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In order to understand the effect of various operational and kinetic parameters on the final crystal size coming out of the crystallizer, a mathematical model was developed to mimic the operation of the industrial unit.
Assuming the inner structure of the nucleus as identical to that of the final crystal, the gain in free energy upon crystallization reads − μ⋅ N with μ being the change in free energy per solute.
Three linear cooling profiles (10 °C, 20 °C and 30 °C/h) were applied for both unseeded and seeded crystallization and the effect of the seeding temperature on the final crystal size distribution was systematically investigated.
It was found that the nozzle size as well as particle collecting method both had great impact on the final crystal forms.
This contact secondary mechanism is assumed to be the dominant nucleation mechanism as it generates about two-thirds of the final crystal number.
The objective is to minimize the standard deviation of the final crystal size distribution (CSD), which is an important feature in many industrial processes.
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Blebbistatin was added to the crystallization because it improved the quality of the final crystals.
SPT concentration and CSD were monitored as functions of time, and the final crystals visualized by SEM micrography.
The indirect objectives were minimization of the batch time and maximizing the final crystals size and they were closely related to the meeting of the direct objectives.
The shape of the final crystals was laminary, and the crystals attained their maximum size (0.1×0.1×0.02 mm) after 10 d.
The final crystals were grown by the hanging-drop vapor diffusion method at room temperature.
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