Separation of Enantiomers by Preferential Crystallization: Mathematical Modeling of a Coupled Crystallizer Configuration

A mathematical model describing the separation of enantiomers by simultaneous preferential crystallization in a coupled crystallizer configuration is developed. The model was validated against experimental data for a chemical model compound, the conglomerate forming system of asparagine monohydrate in water. The kinetic parameters required were taken from available literature sources and simulations compared to experimental data. Simulations were found to be in good agreement with experimental data. Additional model simulations suggest that the separation process can be improved by increasing the mean residence time of the liquid phase in the crystallizers, and the mass of seeds supplied. Reducing the size of seed crystals will also lead to an improved separation. The model can also be used to simulate the performance of the crystallization process for a racemic compound forming system. The racemic compound and the pure enantiomer can be separated simultaneously in each crystallizer, having sufficient enrichment of the pure enantiomer in the feed solution. The model can also be extended to represent a fully continuous separation process taking into account the continuous supply of enantiopure seed crystals and liquid feed solution and the continuous removal of solid product and mother liquor

Separation of Enantiomers by Continuous Preferential Crystallization: Experimental Realization Using a Coupled Crystallizer Configuration

The experimental realization of a continuous preferential crystallization process, consisting of two mixed-flow crystallizers coupled via crystal-free liquid exchange streams and with only the liquid phases operating continuously, is addressed. Experiments in triplicate, using the conglomerate-forming system of dl-asparagine monohydrate in water, were conducted, and the achievement of nearly racemic composition of the liquid phase in the crystallizers was verified. An experiment was also carried out using seed crystals of a smaller average particle size than used in the reference experiments. Successful enantioseparation by crystal growth, with the repeatability being within ±10% deviation, was obtained. However, slow crystal growth, due to a low surface integration rate, led to a negligible consumption of the desired enantiomer added in the feed solution, resulting in low productivities. Productivities, yields, and purities of solid products were influenced by the morphological differences in the seed crystals. Due to irregularly shaped seed crystals, increase in the productivities and yields were achieved in the L-Tank. Lower purities of solid products from the L-Tank compared to purities of the solid products from the D-Tank were obtained. This could be due to surface nucleation of d-asparagine monohydrate, ascribed to the surface structure of the seeds of l-asparagine monohydrate supplied. Improvements in productivity, yield, and purity in the L-Tank, for the same process duration, were realized using seed crystals of lower average particle size having a smoother surface structure. The main advantages compared to other separation processes are low capital cost, high crystal purity and yield, ease of upscaling, increased safety, and reduced environmental impact due to reduction in the amount of solvent used. The application is currently limited to conglomerate-forming systems, but the separation concept may open new possibilities for process improvements regarding enantioseparation of racemic compound-forming systems as well