Embodiments of the disclosure produce a method and system for deasphalting a hydrocarbon feed. The hydrocarbon feed and a first solvent is combined using a Taylor-Couette mixer to form a mixed stream. The mixed stream and a second solvent are introduced to an extractor to produce a first deasphalted oil stream and a pitch stream. The first deasphalted oil stream is introduced to a solvent recovery unit to recover the first solvent and the second solvent via a recovered solvent stream and to produce a second deasphalted oil stream.

An initial introduction control part introduces an aqueous solution containing molybdenum 99 and technetium 99m, and an organic solvent being capable of dissolving the technetium 99m into an extraction tank. A micro-mixing control part micro-mixes the aqueous solution and the organic solvent by heating and stirring a mixed solution of the aqueous solution and the organic solvent introduced into the extraction tank with a heater, while applying ultrasonic to the mixed solution. A separation control part separates the mixed solution micro-mixed into two phases of aqueous solution and an organic solvent. A taking-out introduction control part passes the organic solvent separated into two phases through an adsorption column be capable of adsorbing molybdenum 99 and introduces the organic solvent into an evaporation elution tank. An evaporation control part evaporates the organic solvent and leaves residue by reducing pressure inside the evaporation elution tank and heating the organic solvent introduced into the evaporation elution tank with a heater, while applying ultrasonic to the organic solvent. An elution control part introduces physiological saline solution into the residue and elutes technetium 99m into the physiological saline solution from the residue.

The invention concerns a method for purifying a hydroalcoholic feedstock, comprising: a) a step of counter-current liquid-liquid extraction, comprising an extraction section supplied at the top with said hydroalcoholic feedstock and at least one intermediate raffinate fraction from step b) and at the bottom with an extraction solvent, and producing at the top an extraction stream and at the bottom a raffinate, wherein the extraction section is operated at a mean temperature in the extractor of between 10 and 40° C.; b) a counter-current liquid-liquid back-extraction comprising a back-extraction section supplied at the top with an acidic aqueous solution, having a pH between 0.5 and 5.0, and at the bottom with the extraction stream from step a), and producing at the top an extract and at the bottom the intermediate raffinate, wherein the back-extraction section is operated at a mean temperature between 40 and 80° C.

There is a process for the selective recovery of transition metals from an organic stream containing transition metals. The organic stream and possibly a first extractor if solid, are melted up to the liquid state. The extractor consists of an ionic liquid or a mixture of two or more ionic liquids and the ionic liquid contains an ammonium salt as cation and as anion an anion with chelating properties. A melted organic stream and a first extractor, optionally melted, are fed to a first liquid-liquid extraction unit working at a temperature of at least 150° C. where the liquid-liquid extraction is carried out obtaining a liquid mixture containing an ionic liquid, or a mixture of two or more ionic liquids, and metals. After extraction, the liquid mixture is cooled at a temperature between 0° C. and 70° C. and becomes biphasic; then the cooled mixture is sent to a first separation unit, to separate a liquid phase that contains ionic liquids and metals, and a metal-depleted solid phase. After the first separation, the separated metal-depleted solid phase is optionally sent to a washing unit to which a solvent is fed, so as to eliminate the residual ionic liquid by transferring it into the solvent and obtaining a metal-depleted solid phase. Then the separate liquid phase containing ionic liquids and metals is sent into a liquid-liquid precipitation and separation unit, adding a counter-solvent, thereby obtaining a solid phase containing the metals and a liquid stream containing counter-solvent and ionic liquids.

Single-stage and multi-stage systems and methods for the recovery of critical elements in substantially pure form from lithium ion batteries are provided. The systems and methods include supported membrane solvent extraction using an immobilized organic phase within the pores of permeable hollow fibers. The permeable hollow fibers are contacted by a feed solution on one side, and a strip solution on another side, to provide the simultaneous extraction and stripping of elements from dissolved lithium ion cathode materials, while rejecting other elements from the feed solution. The single- and multi-stage systems and methods can selectively recover cobalt, manganese, nickel, lithium, aluminum and other elements from spent battery cathodes and are not limited by equilibrium constraints as compared to traditional solvent extraction processes.

