METHOD FOR GENERATING A LITHIUM ELUATE SOLUTION FROM A LIQUID RESOURCE

Abstract

A method for generating a lithium eluate solution from a liquid resource, comprising using an ion-exchange reactor comprising a tank and ion-exchange particles, wherein the ion-exchange particles selectively absorb lithium from a liquid resource and elute a lithium eluate solution when treated with an acidic solution after absorbing lithium ions from said liquid resource, one or more particle traps, and provision for modulating the pH of said liquid resource; flowing a liquid resource into said ion-exchange reactor, thereby enabling said ion-exchange particles to selectively absorb lithium from said liquid resource; treating said ion-exchange particles with an acidic solution to produce said lithium eluate solution;and passing said lithium eluate solution through said particle traps to collect said lithium eluate solution, wherein said particle traps are configured to retain the ion exchange particles in the tank while allowing flows of said liquid resource, said lithium eluate solution, water or said acid solution to enter and exit the tank, or recirculate the ion exchange particles in the tank while allowing flows of said liquid resource, said lithium eluate solution, water or said acid solution to enter and exit the tank.

Description

METHOD FOR GENERATING A LITHIUM ELUATE SOLUTION FROM A LIQUID RESOURCE CROSS REFERENCE This application claims the benefit of U.S. Provisional Patent Application No. 62 / 636,766, filed February 28, 2018, which is incorporated herein by reference in its entirety. BACKGROUND OF THE INVENTION Lithium is an essential element for high-energy rechargeable batteries and other technologies. Lithium can be found in a variety of liquid solutions, including natural and synthetic brines and leachate solutions from minerals and recycled products. SUMMARY OF THE INVENTION Lithium can be extracted from liquid resources using an ion exchange process based on inorganic ion exchange materials. Inorganic ion exchange materials absorb lithium ions from a liquid resource while releasing hydrogen ions, and then elute the lithium ions in acid while absorbing the hydrogen ions. The ion exchange process can be repeated to extract lithium ions from a liquid resource and produce a concentrated lithium ion solution. The concentrated lithium ion solution can be further processed into chemicals for the battery industry or other industries. Ion exchange particles are loaded into an ion exchange reactor for lithium extraction. Alternating streams of brine, water, and acid flow through the ion exchange reactor to allow for the uptake of lithium from the brine onto the ion exchange particles, the washing of residual brine from the ion exchange particles with water, and the acidic elution of lithium from the ion exchange particles to form a lithium eluate solution. The release of hydrogen during lithium uptake will acidify the brine and limit lithium uptake unless the brine pH is maintained within a suitable range to facilitate thermodynamically favorable lithium uptake and concomitant hydrogen release. To retain the ion exchange particles in the ion exchange reactor, while allowing brine, water, and acid flows to enter and exit the ion exchange reactor, one or more particle traps are used with the ion exchange reactor. These particle traps separate the solid ion exchange particles from the 1 2085695 of 53 liquid flows by using filtration, gravity sedimentation, centrifugal sedimentation, magnetic fields, other solid-liquid separation methods, or combinations thereof. One aspect of the present invention is an ion exchange reactor for generating a lithium eluate solution from a liquid resource, comprising: a tank; ion exchange particles that selectively adsorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acidic solution after adsorbing lithium from said liquid resource; one or more particle traps; and provision for modulating the pH of said liquid resource. In some embodiments, said tank has a conical shape. In some embodiments, said conical shape allows said ion exchange particles to settle into a settled bed such that liquid can be removed from said settled bed. In some embodiments, the modulation of said pH of said liquid resource occurs in the tank. In some embodiments, the modulation of said pH of said liquid resource occurs prior to injection of said liquid resource into the tank. In some embodiments, said one or more particulate traps comprise one or more filters within said tank. In some embodiments, said one or more traps are located at the bottom of said tank. In some embodiments, said one or more particulate traps comprise one or more mesh screens. In some embodiments, the one or more meshes comprise a pore space of less than about 200 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 100 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 100 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 50 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 25 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 10 micrometers. In some embodiments, the one or more particle traps comprise multi-layered meshes. In some embodiments, the multi-layered meshes comprise at least one finer mesh for filtration and at least one coarser mesh for structural support. In some embodiments, the one or more particle traps comprise one or more meshes supported by a structural support. In some embodiments, the one or more particle traps comprise one or more polymeric meshes. 