For non-electrolytic, low-pressure unit operations (< 10 bar) activity coefficient models were selected to model phase equilibria. At low pressure and low data availability, these models commonly predict phase equilibria involving non-ideal liquids more accurately than equations of state (EOS). Suitability of using activity coefficient models for the relevant operating temperatures was confirmed by calculating the reduced temperature 𝑇𝑟 using Kay's rule (eq. 1), which did not exceed 0.75 for all modelled process steps. At 𝑇𝑟>0.75 liquids expand rapidly, and the accuracy of activity coefficient models -designed to model characteristic liquid phase interactions -would reduce. The NRTL activity coefficient model was chosen for simulations as it is capable of modelling VLE and LLE, and has been found to outperform UNIQUAC and Wilson for VLE modelling of most mixtures relevant to this study, especially aqueous organics. To estimate the NRTL binary interaction parameters α and τ of component pairs for which the Aspen Plus V10 databases did not hold regressed model coefficients, α was set to the recommended documentation value (0.2 for LLE systems; 0.3 for non-associative, slightly non-ideal liquid mixtures of non-polar and polar compounds), 60 and τ was regressed by Aspen Plus's property constant estimation system (PCES) using binary infinite-dilution activity coefficients estimated from the UNIFAC or UNIFAC-LL group contribution method. For component pairs where PCES-derived parameters yielded unreasonable LLE simulations, α and τ were instead estimated from proxy data, as shown in SI Section S2.2.