CONDENSATE FOR
DESUPERHEATING
Steam from
Utility plant
P = 41 kg/cm2a
T = 334 0C
H = 3052KJ/kg
Condensate
control valve
P = 25 kg/cm2a
T = 110 0C
H = 460 KJ/kg
m = 4500 kg/hr
25
Let Down valve
P = 18 kg/cm2a
T = 309.5 0C
H = 3052KJ/kg
18 kg/cm2a =
Energy balance for steam loop:
Enthalpy of condensate + Enthalpy of Steam from U
Steam to Plant A
4500*460 + 3052*x = 2847*4500 +2847*10000
Solving gives, x=12847 kg/hr
Steam from Utility = 12847kg/hr
Mass balance for steam loop:
Mass of condensate + Mass of Steam from Utility =
4500 + x = 4500 +10000
Solving gives, x=10000 kg/hr
Mass of condensate + Mass of Steam from Utility =
4500 + x = 4500 +10000
Solving gives, x=10000 kg/hr
Steam from Utility = 10000 kg/hr
kg/cm2a =
24.5166 barA
This simple flow diagram is all wrong! You are not depi
As a consequence, your calculations are WRONG. You
paste text boxes containing the data for calculations. T
that does the correct and accurate calculations for you
DO THE CALCULATIONS!
Use your common sense. You cannot mix the condensa
I believe you have your condensate properties all wron
condensate (at 25 kg/cm2A) down to to 18 kg/cm2A. Y
110 oC & 25
kg/cm2A. Look at the Thermo Properties
P = 18 kg/cm2a
T = 225 0C
H = 2847 KJ/kg
m = 10000 kg/hr
17.652 barA
P = 18 kg/cm a
T = 225 0C
H = 2847 KJ/kg
m = 4500 kg/hr
2
Plant B
P = 18.2 kg/cm2a
T = 208 0C
HSteam = 2796 KJ/kg
HWater = 2796 KJ/kg
m = 8000 kg/hr
Steam from Utility = Enthalpy of Steam to Plant B + Enthalpy
7*10000
rom Utility = Mass of Steam to Plant B + Mass of Steam to Pl
rom Utility = Mass of Steam to Plant B + Mass of Steam to Pl
ng! You are not depicting correctly what you are trying to do.
ns are WRONG. You are using an engineering spreadsheet to
ta for calculations. This is an ignorant way to employ a tool
calculations for you. PUT THE DATA IN CELLS AND LET EXCEL
not mix the condensate at a pressure higher than your steam!
e properties all wrong because you fail to expand your
to to 18 kg/cm2A. You cannot have saturated condensate at
e Thermo Properties on the next Tab.
Plant A
P = 18.2 kg/cm2a
T = 208 0C
HSteam = 2796 KJ/kg
HWater = 2796 KJ/kg
m = 8000 kg/hr
B + Enthalpy of
Steam to Plant A
STEAM
Regenerate
d in Reactor
in Plant A
Steam to Plant A
Source: http://webbook.nist.gov/chemistry/fluid/
Isobaric Properties for Water
Fluid Data
Isobaric Data for P = 17.652 bar
Temperature
Pressure (bar)
(C)
309
309.5
310
17.652
17.652
17.652
Density
(kg/m3)
6.8574
6.8504
6.8435
Volume (m3/kg)
0.14583
0.14598
0.14612
Internal
Energy
(kJ/kg)
2793.8
2794.7
2795.5
Enthalpy
(kJ/kg)
3051.2
3052.4
3053.5
Entropy
(J/g*K)
6.8702
6.8721
6.8741
Saturation Properties for Water Temperature Increments
Liquid Phase Data
Data on Saturation Curve
Temperature
Pressure (bar)
(C)
110
111
112
113
114
115
1.4338
1.4826
1.5328
1.5844
1.6374
1.6918
Density
(kg/m3)
950.95
950.18
949.41
948.64
947.86
947.08
Volume (m3/kg)
0.0010516
0.0010524
0.0010533
0.0010541
0.001055
0.0010559
Internal
Energy
(kJ/kg)
461.26
465.49
469.72
473.95
478.18
482.41
Enthalpy
(kJ/kg)
461.42
465.65
469.88
474.12
478.35
482.59
Entropy
(J/g*K)
1.4188
1.4298
1.4408
1.4518
1.4628
1.4737
Cv (J/g*K)
1.6672
1.6668
1.6665
Cv (J/g*K)
3.7167
3.7116
3.7065
3.7014
3.6963
3.6913
Cp (J/g*K)
2.257
2.2561
2.2552
Cp (J/g*K)
4.2283
4.2297
4.2312
4.2326
4.2341
4.2356
Sound Spd. Joule-Thomson
Therm. Cond.
Viscosity (cP)
(m/s)
(K/bar)
(W/m*K)
577.17
577.46
577.75
1.1712
1.168
1.1647
0.020492 0.047146
0.020514 0.04719
0.020536 0.047235
Phase
vapor
vapor
vapor
Sound Spd. Joule-Thomson
Therm. Cond. Surf. Tension
Viscosity (cP)
(m/s)
(K/bar)
(W/m*K)
(N/m)
1532.9
1531.7
1530.5
1529.3
1528
1526.7
-0.017208
-0.017145
-0.017082
-0.017018
-0.016954
-0.016889
0.2547
0.25225
0.24985
0.24749
0.24517
0.24289
0.68169
0.68189
0.68207
0.68225
0.68241
0.68257
0.056962
0.056765
0.056567
0.056368
0.05617
0.05597
Phase
liquid
liquid
liquid
liquid
liquid
liquid