2085695 of 53 In some embodiments, the one or more polymeric meshes are selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. In some embodiments, the one or more particle traps comprise one or more meshes comprising a metal wire mesh. In some embodiments, the metal wire mesh is coated with a polymer. In some embodiments, said ion exchange reactor is configured to move said ion exchange particles into one or more washing columns. In some embodiments, said ion exchange reactor is configured to allow the ion exchange particles to settle in one or more washing columns. In some embodiments, said columns are fixed to the bottom of said tank. In some embodiments, said one or more particulate traps comprise one or more filters mounted in one or more ports through the wall of said tank. In some embodiments, said one or more particulate traps comprise one or more filters external to said tank, and with provision for fluid communication between said one or more filters and said tank.In some embodiments, said one or more particle traps comprise one or more gravity settling devices external to said tank, and with provision for fluid communication between said one or more gravity settling devices and said tank. In some embodiments, said one or more particle traps comprise one or more gravity settling devices internal to said tank. In some embodiments, said one or more particle traps comprise one or more centrifugal settling devices external to said tank, and with provision for fluid communication between said one or more centrifugal settling devices and said tank. In some embodiments, said one or more particulate traps comprise one or more centrifugal settling devices internal to said tank. In some embodiments, said one or more particulate traps comprise one or more settling tanks, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more settling tanks, centrifugation devices, or combinations thereof, and said tank. In some embodiments, said one or more particulate traps comprise one or more screens, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more screens, centrifugation devices, or combinations thereof, and said tank. In some embodiments, said one or more particulate traps 2085695 of 53 comprise one or more settling tanks, one or more screens, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more settling tanks, screens, or combinations thereof, and said tank. In some embodiments, said one or more particle traps comprise one or more screens, one or more settling tanks, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more screens, one or more settling tanks, centrifugation devices, or combinations thereof, and said tank. In some embodiments, the ion exchange particles are agitated. In some embodiments, the ion exchange particles are agitated by a mixer. In some embodiments, the ion exchange particles are agitated by an impeller. In some embodiments, the ion exchange particles are fluidized by pumping a solution into the tank near the bottom of the tank. In some embodiments, the ion exchange particles are fluidized by pumping a solution from the tank back into the tank near the bottom of the tank. In some embodiments, the ion exchange particles are fluidized by pumping a slurry of ion exchange particles from near the bottom of the tank to a higher level in the tank. In some embodiments, the ion exchange reactor further comprises one or more staged elution tanks, wherein intermediate eluate solutions comprising mixtures of protons and lithium ions are stored and further used to elute lithium from said freshly lithiated ion exchange particles. In some embodiments, the ion exchange reactor further comprises one or more staged elution tanks, wherein intermediate eluate solutions comprising mixtures of protons and lithium ions are mixed with additional acid and further used to elute lithium from said ion exchange particles. In some embodiments, said ion exchange particles further comprise a coating material. In some embodiments, said coating material is a polymer. In some embodiments, said coating material comprises a chloropolymer, a fluoropolymer, a chlorofluoropolymer, a hydrophilic polymer, a hydrophobic polymer, copolymers thereof, mixtures thereof, or combinations thereof. An aspect described herein is an ion exchange system for generating a lithium eluate solution from a liquid resource, comprising: a networked plurality of tanks; ion exchange particles that selectively absorb lithium from said 2085695 of 53 liquid resource and elute said lithium eluate solution when treated with an acid solution; one or more particle traps; and provision for modulating the pH of said liquid resource. In some embodiments, said ion exchange particles are retained in said networked plurality of tanks with flows of brine, wash solution, and acid moving alternately through said plurality of tanks. In some embodiments, said ion exchange particles move through said networked plurality of tanks against countercurrent flows of brine, wash solution, and acid. In some embodiments, tanks selected from said networked plurality of