A method for purification and extraction of cannabinoids includes: providing a cannabis oil including phospholipids and cannabinoid acids; contacting the cannabis oil with a degumming solvent, wherein the degumming solvent and cannabis oil are substantially immiscible; and separating an aqueous phase including the degumming solvent and at least a portion of the phospholipids from an oil phase including the cannabis oil. The method may further include contacting the oil phase with an extraction solvent, where the extraction solvent and oil phase are substantially immiscible; and separating an aqueous phase including the extraction solvent and at least a portion of the cannabinoid acids from a second oil solvent phase including the oil phase and/or simply the liberated cannabinoids following acidification of the extraction solvent.

An initial introduction control part introduces an aqueous solution containing molybdenum 99 and technetium 99m, and an organic solvent being capable of dissolving the technetium 99m into an extraction tank. A micro-mixing control part micro-mixes the aqueous solution and the organic solvent by heating and stirring a mixed solution of the aqueous solution and the organic solvent introduced into the extraction tank with a heater, while applying ultrasonic to the mixed solution. A separation control part separates the mixed solution micro-mixed into two phases of aqueous solution and an organic solvent. A taking-out introduction control part passes the organic solvent separated into two phases through an adsorption column be capable of adsorbing molybdenum 99 and introduces the organic solvent into an evaporation elution tank. An evaporation control part evaporates the organic solvent and leaves residue by reducing pressure inside the evaporation elution tank and heating the organic solvent introduced into the evaporation elution tank with a heater, while applying ultrasonic to the organic solvent. An elution control part introduces physiological saline solution into the residue and elutes technetium 99m into the physiological saline solution from the residue.

The present invention belongs to the technical field of petrochemical engineering, and relates to a method for continuous post-treatment of benzotriazole (abbreviated as BTA) synthetic fluid. In particular, the present invention relates to a method for synthesizing BTA, including subjecting the BTA synthetic fluid to post-treatment steps of continuous acidification, water washing, extraction, back-extraction, dehydration, and distillation and the like. The method utilizes the difference in solubility of the BTA in water under different pHs to achieve separation by extraction without consuming a large amount of evaporation energy. The present invention is easy to operate, has little environmental pollution, high economic efficiency and low energy consumption, and is easily industrialized.

A method of inhibiting degradation of an extractant by utilizing several auxiliary means in the DSX process: includes (a) preparing adjustment of the concentration of an extractant of a DSX solvent to a certain range; (b) extracting a metal contained in a pregnant leached solution by adjusting the ratio of the extractant and the diluent in the DSX solvent to a certain range; (c) measuring the pH of the aqueous phase solution by separating mixture into the aqueous phase solution and the organic phase solvent using a settler after step of extracting; (d) controlling the pH by adding soda ash (Na.sub.2CO.sub.3) so as to maintain the pH of the aqueous phase solution to be 3 to 7; and (e) scrubbing with scrubbing solution having a zinc concentration of 2 to 20 g/L by zinc sulfate (ZnSO.sub.4) to remove the manganese from the organic phase solvent containing the extracted metal.

Provided is a method of inhibiting degradation of an extractant by an anhydrous environment avoiding and metal stripping, the method including the steps of: (a) stopping the addition of soda ash (Na.sub.2CO.sub.3) to an extracting reaction tank; (b) starting solution recirculation and stopping solvent recirculation of a settler; (c) supplying a solvent from a loaded organic tank to a scrubbing reaction tank, in which the scrubbing reaction tank, stripping reaction tank and extracting reaction tank are connected for circulation and operating stirrers of the scrubbing reaction tank, stripping reaction tank and extracting reaction tank; (d) supplying a sulfuric acid solution having a controlled concentration with a diluting solution to the stripping reaction tank; (e) transferring the solvents of the settler, the loaded organic tank and all the pipes to the scrubbing reaction tank; and (f) stopping the step (e) and initiating solvent recirculation.