During the early design stage of an industrial process, system-specific separation data is sometimes only available for dead-end batch filtration, due to equipment availability and practicality. Thus, the separation performance of the scaled-up system in continuous crossflow mode may need to be estimated based on separation characteristics determined from a small-scale batch set-up. To model the performance of a continuous cross-flow separation unit (CCSU) for the isolation of nopinone from methanol-water solvent, a series of hypothetical dead-end batch separation units (DBSU) were considered (Figure ). In this model, the permeate properties of each DBSU were calculated using experimentally determined 𝑅 %&' , the retentate properties were calculated from a mass balance and the required membrane area was found using the measured flux values 𝐽 ! (Figure ). The model workflow is illustrated in Figure , and model equations are given in SI Section S8. The model predicted the removal of ~64 mol% feed solvent and ~2 mol% feed nopinone into the CMSU permeate stream, yielding 𝐶𝐹 ≈ 1.7. This result shows that significant nopinone separation can be attained through energy-efficient membrane technology using the BW30 membrane, which reduces the need for energy intense separation strategies during nopinone purification. The active membrane area requirement was calculated as 𝑎 I`ab = 55.25 m 2 , which is a reasonable order of magnitude, and cross-flow separation units containing comparable BW30 sizes can be purchased commercially. It is acknowledged that the parameters determined in dead-end batch operation cannot accurately represent nopinone separation across BW30 in continuous cross-flow, given the different separation dynamics of the two filtration systems. However, the presented model is proof of principle that highlights the potential of the investigated system for the energy-efficient isolation of nopinone in continuous flow processes.