The present disclosure provides a system for extracting long chain dicarboxylic acid, the system comprising: a primary membrane filtration unit, a first crystallization unit, a first separation unit, a first dissolution tank, a secondary membrane filtration unit, a second separation unit, a second crystallization unit and a third separation unit. By the system for extracting long chain dicarboxylic acid of an embodiment of the present invention, the resulted long chain dicarboxylic acid product has a high purity, very low and even no residual alkane residue, and organic solvent-free.

A process and system for the precipitation of poly(phenylene ether) is described. Precipitated poly(phenylene ether) obtained by the processes disclosed herein are in the form of poly(phenylene ether) particles having a bulk density of 150 to 500 kg/m.sup.3, preferably 250 to 500 kg/m.sup.3.

The present invention discloses a mangosteen pericarp extract and process for its preparation thereof. The mangosteen pericarp extract containing α-mangostin and γ-mangostin which obtains from preparation steps comprising fragmentation, organic solvent soaking, aqueous solution, or acidic solution soaking, concentration, spray drying and grinding steps from the rind of the mangosteen. The present invention has advantages of simple preparation process to address efficiency issue, no need to have heating under reflux in extraction steps and the solvents which used are friendly to human body and environment.

The disclosure relates to a microfluidic system for the screening of polymorphs, morphology, and crystallization kinetics under well-mixed, continuous-flow at controlled supersaturations. The disclosure also relates to a method for screening crystalline polymorphs and morphology, and crystallization kinetics. The microfluidic system includes a microfluidic chamber having one or more inlets, a passive mixing zone, and a trap zone. The passive mixing zone promotes mixing of solvent, solute, and optionally antisolvent under stable, controlled levels of supersaturation. The trap zone similarly has stable, controlled levels of supersaturation and correspondingly low velocity to retain solute crystals formed in the trap zone for time-dependent evaluation.

Described is a method for extracting lithium from salt lake brine and simultaneously preparing aluminum hydroxide. This method includes a. adding an aluminum salt to the brine, adding an alkali solution, then subjecting to crystallization reaction and solid-liquid separation to obtain lithium-containing brine; b. evaporating and concentrating the lithium-containing brine, adding an aluminum salt, adding an alkali solution dropwise to perform a co-precipitation reaction and solid-liquid separation to obtain a lithium-containing layered material filter cake, wherein in steps a and b, the alkali solution is an alkali solution free of carbonate ion; c. dispersing the lithium-containing layered material filter cake in deionized water to form a suspension slurry, then adjusting the pH value of the suspension slurry so as to carry out a lithium deintercalation reaction; d. filtering to obtain aluminum hydroxide filter cake; e. washing the aluminum hydroxide filter cake with deionized water and drying.

A method for isolating a lithium precursor according to an embodiment of the present disclosure includes preparing a preliminary precursor mixture including a preliminary lithium precursor and a preliminary transition metal precursor, mixing the preliminary precursor mixture and a precipitation liquid in a reactor to form a precursor mixture, and injecting a non-reactive gas into the precursor mixture. Accordingly, the lithium precursor can be isolated with high yield and high efficiency.

Disclosed are methods for separating, recovering, and purifying cannabidiolic acid (CBDA) salts from an organic solvent solution comprising a mixture of cannabinoids. The methods comprise solubilizing the mixture of cannabinoids in C5-C7 hydrocarbon solvents, adding thereto a selected amine to thereby precipitate a CBDA-amine salt therefrom, dissolving the recovered CBDA-amine salt in a selected solvent and then adding thereto a selected antisolvent to thereby recrystallizing a purified CBDA-amine salt therefrom. The recrystallized CBDA-amine salt may be decarboxylated to form a mixture of cannabidiol (CBD) and amine. The CBD amine mixture may be acidified to separate the amine from CBD. The recovered CBD may be concentrated to produce a highly purified CBD. Also disclosed are CBDA-amine salts produced with certain amines selected from groups of secondary amines, tertiary amines, diamines, amino alcohols, amino ethers, and highly basic amines.

Disclosed herein is a method for producing crystalline cannabinoid particles in continuous mode. The method comprises preparing a cannabinoid-rich solution that comprises a first cannabinoid, and inducing the cannabinoid-rich solution to a supersaturated state in which the first cannabinoid has a supersaturated concentration that is greater than a corresponding saturation concentration of the first cannabinoid. The method further comprises flowing the cannabinoid-rich solution through a tubular reactor in a continuous manner under turbulent flow conditions to form a plurality of crystalline cannabinoid particles and a cannabinoid-depleted solution within the tubular reactor, and separating crystalline cannabinoid particles from the plurality of crystalline cannabinoid particles and the cannabinoid-depleted solution. The turbulent flow conditions are defined by a Reynold number that is greater than a critical Reynolds number for the cannabinoid-rich solution and the tubular reactor.

Disclosed herein is a method for continuously preparing crystalline cannabinoid particles. The method includes preparing a cannabinoid-rich solution that comprises a first cannabinoid and inducing the cannabinoid-rich solution to a supersaturated state in which the first cannabinoid has a supersaturated concentration that is greater than a corresponding saturation concentration of the first cannabinoid. The method includes flowing the cannabinoid-rich solution into a continuous stirred-tank reactor (CSTR) in a continuous manner, mixing the cannabinoid-rich solution under turbulent mixing conditions to form a plurality of crystalline cannabinoid particles and a cannabinoid-depleted solution within the CSTR, and discharging the plurality of crystalline cannabinoid particles and the cannabinoid-depleted solution from the CSTR in a continuous manner to provide a flow rate through the CSTR. The method includes separating crystalline cannabinoid particles from the plurality of crystalline cannabinoid particles and the cannabinoid-depleted solution in a continuous manner.

A saline feed stream flows into a liquid-liquid extraction system; and a volatile organic solvent flows through a main compressor. The compressed volatile organic solvent then flows through a solvent regenerator, which can be a heat exchanger or a combination of a vaporization device and a condenser, to cool the volatile organic solvent. The cooled volatile organic solvent in liquid phase then flows into the liquid-liquid extraction system, where the saline feed stream contacts the volatile organic solvent to selectively extract water from the saline feed stream into the volatile organic solvent, producing a concentrated brine and an organic-rich mixture of water and the volatile organic solvent. The organic-rich mixture flows from the liquid-liquid extraction system into the solvent regenerator, where the organic-rich mixture is heated to produce an organic-rich vapor and desalinated water; and the organic-rich vapor is recycled as volatile organic solvent back into the liquid-liquid extraction system.