tanks are sized for batches of brine, wash solution, or acid, and wherein said ion exchange particles move through said networked plurality of tanks. An aspect of the present invention is a method for generating a lithium eluate solution from a liquid resource, comprising: providing an ion exchange reactor comprising a tank, ion exchange particles that selectively adsorb lithium from a liquid resource and elute a lithium eluate solution when treated with an acidic solution after adsorbing lithium ions from said liquid resource, one or more particle traps, and provision for modulating the pH of said liquid resource; flowing a liquid resource into said ion exchange reactor, thereby allowing said ion exchange particles to selectively adsorb lithium from said liquid resource; treating said ion exchange particles with an acidic solution to produce said lithium eluate solution; and passing said lithium eluate solution through said one or more particle traps to collect said lithium eluate solution. In some embodiments, said tank has a conical shape. In some embodiments, said conical shape allows said ion exchange particles to settle into a settled bed such that liquid can be removed from said settled bed. In some embodiments, the modulation of said pH of said liquid resource occurs in the tank. In some embodiments, the modulation of said pH of said liquid resource occurs prior to injection of said liquid resource into the tank. In some embodiments, said one or more particulate traps comprise one or more filters within said tank. In some embodiments, said one or more traps are located at the bottom of said tank. In some embodiments, said one or more particulate traps comprise one or more mesh screens. In some embodiments, said one or more meshes comprise a pore space of less than about 200 microns. In some embodiments, said one or more meshes comprise a pore space of less than about 100 microns. 2085695 of 53 micrometers. In some embodiments, said one or more meshes comprise a pore space of less than about 100 micrometers. In some embodiments, said one or more meshes comprise a pore space of less than about 50 micrometers. In some embodiments, said one or more meshes comprise a pore space of less than about 25 micrometers. In some embodiments, said one or more meshes comprise a pore space of less than about 10 micrometers. In some embodiments, said one or more particle traps comprise multi-layered meshes. In some embodiments, said multi-layered meshes comprise at least one finer mesh for filtration and at least one coarser mesh for structural support. In some embodiments, said one or more particle traps comprise one or more meshes supported by a structural support.In some embodiments, said one or more particle traps comprise one or more polymeric meshes. In some embodiments, said one or more polymeric meshes are selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. In some embodiments, said one or more particle traps comprise one or more meshes comprising a metal wire mesh. In some embodiments, said metal wire mesh is coated with a polymer. In some embodiments, said ion exchange reactor is configured to move said ion exchange particles into one or more washing columns. In some embodiments, said ion exchange reactor is configured to allow the ion exchange particles to settle in one or more washing columns. In some embodiments, said columns are secured to the bottom of said tank. In some embodiments, said one or more particle traps comprise one or more filters mounted in one or more ports through the wall of said tank. In some embodiments, said one or more particulate traps comprise one or more filters external to said tank, and with provision for fluid communication between said one or more filters and said tank. In some embodiments, said one or more particulate traps comprise one or more gravity settling devices external to said tank, and with provision for fluid communication between said one or more gravity settling devices and said tank. In some embodiments, said one or more particulate traps comprise one or more gravity settling devices internal to said tank. In some embodiments, said one or more particulate traps comprise one or more centrifugal settling devices external to said tank, and with provision for fluid communication between said one or more 2085695 of 53 centrifugal sedimentation devices and said tank. In some embodiments, said one or more particulate traps comprise one or more centrifugal sedimentation devices internal to said tank. In some embodiments, said one or more particulate traps comprise one or more sedimentation tanks, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more sedimentation tanks, centrifugation devices, or combinations thereof, and said tank. In some embodiments, said one or more particulate traps comprise one or more screens, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more screens, centrifugation devices, or combinations thereof, and said tank.In some embodiments, said one or more particulate traps comprise one or more settling tanks, one or more screens, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more settling tanks, screens, or combinations thereof, and said tank. In some embodiments, said one or more particulate traps comprise one or more screens, one or more settling