3/EX3.5/ex5.sce b/167/CH3/EX3.5/ex5.sce
new file mode 100755
index 000000000..e73dccd6c
--- /dev/null
+++ b/167/CH3/EX3.5/ex5.sce
@@ -0,0 +1,23 @@
+//ques5
+//Properties of Saturated Liquid Vapour Mixture
+clc
+V=0.080;//volume in m^3 given
+m=4;//in kg given
+v=V/m;//in m^3/kg
+vf=0.0007437;//@160kPa from table A-4 in m^3/kg
+vg=0.12348;//@160kPa from table A-4 in m^3/kg
+//(a)Temperature
+Tsat=-15.60;//in C from table A-4
+printf('\n(a) Since vf<v<vg so saturated region, so temperature at saturated state = %.2f C \n',Tsat);
+//(b)Quality Factor
+x=(v-vf)/(vg-vf);
+printf('(b) Quality factor =%.3f \n',x);
+//(c) Enthalpy of refrigerant
+hf=31.21//from table A-12 @ 160kpa in kJ/kg
+hfg=209.90//from table A-12 @ 160kpa in kJ/kg
+h=hf+x*hfg;// n kJ/kg
+printf('(c) Enthalpy of refrigerant = %.1f kJ/kg \n',h);
+//(d) Volume occupied by phase
+mg=x*m//mass of vapour n kg
+Vg=mg*vg;//volume of vapour in m^3
+printf('(d) Volume of vapour =%.4f m^3 \n',Vg);
diff --git a/167/CH3/EX3.7/ex7.sce b/167/CH3/EX3.7/ex7.sce
new file mode 100755
index 000000000..452ea37b2
--- /dev/null
+++ b/167/CH3/EX3.7/ex7.sce
@@ -0,0 +1,11 @@
+//ex6
+//Internal Energy of Superheated Vapor using linear interpolation
+clc
+disp('h1=2855.8 @ T1=200 C and h2=2961.0 @ T2=250 C and h=2890 lies in between these two so using linear interpolation we can get Temperature ');
+h1=2855.8;//Enthalpy at T1 in kJ/Kg
+T1=200;//temp in C
+h2=2961.0;//Enthalpy at T2 in kJ/Kg
+T2=250;//Temp T2 in C
+h=2890;//Enthalpy in kJ/kg at which temp is to be determined
+T=(T2-T1)/(h2-h1)*(h-h1)+T1;//Temp for given value of enthalpy in C
+printf('Temperature = %.1f C',T);
diff --git a/167/CH3/EX3.8/ex8.sce b/167/CH3/EX3.8/ex8.sce
new file mode 100755
index 000000000..36415b4d4
--- /dev/null
+++ b/167/CH3/EX3.8/ex8.sce
@@ -0,0 +1,9 @@
+//ques8
+//Approximating Compressed Liquid as Saturated Liquid
+clc
+u1=333.82;//(a) internal energy in KJ/Kg @ P=5MPa and T=80 C from table A-7
+printf("\n(a) Data as from compress liquid table, u= %.2f kJ/kg\n",u1);
+u2=334.97;//(b)internal energy in KJ/Kg @80 C from table A-4
+printf("(b) Data as from saturated liquid table, u = %.2f kJ/kg",u2);
+er=(u2-u1)/u1*100;//(c) %age error
+printf('\n(c)Error involved = %.2f percent',er);
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