The present invention relates to a technique for flow crystallization. The system comprises a container having a bottom surface defining a first plane, the container including at least two planar magnetic surfaces being arranged in a spaced-apart manner along a first plane and being substantially parallel to a second plane; a magnetization vector of each of the magnetic surfaces being perpendicularly to the surface, wherein the container is configured such that the first plane is substantially perpendicularly to the second plane; wherein a cavity formed in between the planar magnetic surfaces is configured to accommodate a racemic mixture including different enantiomers such that each magnetic surface interacts differently with each of the different enantiomers to thereby enable enantio-selective crystallization. Therefore, the system of the present invention is based on enantio-separation of the crystals using magnetic surfaces.

The present disclosure relates to a method for continuous preparation of high bulk density methionine crystals. The process of the method is as follows: a hydrolysate solution, which is obtained from a reaction of 5-(?-methylmercaptoethyl) hydantoin and a potassium carbonate solution, is mixed with an external circulation material from a DTB neutralization crystallizer having a gas phase neutralization section; after being cooled, the mixture enters a liquid distributor of a neutralization region in the upper part of the crystallizer and is sprayed in the form of liquid droplet or trickle into carbon dioxide gas for neutralization reaction, and then naturally falls into a crystallization region in the lower part to be mixed with a material in the region; the obtained mixture grows on fine crystals in a system to form crystals having larger particle diameters, and meanwhile new crystal nucleuses are formed; in a deposition area in the middle part of the crystallization region, the crystals having larger particle diameters deposits into an elutriation leg, while the fine crystals circulate with the external circulation material, and a part of the external circulation material is used to elutriate the crystals in the elutriation leg, while another part of the same is used to be mixed with the hydrolysate solution; and the crystals in the elutriation leg are separated, washed and dried to obtain the high bulk density methionine product.

The process described below is a method of making tinctures starting with extraction of a full spectrum oil from a biomass, then activating the cannabinoids in the full spectrum oil, finally formulating tinctures using the activated full spectrum oil.

Optional additional steps of winterization, distillation, and isolation increase the purity of the resulting product.

A method for producing high purity D-psicose crystals having a purity of 98% (w/w) or more and a grain size of MA200 or more. The method includes: removing impurities from a D-psicose solution to obtain a purified D-psicose solution; concentrating the purified D-psicose solution; cooling the concentrated D-psicose solution to 30 C. to 40 C. through a heat exchanger; seed crystallizing the D-psicose solution at 30 C. to 40 C. to obtain a seed crystallized massecuite; and full-scale crystallizing the seed crystallized massecuite. The method can produce pure D-psicose crystals in a suitable form for industrial application through an economical crystallization process from the D-psicose solution without using organic solvents.

A desalinating system and method is disclosed. The desalination system comprises using a turbo freeze or fast-cooling process to freeze saline water droplets and separate salt crystals from pure water crystals, wherein said system provides for simultaneous injection of saline water droplets and a chilled refrigerant into a freezing chamber at a slip velocity sufficient to reduce the size of the saline water droplets to an optimal diameter.

A system is provided for performing crystallisation by cooling, comprising two crystallisation units, each of the two crystallisation units comprising a cooling body with a crystallisation surface for forming crystals on, and a scraper unit, comprising a scraping member arranged to be moved over the crystallisation surface for scraping crystals from the crystallisation surface and a scraper actuator for moving the scraping member over the crystallisation surface, wherein the scraper actuator of a first of the two crystallisation units can be actuated independently from a scraper actuator of a second of the two crystallisation units.

Stable liquid formulations dominant in cannabidiol (CBD) can be manufactured by a sequential process of purification to create a formulation that does not crystallize under a variety of storage and use conditions, and without the use of potentially harmful additives. For example, the formulation may be used in vaporization devices (i.e., electronic cigarettes) that typically require formulations to remain in a non-crystalline, non-solid, or non-partially solid state. The liquid formulations dominant in CBD may further contain other phytocannabinoids, including, but not limited to, tetrahydrocannabinol (THC), cannabigerol (CBG), cannabichromene (CBC), cannabinol (CBN), and cannabidivarin (CBDV) in higher concentrations than unrefined and refined cannabis extracts obtained via existing methods.

A system for generating a concentrated product from a feedstock includes a reciprocating concentration system that includes first and second chambers to which the feedstock is alternately provided and from which the concentrated product is alternately removed, and a heat transfer system in thermal communication with the first and second chambers, the heat transfer system being configured to reversibly transfer heat between the first and second chambers such that the first chamber alternates between melting a frozen portion of the feedstock in the second chamber and having a frozen portion of the feedstock in the first chamber melted by the feedstock in the second chamber. The system further includes a heat dump system in thermal communication with the reciprocating concentration system, the heat dump system being configured to remove heat from the reciprocating concentration system.

A heat storage apparatus according to the present disclosure includes a heat storage material and a member. The heat storage material forms a clathrate hydrate by cooling. The member has a surface with a plurality of holes. In the case that the lattice constant of the clathrate hydrate is denoted by L and the outside diameter of a cage included in the clathrate hydrate is denoted by D, the plurality of holes are spaced at intervals of 1L to 10L, and each of the plurality of holes has a hole diameter of 1D to 20D.

Digestion of impure alumina with sulfuric acid dissolves all constituents except silica. The resulting sulfatesaluminum sulfate, ferric sulfate, titanyl sulfate, and magnesium sulfate for alumina contaminated with iron-, titanium-, and/or magnesium-containing speciesremain in solution at approximately 90 C. Hot filtration separates silica. Solution flow over metallic iron reduces ferric sulfate to ferrous sulfate. Controlled ammonia addition promotes hydrolysis and precipitation of hydrated titania from titanyl sulfate that is removed by filtration. Addition of ammonium sulfate forms ferrous ammonium sulfate and ammonium aluminum sulfate solutions. Alum is preferentially separated by crystallization. Addition of ammonium bicarbonate to an ammonium alum solution precipitates ammonium aluminum carbonate which may be heated to produce alumina, ammonia, and carbon dioxide. The remaining iron rich liquor also contains magnesium sulfate. The addition of oxalic acid generates insoluble ferrous oxalate which is thermally decomposed to ferrous oxide and carbon monoxide which is used to reduce the ferrous oxide to metallic iron. Further oxalic acid addition precipitates magnesium oxalate which is thermally decomposed to magnesium oxide.