tanks, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more screens, one or more settling tanks, centrifugation devices, or combinations thereof, and said tank. In some embodiments, the ion exchange particles are agitated. In some embodiments, the ion exchange particles are agitated by a mixer. In some embodiments, the ion exchange particles are agitated by an impeller. In some embodiments, the ion exchange particles are fluidized by pumping a solution into the tank near the bottom of the tank. In some embodiments, the ion exchange particles are fluidized by pumping a solution from the tank back into the tank near the bottom of the tank. In some embodiments, the ion exchange particles are fluidized by pumping a slurry of ion exchange particles from near the bottom of the tank to a higher level in the tank. In some embodiments, the method further comprises one or more stepwise elution tanks, wherein intermediate eluate solutions comprising mixtures of protons and lithium ions are stored and further used to elute lithium from said freshly lithiated ion exchange particles. In some embodiments, the method further comprises one or more stepwise elution tanks, wherein the intermediate eluate solutions comprising mixtures of protons and lithium ions are stored and further used to elute lithium from said freshly lithiated ion exchange particles. 2085695 of 53 intermediate eluates comprising mixtures of protons and lithium ions are mixed with additional acid and are further used to elute lithium from said ion exchange particles. In some embodiments, said ion exchange particles further comprise a coating material. In some embodiments, said coating material is a polymer. In some embodiments, said coating material comprises a chloropolymer, a fluoropolymer, a chlorofluoropolymer, a hydrophilic polymer, a hydrophobic polymer, copolymers thereof, mixtures thereof, or combinations thereof. An aspect described herein is an ion exchange reactor for generating a lithium eluate solution from a liquid resource, comprising: a conical shaped tank, said conical shape allowing said ion exchange particles to settle into a settled bed so that liquid can be removed from said settled bed; ion exchange particles that selectively adsorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acidic solution after adsorbing lithium from said liquid resource; one or more particle traps located at the bottom of said tank, wherein said one or more particle traps comprise one or more meshes; and provision for modulating a pH of said liquid resource, wherein said modulating said pH of said liquid resource is configured to take place in the tank or prior to injection of said liquid resource into the tank. In some embodiments, the one or more meshes comprise a pore space of less than about 200 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 100 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 100 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 50 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 25 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 10 microns. In some embodiments, said one or more meshes are one or more polymeric meshes. In some embodiments, said one or more polymeric meshes are selected from the group consisting of polyether ether ketone, ethylene tetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. In some embodiments, said one or more meshes comprise a metal wire mesh. In some embodiments, said metal wire mesh is coated with a polymer. In some 2085695 of 53 embodiments, said polymeric coating of said metal wire mesh is selected from the group consisting of polyether ether ketone, ethylene-tetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. An aspect described herein is an ion exchange reactor for generating a lithium eluate solution from a liquid resource, comprising: a conical shaped tank, said conical shape allowing said ion exchange particles to settle into a settled bed so that liquid can be removed from said settled bed; ion exchange particles that selectively adsorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acidic solution after adsorbing lithium from said liquid resource; one or more particle traps located at the bottom of said tank, wherein said one or more particle traps comprise multi-layered meshes; and provision for modulating a pH of said liquid resource, wherein said modulating said pH of said liquid resource is configured to take place in the tank or prior to injection of said liquid resource into the tank.In some embodiments, said multi-layer meshes comprise at least one finer mesh for filtration and at least one coarser mesh for structural support. In some embodiments, said one or more particle traps comprise one or more meshes supported by a structural support. In some embodiments, said one or more meshes are one or more polymeric meshes. In some embodiments, said one or more polymeric meshes are selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethyleneterephthalate, polypropylene, and combinations thereof. In some embodiments, said one or more meshes comprise a metal wire mesh. In some embodiments, said metal wire mesh is coated with a polymer.In some embodiments, said polymeric coating of said metal wire mesh is selected from the group consisting of polyether ether ketone, ethylene tetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. An aspect described herein is a method for generating a lithium eluate solution from a liquid resource, comprising: providing an ion exchange reactor comprising (i) a conical shaped tank, wherein said conical shape allows said ion exchange particles to settle into a settled bed so that liquid can be removed from said settled bed; (ii) ion exchange particles that selectively absorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acid solution after absorbing lithium from said liquid resource; (iii) one or more particle traps located at the bottom of said tank, wherein said one or more 2085695 of 53 particle traps comprising one or more meshes; and (iv) provision for modulating the pH of said liquid resource, wherein said modulation of said pH of said liquid resource is configured to take place in the tank or prior to injection of said liquid resource into the tank; flowing a liquid resource to said ion exchange reactor, thereby allowing said ion exchange particles to selectively absorb lithium from said liquid resource; treating said ion exchange particles with an acidic solution to produce said lithium eluate solution; and passing said lithium eluate solution through said one or more particle traps to collect said lithium eluate solution. In some embodiments, the one or more meshes comprise a pore space of less than about 200 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 100 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 100 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 50 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 25 microns. In some embodiments, the one or more meshes comprise a pore space of less than about 10 microns. In some embodiments, said one or more meshes are one or more polymeric meshes. In some embodiments, one or more polymeric meshes are selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. In some embodiments, said one or more meshes comprise a metal wire mesh. In some embodiments, said metal wire mesh is coated with a polymer. In some embodiments, said polymeric coating of said metal wire mesh is selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. An aspect described herein is a method for generating a lithium eluate solution from a liquid resource, comprising: providing an ion exchange reactor comprising: (i) a conical shaped tank, wherein said conical shape allows said ion exchange particles to settle into a settled bed so that liquid can be removed from said settled bed; (ii) ion exchange particles that selectively absorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acid solution after absorbing lithium from said liquid resource; (iii) one or more particle traps located at the bottom of said tank, wherein said one or more 2085695 of 53 particle traps comprising multi-layer meshes; and (iv) provision for modulating the pH of said liquid resource, wherein said modulation of said pH of said liquid resource is configured to take place in the tank or prior to injection of said liquid resource into the tank; flowing a liquid resource to said ion exchange reactor, thereby allowing said ion exchange particles to selectively absorb lithium from said liquid resource; treating said ion exchange particles with an acidic solution to produce said lithium eluate solution; and passing said lithium eluate solution through said one or more particle traps to collect said lithium eluate solution. In some embodiments, said multi-layer meshes comprise at least one finer mesh for filtration and at least one coarser mesh for structural support. In some embodiments, said one or more particle traps comprise one or more meshes supported by a structural support. In some embodiments, said one or more meshes are one or more polymeric meshes. In some embodiments, said one or more polymeric meshes are selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. In some embodiments, the one or more meshes comprise a metal wire mesh. In some embodiments, the metal wire mesh is coated with a polymer. In some embodiments, the polymer coating of the metal wire mesh is selected from the group consisting of polyether ether ketone, ethylene tetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. INCORPORATION BY REFERENCE All publications, patents and patent applications mentioned in this specification are incorporated herein by reference to the same extent as if each individual publication, patent or patent application were specifically and individually indicated as incorporated by reference. BRIEF DESCRIPTION OF THE DRAWINGS The novel features of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description, which sets forth illustrative embodiments in which the principles of the invention are utilized, and the accompanying drawings, of which: 2085695 of 53 FIG. 1 illustrates an ion exchange reactor comprising a stirred tank having a conical shape and one or more filters mounted in a port through the wall of the tank. FIG. 2 illustrates an ion exchange reactor comprising a stirred tank having a conical shape and one or more filters within the tank. FIG. 3 illustrates an ion exchange reactor comprising a stirred tank having a conical shape and one or more filters external to the tank, with provision for fluid communication between the one or