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

---
 2873/CH6/EX6.14/Ex6_14.sce   |  68 +++++++++++++++++++++++++++++++++++++++++++
 2873/CH6/EX6.14/Ex6_14_1.jpg | Bin 0 -> 340784 bytes
 2873/CH6/EX6.14/Ex6_14_2.jpg | Bin 0 -> 801655 bytes
 3 files changed, 68 insertions(+)
 create mode 100755 2873/CH6/EX6.14/Ex6_14.sce
 create mode 100755 2873/CH6/EX6.14/Ex6_14_1.jpg
 create mode 100755 2873/CH6/EX6.14/Ex6_14_2.jpg

(limited to '2873/CH6/EX6.14')

diff --git a/2873/CH6/EX6.14/Ex6_14.sce b/2873/CH6/EX6.14/Ex6_14.sce
new file mode 100755
index 000000000..efc3036ea
--- /dev/null
+++ b/2873/CH6/EX6.14/Ex6_14.sce
@@ -0,0 +1,68 @@
+// Display mode
+mode(0);
+// Display warning for floating point exception
+ieee(1);
+clear;
+clc;
+disp("Engineering Thermodynamics by Onkar Singh Chapter 6 Example 14")
+x1=0.5;//dryness fraction 
+m1=100;//mass of steam in kg
+v1=0.8475;//
+disp("it is constant volume process")
+disp("volume of vessel(V)=mass of vapour * specific volume of vapour")
+disp("initial specific volume,v1")
+disp("v1=vf_100Kpa+x1*vfg_100 in m^3/kg")
+disp("at 100 Kpa from steam table;")
+disp("hf_100Kpa=417.46 KJ/kg,uf_100Kpa=417.36 KJ/kg,vf_100Kpa=0.001043 m^3/kg,hfg_100Kpa=2258 KJ/kg,ufg_100Kpa=2088.7 KJ/kg,vg_100Kpa=1.6940 m^3/kg")
+hf_100Kpa=417.46;
+uf_100Kpa=417.36;
+vf_100Kpa=0.001043;
+hfg_100Kpa=2258;
+ufg_100Kpa=2088.7;
+vg_100Kpa=1.6940;
+disp(" here vfg_100Kpa=vg_100Kpa-vf_100Kpa in m^3/kg")
+vfg_100Kpa=vg_100Kpa-vf_100Kpa
+disp("so v1=vf_100Kpa+x1*vfg_100Kpa in m^3/kg")
+v1=vf_100Kpa+x1*vfg_100Kpa
+disp("and volume of vessel(V)=m1*x1*v1 in m^3")
+V=m1*x1*v1
+disp("enthalpy at 1,h1=hf_100Kpa+x1*hfg_100Kpa in KJ/kg")
+h1=hf_100Kpa+x1*hfg_100Kpa
+disp("internal energy in the beginning=U1=m1*u1 in KJ")
+U1=m1*(uf_100Kpa+x1*ufg_100Kpa)
+disp("let the mass of dry steam added be m,final specific volume inside vessel,v2")
+disp("v2=vf_1000Kpa+x2*vfg_1000Kpa")
+disp("at 2000 Kpa,from steam table,")
+disp("vg_2000Kpa=0.09963 m^3/kg,ug_2000Kpa=2600.3 KJ/kg,hg_2000Kpa=2799.5 KJ/kg")
+vg_2000Kpa=0.09963;
+ug_2000Kpa=2600.3;
+hg_2000Kpa=2799.5;
+disp("total mass inside vessel=mass of steam at2000 Kpa+mass of mixture at 100 Kpa")
+disp("V/v2=V/vg_2000Kpa+V/v1")
+disp("so v2=1/((1/vg_2000Kpa)+(1/v1))in m^3/kg")
+v2=1/((1/vg_2000Kpa)+(1/v1))
+disp("here v2=vf_1000Kpa+x2*vfg_1000Kpa in m^3/kg")
+disp("at 1000 Kpa from steam table,")
+disp("hf_1000Kpa=762.81 KJ/kg,hfg_1000Kpa=2015.3 KJ/kg,vf_1000Kpa=0.001127 m^3/kg,vg_1000Kpa=0.19444 m^3/kg")
+hf_1000Kpa=762.81;
+hfg_1000Kpa=2015.3;
+vf_1000Kpa=0.001127;
+vg_1000Kpa=0.19444;
+disp("here vfg_1000Kpa=vg_1000Kpa-vf_1000Kpa in m^3/kg")
+vfg_1000Kpa=vg_1000Kpa-vf_1000Kpa
+disp("so x2=(v2-vf_1000Kpa)/vfg_1000Kpa")
+x2=(v2-vf_1000Kpa)/vfg_1000Kpa
+disp("for adiabatic mixing,(100+m)*h2=100*h1+m*hg_2000Kpa")
+disp("so mass of dry steam at 2000 Kpa to be added(m)in kg")
+disp("m=(100*(h1-h2))/(h2-hg_2000Kpa)")
+m=(100*(h1-(hf_1000Kpa+x2*hfg_1000Kpa)))/((hf_1000Kpa+x2*hfg_1000Kpa)-hg_2000Kpa)
+disp("quality of final mixture=x2")
+x2
+
+
+
+
+
+
+
+
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-- 
cgit