Minimal MEA consumption occurs in the cold-rich solvent pipeline to the heat exchanger (both pipework and heat exchangers are modelled as plug flow reactors) due to the low residence time and temperature. Within the heat exchanger, dissolved O2 consumption increases rapidly due to the increased reaction rate stemming from the increased temperatures. By the time the solvent reaches the stripper column, O2 is predicted to have been entirely consumed in all cases, as also seen in previous work . Minimal O2 in the export CO2 stream is a crucial CO2 pipeline specification due to downstream pipeline integrity concerns. As a result, deoxygenation systems are often included in the design downstream of the stripper at considerable capital expenditure. That being the case, confirmation of total O2 consumption in the solvent prior to the stripper through pilot or operational studies may allow the omission or reduction in the capacity of the deoxygenation system, leading to a reduction in capital and operational expenditure for systems using aqueous MEA as solvent. This may not be the case for an alternativesolvents with greater resistance to oxidative degradation.