more filters and the tank. FIG. 4 illustrates an ion exchange reactor comprising a stirred tank and a conical-shaped settling tank, with provision for fluid communication between the settling tank and the tank. FIG. 5 illustrates an ion exchange system comprising a networked plurality of stirred tanks, and one or more filters external to the tanks. FIG. 6 illustrates an ion exchange system comprising a networked plurality of tanks including multiple brine reactors networked with an acid reactor. FIG. 7 illustrates an ion exchange system comprising a network of tanks wherein ion exchange particles move against a countercurrent flow of brine, wash solution, and acid, and the system is configured to operate continuously or semi-continuously. FIG. 8 illustrates an ion exchange reactor with provision for a series of staged elution tanks, wherein intermediate eluate solutions comprising a mixture of protons and lithium ions are stored and further used to elute lithium from the ion exchange particles. FIG. 9A illustrates an ion exchange reactor comprising a stirred tank having a partially conical shape and one or more filters within the tank. FIG. 9B depicts the recovery of lithium from a liquid resource in multiple cycles between the liquid resource and the acid using the ion exchange reactor illustrated in FIG. 9A. FIG. 10 illustrates an ion exchange reactor comprising a stirred tank having a partially conical shape terminating in a thinner cylindrical column with one or more filters within the tank. FIG. 11 illustrates an ion exchange reactor comprising a stirred tank having a partially conical shape terminating in a thinner cylindrical column with one or more filters within the tank and a pumping unit for pumping liquid out of the tank and back to the bottom of the thinner cylindrical column. 2085695 of 53 FIG. 12 illustrates an ion exchange reactor comprising a stirred tank having a partially conical shape with one or more filters within the tank and a pumping unit for pumping liquid out of the tank and back to the bottom of the thinner cylindrical column. DETAILED DESCRIPTION OF THE INVENTION The terms lithium, lithium ion, and Li+ are used interchangeably herein, and these terms are synonyms unless specifically indicated otherwise. The terms hydrogen, hydrogen ion, proton, and H+ are used interchangeably herein, and these terms are synonyms unless specifically indicated otherwise. The terms lithiated, lithium, lithium-enriched, and lithium-exchanged are used interchangeably herein, and these terms are synonyms unless specifically indicated otherwise. The terms protonated, hydrogen-enriched, and proton-exchanged are used interchangeably herein, and these terms are synonyms unless specifically indicated otherwise. Lithium ion exchange reactor with particle traps An aspect of the invention described herein is an ion exchange reactor for extracting lithium from a liquid resource. This reactor functions to contact the liquid resource with ion exchange particles such that the ion exchange particles can capture lithium from the liquid resource, separate the ion exchange particles from the liquid resource, wash the particles with an aqueous solution, separate the ion exchange particles from the aqueous solution, elute the lithium from the particles using an acidic solution, and separate the particles from the acidic solution. The reactor includes a provision for measuring and adjusting the pH of the liquid resource, to neutralize protons released by the ion exchange material during lithium capture. One aspect of the invention described herein is an ion exchange reactor for extracting lithium from a liquid resource, comprising: a) one or more tanks; b) ion exchange particles; c) one or more particle traps; and d) provision for modulating the pH of the liquid resource. An aspect of the invention described herein is a method for extracting lithium from a liquid resource, comprising: a) providing an ion exchange reactor comprising one or more particle traps; b) providing ion exchange particles in said ion exchange reactor; c) contacting said ion exchange particles in said ion exchange reactor with said liquid resource, wherein hydrogen ions from said particles are released into the atmosphere. 2085695 of 53 ion exchange particles are exchanged with lithium ions from said liquid resource to produce lithium-enriched ion exchange particles in said ion exchange unit; d) withdrawing said liquid resource from said ion exchange reactor while retaining said ion exchange particles in said ion exchange reactor using said one or more particle traps; e) washing said lithium-enriched ion exchange particles with an aqueous solution one or more times; f) withdrawing said aqueous solution from said ion exchange reactor while retaining said ion exchange particles in said ion exchange reactor using said one or more particle traps;g) treating said lithium-enriched ion exchange particles with an acid solution, wherein said lithium ions in said lithium-enriched ion exchange particles are exchanged with hydrogen ions in said acid solution to produce a lithium eluate; and h) removing said lithium eluate from said ion exchange reactor while retaining said ion exchange particles in said ion exchange reactor using said one or more particle traps; In some embodiments, the