Page 158 - Gas Purification 5E

146 Gas Puripcation

Table 2-22
Operating Data from Amine Guard 111 MEA C& Removal Test Unit
in an Ammonia Plant

Constant conditions
Absorber Pressure, psig 395
Number of Trays 30
Stripper Pressure, psig at bottom 12
Number of trays (solution feed to top tray) 17
Reboiler heat input, Btdb mole C02 -60,000
Reboiler pressure, psig 12
Stripper top pressure, psig 8
Feed Gas, 8 C02 17.8
Product Gas, ppmv CO, 100
Test Number
Test Variables 1 2 3
Solution
MEA concentration, %I 43.6 35 42.4
Lean solution flow rate, gpm 2,750 2,750 2,550
Lean solution temp.,"F 120 112 110
Lean solution loading, moldmole - 0.15 0.15
Rich solution temp., "F 215 206 222
Rich solution loading, moldmole - 0.47 0.44
Feed Gas Temp.,"F 212 227 216
Stripper Conditions
Inlet solution temp.,"F 237 235 237
Reboiler temp.,"F 247 244 244
Stripper overhead temp.,"F 207 207 206
Ammonia Production
Short tondstream day 1,100 1,110 1,125

Additional data on the operation of aqueous MEA plants, including one with a split flow
cycle, are given by Estep et al. (1962). Operating data on Glycol-Amine plants, which
employ a mixture containing MEA and DEG, are not included here because the process is
considered obsolete; however, such data are included in previous editions of this book and
are available in the literature (Kohl and Blohm, 1950).

Diethanolamine is frequently used for purifying refinery gas streams because of its resis-
tance to COS, which reacts nonregenerably with MEA. In refinery operations, the purified
gas is often used for fuel within the refinery, so a high degree of purity is not required. Typi-