In a method for recovering active metals of a lithium secondary battery according to an embodiment, a cathode active material mixture is collected from the cathode of the lithium secondary battery, the cathode active material mixture is reduced by a reducing reaction to prepare a preliminary precursor mixture, an aqueous lithium precursor solution is formed from the preliminary precursor mixture, and an aluminum-containing material is removed from the aqueous lithium precursor solution with an aluminum removing resin.

An aqueous modified acid composition for industrial activities, said composition comprising: an alkanolamine and strong acid in a molar ratio of not less than 1:15, preferably not less than 1:10; it can also further comprise a metal iodide or iodate. Said composition demonstrates advantages over known conventional acids and modified acids.

An aqueous modified acid composition for industrial activities, said composition comprising: an alkanolamine and strong acid in a molar ratio of not less than 1:15, preferably not less than 1:10; it can also further comprise a metal iodide or iodate. Said composition demonstrates advantages over known conventional acids and modified acids.

The invention relates to a compressed salt block comprising a longitudinally extending elongated body having a vertical longitudinal axis, a top horizontal face, a bottom horizontal face. The block portion has a rectangular cross-section taken in a horizontal plane that is perpendicular to the vertical longitudinal axis, wherein the rectangular cross-section is defined by a major front exterior surface that is a base surface of the block portion, a major rear surface, and a pair of exterior minor surfaces. An extension portion is formed integrally with the major rear surface of the rectangular cross-section of the block portion as a single compressed salt block, wherein the extension portion has a cross-sectional area in said horizontal plane in the form of a right truncated triangle, the extension portion having a first exterior side that is contiguous with one of the pair of exterior minor side surfaces of the block portion, a second side that is contiguous with the major rear surface of the block portion, and an exterior hypotenuse side that extends at an acute angle relative to the base surface of the block portion from a rear edge of the first exterior side toward the major rear surface of the block portion. A horizontal cross section of the elongated body is constant along the vertical longitudinal axis of the elongated body and the exterior hypotenuse side of the extension portion defines a functional face adapted to abut against a vertical wall or an exterior vertical surface of a tank of a water softener apparatus to position the compressed salt block within said water softener apparatus.

In alternative embodiments, the invention provides processes and methods for the recovery, removal or extracting of, and subsequent purification of uranium from a wet-process phosphoric acid using a continuous ion exchange processing approach, where the uranium is recovered from a phosphoric acid, or a phos-acid feedstock using either a dual or a single stage extraction methodology. In both cases an intermediate ammonium uranyl-tricarbonate solution is formed. In alternative embodiments, in the dual cycle approach, this solution is contacted in a second continuous ion exchange system with a strong anion exchange resin then subsequently recovered as an acidic uranyl solution that is further treated to produce an intermediate uranyl peroxide compound which is ultimately calcined to produce the final uranium oxide product. In alternative embodiments, in the single cycle case, the intermediate ammonium uranyl-tricarbonate solution is evaporated to decompose the ammonium carbonate and produce an intermediate uranium carbonate/oxide solid material. These solids are digested in an acid medium, and then processed in the same manner as the secondary regeneration solution from the dual cycle process to produce an intermediate uranyl peroxide that is calcined to produce a final uranium oxide product.

In alternative embodiments, the invention provides processes and methods for the recovery, removal or extracting of, and subsequent purification of uranium from a wet-process phosphoric acid using a continuous ion exchange processing approach, where the uranium is recovered from a phosphoric acid, or a phos-acid feedstock using either a dual or a single stage extraction methodology. In both cases an intermediate ammonium uranyl-tricarbonate solution is formed. In alternative embodiments, in the dual cycle approach, this solution is contacted in a second continuous ion exchange system with a strong anion exchange resin then subsequently recovered as an acidic uranyl solution that is further treated to produce an intermediate uranyl peroxide compound which is ultimately calcined to produce the final uranium oxide product. In alternative embodiments, in the single cycle case, the intermediate ammonium uranyl-tricarbonate solution is evaporated to decompose the ammonium carbonate and produce an intermediate uranium carbonate/oxide solid material. These solids are digested in an acid medium, and then processed in the same manner as the secondary regeneration solution from the dual cycle process to produce an intermediate uranyl peroxide that is calcined to produce a final uranium oxide product.

A system includes an ion exchange softener fluidly coupled to a wastewater treatment system. The first ion exchange softener may receive a first brine stream from the wastewater treatment system and to remove a plurality of minerals from the first brine stream to generate a second brine stream including the plurality of minerals and a third brine stream. The system also includes a mineral removal system disposed downstream from the ion exchange softener and that may receive the second brine stream and to generate a sodium chloride (NaCl) brine stream and an acid and caustic production system disposed downstream from and fluidly coupled to the mineral removal system. The acid and caustic production system includes a first electrodialysis (ED) system that may receive the NaCl brine stream from the mineral removal system and to generate hydrochloric acid (HCl) and sodium hydroxide (NaOH) from the NaCl brine stream. The system also includes a second ED system disposed downstream from the ion exchange softener and upstream of the acid and caustic production system. The second ED system is fluidly coupled to the ion exchange softener and to the acid and caustic production system, and the second ED may generate desalinated water from the third brine stream and an ED concentrate stream. The second ED system may direct the ED concentrate stream to the acid and caustic production system.

A system includes an ion exchange softener fluidly coupled to a wastewater treatment system. The first ion exchange softener may receive a first brine stream from the wastewater treatment system and to remove a plurality of minerals from the first brine stream to generate a second brine stream including the plurality of minerals and a third brine stream. The system also includes a mineral removal system disposed downstream from the ion exchange softener and that may receive the second brine stream and to generate a sodium chloride (NaCl) brine stream and an acid and caustic production system disposed downstream from and fluidly coupled to the mineral removal system. The acid and caustic production system includes a first electrodialysis (ED) system that may receive the NaCl brine stream from the mineral removal system and to generate hydrochloric acid (HCl) and sodium hydroxide (NaOH) from the NaCl brine stream. The system also includes a second ED system disposed downstream from the ion exchange softener and upstream of the acid and caustic production system. The second ED system is fluidly coupled to the ion exchange softener and to the acid and caustic production system, and the second ED may generate desalinated water from the third brine stream and an ED concentrate stream. The second ED system may direct the ED concentrate stream to the acid and caustic production system.

A reclaiming method is disclosed including conducting evaporation by introducing a part of the absorbent to recover CO.sub.2 or H.sub.2S in a gas in a closed system recovery unit and separating a degraded substance contained in the absorbent from the absorbent to be introduced into an evaporator and obtain recovery steam containing an absorbent and CO.sub.2 or H.sub.2S by a heating section that is provided on a circulation line that circulates in the evaporator; and removing ionic degraded substance by cooling the concentrate obtained in the evaporation and removing an ionic degraded substance in the concentrate after the cooling, wherein a purified concentrate from which the ionic degraded substance has been removed is reused as a purified absorbent.

A reclaiming method is disclosed including conducting evaporation by introducing a part of the absorbent to recover CO.sub.2 or H.sub.2S in a gas in a closed system recovery unit and separating a degraded substance contained in the absorbent from the absorbent to be introduced into an evaporator and obtain recovery steam containing an absorbent and CO.sub.2 or H.sub.2S by a heating section that is provided on a circulation line that circulates in the evaporator; and removing ionic degraded substance by cooling the concentrate obtained in the evaporation and removing an ionic degraded substance in the concentrate after the cooling, wherein a purified concentrate from which the ionic degraded substance has been removed is reused as a purified absorbent.