acid solution is hydrochloric acid, sulfuric acid, nitric acid, other acid, or combinations thereof. In some embodiments, the acid solution has a proton concentration of less than about 10 N, less than about 3 N, less than about 1 N, less than about 0.3 N, less than about 0.1 N, more than about 0.05 N, more than about 0.1 N, more than about 0.2 N, more than about 0.3 N, more than about 0.4 N, more than about 0.5 N, more than about 0.75 N, more than about 1 N, more than about 2 N, more than about 3 N, more than about 4 N, more than about 5 N, more than about 6 N, more than about 7 N, more than about 8 N, more than about 9 N, from about 0.05 N to about 10 N, from about 0.1 N to about 10 N, from about 0.2 N to about 10 N, from about 0.3 N to about 10 N, from about 0.4 N to about 10 N, from about 0.5 N to about 10 N, from about 0.6 N to about 10 N, from about 0.7 N to about 10 N, from about 0.8 N to about 10 N, from about 0.9 N to about 10 N, from about 1 N to about 10 N, from about 1 N to about 9 N, from about 2 N to about 8 N, or from about 3 N to about 7 N., 2085695 of 53 In some embodiments, the lithium eluate solution contains lithium chloride, lithium sulfate, lithium nitrate, or other lithium salts. In some embodiments, the lithium eluate solution is processed to produce lithium metal, lithium carbonate, lithium hydroxide, lithium hydroxide monohydrate, lithium nitrate, lithium phosphate, lithium chloride, lithium metal, organometallic lithium, or other lithium salts. Modeled tanks An aspect of the invention described herein is an ion exchange reactor for extracting lithium from liquid resources, comprising: a) a tank with a cross-sectional area that is smaller at the bottom; b) ion exchange particles that are loaded into the tank; c) one or more particle traps for containing the ion exchange particles in the tank while removing liquid flows from the tank; and d) a provision for modulating the pH of the liquid resource in the tank. An aspect of the invention described herein is an ion exchange reactor for generating a lithium eluate solution from a liquid resource, comprising: a conical shaped tank, said conical shape allowing said ion exchange particles to settle into a settled bed so that liquid can be removed from said settled bed; ion exchange particles that selectively absorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acidic solution after absorbing lithium from said liquid resource; one or more particle traps located at the bottom of said tank, wherein said one or more particle traps comprise one or more meshes; and provision for modulating the pH of said liquid resource, wherein said modulation of said pH of said liquid resource is configured to take place in the tank or prior to injection of said liquid resource into the tank.An aspect of the invention described herein is an ion exchange reactor for generating a lithium eluate solution from a liquid resource, comprising: a conical shaped tank, said conical shape allowing said ion exchange particles to settle into a settled bed so that liquid can be removed from said settled bed; ion exchange particles that selectively adsorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acidic solution after adsorbing lithium from said liquid resource; one or more particle traps located at the bottom of said tank, wherein said one or more particle traps comprise multi-layered meshes;and provision for modulating the pH of said liquid resource, wherein said modulation of said pH of said liquid resource is configured to take place in the tank or prior to injection of said liquid resource into the tank; 2085695 of 53 In some embodiments, the ion exchange reactor comprises a cone-shaped tank. In some embodiments, the cone shape allows the ion exchange particles to settle to the bottom of the cone shape while liquid is removed from the tank above the settled bed of ion exchange particles. In some embodiments, a particle trap may have an inlet located above the settled height of the ion exchange particles. In some embodiments, the shape of the tank allows for the removal of liquid above the settled bed of ion exchange particles. In some embodiments, a port is located at or near the bottom of the tank to allow a slurry comprising ion exchange particles and water to be removed from the tank or injected into the tank.In some embodiments, a filter is located at or near the bottom of the tank, allowing a suspension comprising ion exchange particles and water to be dewatered. In some embodiments, a filter is located at or near the bottom of the tank, allowing solutions to be injected into the tank through the filter. In some embodiments, the ion exchange reactor comprises a tank that is conical or pyramidal near the bottom. In some embodiments, the ion exchange reactor comprises a tank that is conical or pyramidal near the bottom, and cylindrical or rectangular near the top. In some embodiments, volumes of the liquid resource and the acid solution are charged to the ion exchange reactor. In some embodiments, the volume of the liquid resource charged to the ion exchange reactor is greater than the volume of the acid solution by a factor of more than about 2x, more than about 5x, more than about 10x, more than about 20x, more than about 50x, or more than about 100x. In some embodiments, the reactor tank may have a cone shape that is narrower at the bottom to facilitate mixing of ion exchange particles in the tank, to facilitate settling of the ion exchange particles, to facilitate washing of the ion exchange particles, or to facilitate separation of the ion exchange particles from liquid solutions such as liquid resources, acid solution, or wash solution. In some embodiments, the ion exchange reactor may have a mixing device for mixing ion exchange particles with liquid resources, wash solutions, or acid elution solutions. In some embodiments, the mixing device is an overhead mixer. In some embodiments, the mixing device is a propeller or impeller that circulates brine throughout the tank. In some embodiments, the mixing device is an impeller that raises a slurry of brine. 