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.

The present invention provides a semi-automatic pressure type water softener including: an ionic resin tank (100) provided with an ionic resin; a regeneration vessel (200), into which a regenerant is introduced and which generates reclaimed water filled with the ionic resin; a drain valve (293) provided in the regeneration vessel (200) and configured to discharge residual water to the outside; a water inlet part (400) configured to selectively supply raw water to the ionic resin tank (100) and the regeneration vessel (200); and a timer/ceramic disk conversion valve (300) configured to select any one of a water softening mode, a raw water mode, and a regeneration mode to convert a passage between any two of the water inlet part (400), the ionic resin tank (100), and the regeneration tank (200), wherein the water softener is in the regeneration mode, any one of a first mode and a second mode is selected according to a preset method, wherein the first mode is operated for a preset period of time by the timer/ceramic disk conversion valve 300 such that the raw water is supplied to the regeneration vessel (200) to generate reclaimed water, and wherein in the second mode, the drain valve (293) is opened.

The present invention provides a semi-automatic pressure type water softener including: an ionic resin tank (100) provided with an ionic resin; a regeneration vessel (200), into which a regenerant is introduced and which generates reclaimed water filled with the ionic resin; a drain valve (293) provided in the regeneration vessel (200) and configured to discharge residual water to the outside; a water inlet part (400) configured to selectively supply raw water to the ionic resin tank (100) and the regeneration vessel (200); and a timer/ceramic disk conversion valve (300) configured to select any one of a water softening mode, a raw water mode, and a regeneration mode to convert a passage between any two of the water inlet part (400), the ionic resin tank (100), and the regeneration tank (200), wherein the water softener is in the regeneration mode, any one of a first mode and a second mode is selected according to a preset method, wherein the first mode is operated for a preset period of time by the timer/ceramic disk conversion valve 300 such that the raw water is supplied to the regeneration vessel (200) to generate reclaimed water, and wherein in the second mode, the drain valve (293) is opened.

The invention relates to sulfonated aminomethylated chelate resins, to a method for producing same, to the use thereof for obtaining and purifying metals, in particular rare earth metals, from aqueous solutions and organic liquids, and for producing highly pure silicon.

In an ion-exchange separation system, a single regeneration column provides for separation of anion and cation resins and the regeneration of both cation and anion resins with a very low level of cross-contamination. After regeneration most of the anion layer in the column is withdrawn, and most of the cation layer is withdrawn, but a portion of each layer adjacent to the interface between the layers remains in the column, to isolate these cross-contaminated portions from the regenerated resins. The withdrawn, regenerated anion and cation resins are placed back into the working vessel.

In an ion-exchange separation system, a single regeneration column provides for separation of anion and cation resins and the regeneration of both cation and anion resins with a very low level of cross-contamination. After regeneration most of the anion layer in the column is withdrawn, and most of the cation layer is withdrawn, but a portion of each layer adjacent to the interface between the layers remains in the column, to isolate these cross-contaminated portions from the regenerated resins. The withdrawn, regenerated anion and cation resins are placed back into the working vessel.

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.

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.

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.