Vapor/Liquid on Bottom Tray
The bottom tray will have a temperature of 240
F (see Fig. 5 and Table 10). In the
following heat balance, let the lb/h of the stripout vapors to the tray be x:
x ¼ 25,748 lb=h Mole wt
¼ 23:08
Mol=h
¼ 1,115:6
V=Lat bottom tray ¼ 1,115:6=10, 457
¼ 0:107
To Calculate the Number of Theoretical Trays in the Stripper
The Kremser equation which is shown graphically in Fig. 6 will be used for this
calculation.
The V/L factor calculated above will be used for this equation. A tower average
K value for each component in the feed will also be used. The calculation is shown
in Table 11.
steam
V + L
L
V
Bot Tray
Lean Amine (1)
Fig. 5 Tower bottom heat balance loop
Table 10 Bottom tray condition calculation
Stream
V or L
F
lb/h
Btu/lb
MMBtu/h
In
Bot prod
L
240
196,482
224
44.012
Stripout
L
240
x
224
224x
Reboiler
22.049
Total in
196,482 + x
66.061 + 224x
Out
Stripout
V
249
x
1,035
1,035x
Bottoms
L
249
196,482
230
45.179
Total out
196,482 + x
45.179 + 1,035x
524
D.S.J. Jones and S.A. Treese