Internal diameter of tower (calculated) = 3.7 ft
Call it 4 ft. = 12.6 sq. ft. cross-sectional area.
The actual tray design will be done by others (tray manufacturer) to protect the
guarantee requirements.
Calculate the Amine Holdup in the Bottom of the Tower
The minimum liquid holdup will be 1 min from NLL to empty.
The volume of amine in 1 min ¼
3,117
60 ¼ 51:95 cuft
Then NLL will be ¼
51:95
12:6 ¼ 4:1 ft say 4 ft
Then HLL will be set at 8 f. and LLL at 4 f. above tangent.
Add a further 4 f. from HLL to bottom tray.
The Overall Dimensions of the Contactor
The height of the contactor is as follows:
From bottom tangent line:
To bottom tray
¼ 12 ft
To top absorbing tray ¼ 45 ft
To wash water drawoff ¼ 48 ft bottom of chimney tray
ð
Þ
To top of wash section ¼ 54 ft
To top tangent
¼ 58 ft
Overall dimensions for the contactor are 4 f. ID Â 58 f. Tan-Tan.
Calculating the Heat Balance over the Contactor
The rich gas flow will enter at 100
F and 320 psig and will have an enthalpy of
350 Btu/lb. Its flow rate is 34,722 lb/h.
The heat of reaction is calculated at 650 Btu/lb of H 2 S absorbed.
The lean amine solution enters at a temperature of 105
F which will be set by
heat transfer. The lean product gas will leave at about the same temperature.
The rich amine leaving the contactor is determined by difference
Temperature of rich amine out ¼
23:602 Â 10
6
38,949 Â 0:663
ð
Þ þ 155,798
¼ 129:95 say 130
F
The Heat Exchanger Design
The hot lean amine stream to the contactor will be cooled from the stripper bottom
temperature first by heat exchange against the rich amine leaving the contactor. It
will then be trim cooled to the contactor inlet temperature by either water or air. The
following is the calculation to determine the size of the lean/rich amine exchanger.
518
D.S.J. Jones and S.A. Treese
Call it 4 ft. = 12.6 sq. ft. cross-sectional area.
The actual tray design will be done by others (tray manufacturer) to protect the
guarantee requirements.
Calculate the Amine Holdup in the Bottom of the Tower
The minimum liquid holdup will be 1 min from NLL to empty.
The volume of amine in 1 min ¼
3,117
60 ¼ 51:95 cuft
Then NLL will be ¼
51:95
12:6 ¼ 4:1 ft say 4 ft
Then HLL will be set at 8 f. and LLL at 4 f. above tangent.
Add a further 4 f. from HLL to bottom tray.
The Overall Dimensions of the Contactor
The height of the contactor is as follows:
From bottom tangent line:
To bottom tray
¼ 12 ft
To top absorbing tray ¼ 45 ft
To wash water drawoff ¼ 48 ft bottom of chimney tray
ð
Þ
To top of wash section ¼ 54 ft
To top tangent
¼ 58 ft
Overall dimensions for the contactor are 4 f. ID Â 58 f. Tan-Tan.
Calculating the Heat Balance over the Contactor
The rich gas flow will enter at 100
F and 320 psig and will have an enthalpy of
350 Btu/lb. Its flow rate is 34,722 lb/h.
The heat of reaction is calculated at 650 Btu/lb of H 2 S absorbed.
The lean amine solution enters at a temperature of 105
F which will be set by
heat transfer. The lean product gas will leave at about the same temperature.
The rich amine leaving the contactor is determined by difference
Temperature of rich amine out ¼
23:602 Â 10
6
38,949 Â 0:663
ð
Þ þ 155,798
¼ 129:95 say 130
F
The Heat Exchanger Design
The hot lean amine stream to the contactor will be cooled from the stripper bottom
temperature first by heat exchange against the rich amine leaving the contactor. It
will then be trim cooled to the contactor inlet temperature by either water or air. The
following is the calculation to determine the size of the lean/rich amine exchanger.
518
D.S.J. Jones and S.A. Treese