The new operating point P3 is listed in Table . Heat losses in the reboiler, that were determined in another work by Ränger et al. , are considered in the simulation. A reduced reboiler duty of 2.02 kW in the simulation run compared to the experimental value of 3 kW reflects these heat losses of the real column. The listed vapor split ratios are obtainable in both simulation and experiment. In contrast to the preceding experiments, the mass flows of the product streams D, S1, and S2 are controlled by PID controllers instead of manually adjusting the shaking funnels. In the simulation model, the mole fraction of butanone for denaturation is added to the mole fraction of ethanol, as butanone is only present in very small amounts and has a boiling point close to the one of ethanol. is tested in an experimental start-up process and applied to the simulation model, taking as many real effects and differences between simulation and experiment as possible into account.