The total power consumed by the fermentation systems was minimized numerically by varying the flow rate of air provided by the compressor and the power consumed by the agitators under the constraint that the oxygen uptake rate is equal to the oxygen transfer rate at a dissolved oxygen concentration of 50% saturation. The power consumed by the agitator was 0.06 kW•m -3 under the baseline fermentation performance, which is sensible compared to the heuristic value recommended for industrial homogeneous reactions (0.3 kW•m -3 ). The overall mass transfer coefficient, kLa (lumped together with the specific interfacial area), was estimated using Van't Riet's non-viscous mass transfer correlation. The design procedure accounts for the pressure gradient across the vessel due to the liquid head using the log-mean driving force for mass transfer. The uncertainty analysis considers a range of titers, productivities, and product yields from the baseline performance on hydrolysate (13.2 g•L -1 titer, 0.17 g•L -1 •h -1 productivity, 0.132 g•g -1 yield) to an optimistic batch performance achieved on pure glucose substrate (27.4 g•L -1 titer, 0.31 g•L -1 •h -1 productivity, 0.18 g•g -1 yield) . Multi-effect evaporation of the juice and hydrolysate is used to achieve the required titer in each scenario. At the lower and upper ends of performance, Yb does not change significantly (0.39 and 0.42 g•g -1 , respectively). To achieve a continuous design space, we assumed this parameter has an average value of 0.405 g•g -1 .