Methods for recovering lignins are described that include simultaneous acidification and solvation of lignin. A single step process is described that includes combining a lignin-containing feed with a solvent solution that includes both an organic solvent and a strong acid. Upon formation and heating of the resulting mixture, lignin in the feed can be acidified from the salt form to the acid form in conjunction with solvation of the acidified lignin through the creation of both a liquified lignin-rich liquid phase and a solvent-rich liquid phase in a liquid/liquid equilibrium (LLE).

Sample purification systems include a particle extraction assembly having a mixing compartment and a settling compartment. A biological sample is mixed with two liquid phases formulated to effectuate transfer of a biological molecule into a first phase and particulate contaminants into a second phase. The first phase includes a solubilizing salt, the second phase includes an organic molecule, and the mixture can have little or no monoatomic salt or dextran. The molecule-containing first phase can be optionally concentrated without also concentrating the particulate contaminants and introduced into a multi-stage liquid-liquid extractor, by which the biological molecule or molecular contaminants are extracted from the first phase into a third phase, thereby purifying the molecule away from contaminants. The extracted sample can be further purified through a series of processing steps. The system can be run in continuously mode to maintain sterility of the sample.

Provided is a method for purifying organic acids, including: a first extraction which includes separating an aqueous solution of organic acids into a first organic layer and a first aqueous solution layer by adding a solvent containing an amine and an alcohol; removing the alcohol from the separated first organic layer; and a second extraction which includes separating the first organic layer from which the alcohol has been removed into a second organic layer and a second aqueous solution layer by adding water.

The interaction system includes: an interaction unit internally including a process flow path that allows a first fluid and a second fluid to flow through the process flow path so as to come into contact and interact with each other; a separation container connected to an outlet of the process flow path so as to receive a mixed fluid of the first fluid and the second fluid discharged from the outlet of the process flow path to retain the received mixed fluid to separate the mixed fluid into the first fluid and the second fluid; a first fluid supply device configured to supply the first fluid to an inlet of the process flow path; a second fluid path connecting a region, where the separated second fluid is accumulated, of the separation container and the inlet of the process flow path so as to guide the second fluid separated in the separation container to the inlet of the process flow path; and a second fluid feed pump provided on the second fluid path to send the second fluid separated in the separation container from the separation container to the inlet of the process flow path.

A washing and desalting device includes a first shell and a plurality of filaments. The first shell has a first receiving cavity and is provided with a liquid inlet and a liquid outlet that communicate with the first receiving cavity. The plurality of the filaments is provided in the first receiving cavity, and the length direction of each of the filaments is consistent with that of the first receiving cavity. The device can be incorporated in a washing and dehydrating system.

A method and system for performing biomolecule extraction are provided that use liquid-to-liquid extraction (LLE) in combination with an electrowetting on dielectric (EWOD) device to provide a biomolecule extraction solution that has high extraction efficiency and that is less costly and easier to use than current state of the art methods and systems. The system and method are well suited for, but not limited to, extraction of DNA, RNA and protein molecules.

A method of making CBD concentrate or CBD Isolate comprises (a) milling a raw material; (b) contacting the milled raw material with an extraction solvent and separating a solid waste material to form a filtered extract; (c) concentrating the filtered extract; (d) washing the concentrated extract to form an organic phase and an aqueous phase; (e) separating the aqueous phase from the organic phase to form a washed extract; (f) removing an organic solvent from the washed extract to form a concentrated washed extract; (g) decarboxylating the concentrated washed extract; (h) vacuum distilling the decarboxylated extract to form a distillate; (i) dewaxing the distillate to form a post-dewax filtrate; (j) applying a vacuum to the post-dewax filtrate to form a post-dewax concentrate; (k) degassing the post-dewax concentrate; and (l) vacuum distilling the degassed concentrate to form a CBD concentrate.

The present application provides a method for extracting an extractable component from a feed liquid using a porous membrane. One embodiment of the method includes temperature-swing solvent extraction of water from saline water using a porous membrane.

The methods described herein produce a naphthenic process oil, as classified by ASTM D-2226, containing 35-65% saturates and 35-65% aromatics as determined by ASTM D-2007. The produced naphthenic process oil also contains polyaromatic hydrocarbons (PAH), more specifically the EU/US EPA 8-regulated PAHs, less than 10 ppm. The naphthenic process oil is produced by first feeding gas oil ranging in viscosities up to 20 cSt at 100° C. through counter-current liquid-liquid extraction towers with a solvent having a selective affinity for aromatics. The extract is then cooled and either continuously processed through a coalescing separator or batch processed in a tank or decanter to produce a second raffinate, which can be further distilled to produce the naphthenic process oil.

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.