Then actual cubic feet per second ACFS
ð
Þ ¼
30 Â 10
6
 14:7  580
24 Â 3,600 Â 520 Â 335
¼ 16:41 cfs
Feed gas in lb/h is 34,722 = 9.645 lb/s.
ρ v ¼
9:645
16:41
¼ 0:5881b=cuft
lb/h of MEA solution is 194,747.
gals/h is 23,317.
And cubic ft/h is 3,117.
Then lb/cuft = 62.48 and at 120
F (MEA inlet temperature) = 62.1 lb/cuft.
Loading at flood: K f √ ρ v  ρ 1 À ρ v
ð
Þ
f
g
K f is 1,280 from Fig. 3 and, inserting a 60 % foam factor, K f = 768.
Loading ¼ 768 Â √36:17 ¼ 4, 619lb=h sq: ft:
Let design load be 70 % of flood = 3,233 lb/h∙sq. ft.
Cross À sectional area of tray and towerI=D
ð
Þ ¼
34, 722
3, 233
¼ 10:74 sq: ft:
15
20
Tray Spacing ins.
25
30
35
10
100
300
500
700
900
‘K’ Factor
1100
Sieve & Valve tray Food Line.
Sieve & Valve tray Design
Bubble Cap trays (Max)
1300
Fig. 3 The Brown and Souders flood constant
Refinery Gas Treating Processes
517
ð
Þ ¼
30 Â 10
6
 14:7  580
24 Â 3,600 Â 520 Â 335
¼ 16:41 cfs
Feed gas in lb/h is 34,722 = 9.645 lb/s.
ρ v ¼
9:645
16:41
¼ 0:5881b=cuft
lb/h of MEA solution is 194,747.
gals/h is 23,317.
And cubic ft/h is 3,117.
Then lb/cuft = 62.48 and at 120
F (MEA inlet temperature) = 62.1 lb/cuft.
Loading at flood: K f √ ρ v  ρ 1 À ρ v
ð
Þ
f
g
K f is 1,280 from Fig. 3 and, inserting a 60 % foam factor, K f = 768.
Loading ¼ 768 Â √36:17 ¼ 4, 619lb=h sq: ft:
Let design load be 70 % of flood = 3,233 lb/h∙sq. ft.
Cross À sectional area of tray and towerI=D
ð
Þ ¼
34, 722
3, 233
¼ 10:74 sq: ft:
15
20
Tray Spacing ins.
25
30
35
10
100
300
500
700
900
‘K’ Factor
1100
Sieve & Valve tray Food Line.
Sieve & Valve tray Design
Bubble Cap trays (Max)
1300
Fig. 3 The Brown and Souders flood constant
Refinery Gas Treating Processes
517