Editing Crystallization (section)

===Evaporative crystallization===
Another option is to obtain, at an approximately constant temperature, the precipitation of the crystals by increasing the solute concentration above the solubility threshold. To obtain this, the solute/solvent mass ratio is increased using the technique of [[evaporation]]. This process is insensitive to change in temperature (as long as hydration state remains unchanged).

All considerations on control of crystallization parameters are the same as for the cooling models.

====Evaporative crystallizers====
Most industrial crystallizers are of the evaporative type, such as the very large [[sodium chloride]] and [[sucrose]] units, whose production accounts for more than 50% of the total world production of crystals. The most common type is the ''forced circulation'' (FC) model (see [[evaporator]]). A pumping device (a [[pump]] or an axial flow [[axial flow pump|mixer]]) keeps the crystal [[slurry]] in homogeneous [[Suspension (chemistry)|suspension]] throughout the tank, including the exchange surfaces; by controlling pump [[Fluid dynamics|flow]], control of the contact time of the crystal mass with the supersaturated solution is achieved, together with reasonable velocities at the exchange surfaces. The Oslo, mentioned above, is a refining of the evaporative forced circulation crystallizer, now equipped with a large crystals settling zone to increase the retention time (usually low in the FC) and to roughly separate heavy slurry zones from clear liquid. Evaporative crystallizers tend to yield larger average crystal size and narrows the crystal size distribution curve.<ref>{{Cite news|url=http://thermalkinetics.net/evaporation-equipment/submerge-circulating-crystallizer|title=Submerge Circulating Crystallizers |newspaper=Thermal Kinetics Engineering, PLLC|language=en-US|access-date=2017-01-03}}</ref>