Oxidative degradation of an amine is a two-step process involving the dissolution of O2 from the flue gas into the solvent, followed by a liquid phase reaction between the dissolved O2 and the amine. The observed amine degradation rate is thus a function of O2 solubility, mass transfer resistances, and kinetic reaction parameters. Process parameters, such as temperature, O2 partial pressure, amine concentration, and CO2 loading, influence each of these mechanisms. A detailed review of oxidative degradation methods is available in Braakhuis et al. . Braakhuis et al. define two categories of oxidative degradation: direct and indirect. Direct oxidative degradation occurs within the absorber where the solvent is in direct contact with the flue gas, and the quantity of dissolved oxygen is replaced while consumed. The magnitude of this effect is a function of the rate of mass transfer of O2 from the gas phase to the liquid phase and is expected to vary depending on the location within the absorber as the bulk temperature and the solvent loading change. Indirect degradation happens downstream of the absorber, where no further contact with an oxygen-rich flue gas occurs; in this case, the degree of oxidative degradation is limited to the quantity of dissolved oxygen in the solvent when no longer in contact with the flue gas. This can be mitigated with process modifications that reduce the quantity of dissolved O2 that is carried over to the absorber sump, for example, flashing or N2 sparging of rich solvent. The process considerations proposed by Mullen et al. for 100% added CO2 capture might be expected to adversely affect the degree of MEA degradation within post-combustion CO2 capture plants. Higher reboiler temperatures will obviously increase the degree of thermal degradation, all other things being equal. However, the associated reduced loading (i.e., carbamate concentration) in the reboiler may somewhat mitigate this. Concurrently, a reduced average loading in the absorber may increase the solubility of O2 overall and lead to increased oxidative degradation. Additional packing, the inclusion or absence of intercooling, and liquid-to-gas ratios will also all contribute to the uncertainty surrounding MEA degradation rates at 100% added CO2 capture fractions. This work applies the oxidative (Braakhuis and Knuutila ) and thermal degradation (Braakhuis et al. ) models for an MEA solvent with process modelling completed by Mullen et al. to compare the specific quantity of MEA degradation for three industrial flue gas sources (CCGT, EfW and SMR processes) at two distinct CO2 capture fractions (95% gross CO2 capture & 100% added CO2 capture), with the inclusion or not of intercooling serving as a third variable. For the first time, we quantify the expected additional solvent degradation rate when operating at a 100% added CO2 capture fraction, facilitating an assessment of the resulting impact on process economics. It is important to note that the operational conditions proposed for 100% added CO2 capture operation would also provide a reduced energy penalty for lower CO2 capture fraction operation should the resulting solvent degradation rates be deemed economically acceptable. Likewise, if solvent degradation is more critical to a project than thermal efficiency, lean loadings sufficient to achieve high CO2 capture fractions can be achieved at lower temperature regeneration conditions. This work aims to compare the solvent degradation rates at proposed design points for the considered CO2 capture fractions that the authors consider to be valid and viable, acknowledging that such design points are project-specific and do not represent an absolute economic optimum, as no such point can exist except for specific project conditions.