This article presents, for the first time, an assessment of monoethanolamine (MEA) degradation rates when capturing 100% of the added CO2 produced as part of three distinct energy production processes fitted with a post-combustion CO2 capture (PCC) process utilising a 35% wt. MEA solvent. The three processes considered, a combined cycle gas turbine (CCGT), energy from the waste facility (EfW) and a steam methane reformer (SMR), cover the expected range of O2 (1.2 -11.0 % vol) and CO2 concentrations (4.7 -19.5 % vol) within industrial flue gases likely to be relevant in PCC applications. Thus, the MEA degradation rates presented can form a likely range for PCC systems using an MEA solvent within the bounds of the study limitations highlighted throughout. Flue gas conditions are extracted from the previously published works of Mullen et al. and Su et al. and form the input to the process model of the CO2 capture plant, which uses an open-source model developed by the Carbon Capture Simulation for Industry Impact (CCSI) in ASPEN PLUS . For each process, two distinct CO2 capture fractions are considered: 95% gross CO2 capture, which forms the basis for comparison and a CO2 capture fraction resulting in the capture of 100% of the added CO2 produced by the process (99.2, 99.6 & 99.7% for the CCGT, EfW and SMR respectively). The process modifications used to achieve 100% added CO2 capture have previously been described by Mullen et al. and involve the reduction of the solvent lean loading from the typical value of circa 0.2 mol/mol to circa 0.1 mol/mol and, in the case of the CCGT, 4m of additional packing within the absorber column. Mullen et al. have shown that the additional specific thermodynamic penalty of operating at 100% added CO2 capture is minimal if these process modifications are implemented and conclude that to operate efficiently at the reduced lean solvent loading, an increase in stripper operational pressure is required to suppress the production of surplus steam within the regeneration system and minimise energy losses. This increase in operating pressure necessitates an increase in regeneration temperature within the reboiler, a process modification that the authors suggest may increase the thermal degradation of the solvent. Concurrently, a reduced average loading in the absorber may increase the solubility of O2 overall and, coupled with increased residence time due to the increased packing height, may lead to increased oxidative degradation. This study applies thermal and oxidative degradation models developed by Braakhuis et al. to investigate how these process modifications affect the predicted MEA degradation rates compared to operational conditions, which achieve a gross 95% CO2 capture fraction. Additionally, we investigate the effect absorber intercooling, sump O2 dissolution and residence times rates have on total degradation. Initially, we show that for an MEA solvent, oxidative degradation primarily occurs within the absorber packing and that, while the solubility of O2 into the solvent and the partial pressure of O2 in the flue gas will affect total oxidative degradation rates, the effect is dampened by the low order of reaction relative to O2 concentration. In the absence of intercooling, higher CO2 concentrations in the flue gas will tend to lead to higher temperatures in the absorber, as more energy is released by the exothermic reaction between MEA and CO2 per unit of flue gas processed. As the oxidative degradation reaction is strongly influenced by temperature, the increase in flue gas temperature present in low O2/high CO2 concentration flue gases appears to, at least partially, offset the effect of decreased dissolved O2 concentrations. We find that, for the conditions analysed in this work and for equivalent intercooling regimes, oxidative degradation rates within the absorber packing are approximately equal over the three processes analysed, as decreased dissolved O2 concentrations are offset by increased temperatures. The inclusion of intercooling consistently reduces total oxidative degradation rates as the bulk temperature within the absorber is reduced, and the reaction rate is proportionately reduced. This effect is predicted to result in a 30-70% reduction in oxidative degradation within the absorber packing. This indicates that, regardless of CO2 capture fraction or loading, intercooling can be an effective measure for reducing solvent degradation rates. This must, however, be considered in conjunction with the increased CAPEX and operational complexity of including intercooling plus possibly a slight reduction in rich loading. Notably, a 43% increase in oxidative degradation in the absorber packing is seen when comparing the 100% added capture and 95% gross capture CCGT cases at 0.1 mol/mol lean loading (both without intercooling). This is the result of a compounded effect of increased temperatures in the absorber at the higher CO2 capture fraction and the 20m to 24m increase in absorber packing height, increasing residence times. But comparable degradation rates can be seen between the same 95% case and the 100% added capture case when intercooling is included. This novel conclusion indicates that intercooling may be a particularly potent mechanism for reducing solvent degradation in CCGTs at high CO2 capture fractions.