2085695 of 53 ion exchange particles from the bottom of the tank. In some embodiments, the ion exchange reactor may have one or more mixing devices. In some embodiments, the mixing device is a pump that injects solution into the tank, thereby agitating a bed of ion exchange particles. In some embodiments, the mixing device is a pump that injects solution into the tank, thereby fluidizing or suspending ion exchange particles in solution. In some embodiments, the ion exchange particles are mixed into a solution by pumping a slurry from near the bottom of the tank and injecting said slurry at a higher level in the tank. In some embodiments, the fluidized ion exchange material is mixed by being pumped into and / or out of the tank without filtration.In some embodiments, the ion exchange reactor tank is equipped with one or more sprayers that wash the ion exchange particles from the sides of the tank and move them to the bottom of the tank. In some embodiments, the ion exchange reactor is equipped with baffles. In some embodiments, one or more tanks are equipped with baffles. In some embodiments, one or more tanks are equipped with baffles to enhance mixing of the ion exchange particles with brine, water, acid, or other solutions. In some embodiments, the ion exchange reactor tank is rectangular, cylindrical, conical, spherical, parallelogram, rhombohedral, pyramidal, or combinations thereof. In some embodiments, the one or more meshes comprise a pore space of less than about 200 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 100 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 100 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 50 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 25 micrometers. In some embodiments, the one or more meshes comprise a pore space of less than about 10 micrometers. In some embodiments, the one or more meshes are one or more polymeric meshes.In some embodiments, the one or more polymeric meshes are selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. In some embodiments, the one or more meshes comprise a metal wire mesh. In some embodiments, the metal wire mesh is coated with a polymer. In some embodiments, the. 2085695 of 53 polymeric coating of said metal wire mesh is selected from the group consisting of polyether ether ketone, ethylene-tetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. In some embodiments, the multi-layer meshes comprise at least one finer mesh for filtration and at least one coarser mesh for structural support. In some embodiments, the one or more particulate traps comprise one or more meshes supported by a structural support. In some embodiments, the one or more meshes are one or more polymeric meshes. In some embodiments, the one or more polymeric meshes are selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethyleneterephthalate, polypropylene, and combinations thereof. In some embodiments, the one or more meshes comprise a metal wire mesh. In some embodiments, the metal wire mesh is coated with a polymer.In some embodiments, the polymeric coating of said metal wire mesh is selected from the group consisting of polyether ether ketone, ethylene-tetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. Filters In some embodiments, the particle trap is a filter. In some embodiments, the filter is operated as a cake filter. In some embodiments, the filter is operated to limit the formation of a filter cake. In some embodiments, the filter is operated with clean flow. In some embodiments, the filter is operated with backwashing. In some embodiments, the filter comprises a polymer, a porous polymer, a polymeric mesh, or a polymeric composite. In some embodiments, the filter comprises a woven polymer or a polymeric fabric. In some embodiments, the filter comprises polypropylene, polyetheretherketone (PEEK), polyvinylidenedifluoride (PVDF), polysulfone, polyethylene, nylon, or other polymeric material. In some embodiments, the filter comprises a ceramic, metallic, or alloy material. In some embodiments, the filter comprises a polymer, polyaryl ether ketone, polyethylene terephthalate, ethylene tetrafluoroethylene, a hydrophilic polymer, a hydrophobic polymer, a copolymer, a block copolymer, or combinations thereof. In some embodiments, the filter comprises a steel mesh or other metal mesh coated with polymer.In some embodiments, the filter comprises a polymer-coated stainless steel mesh. In some embodiments, the filter comprises a polymer-coated 304 stainless steel mesh. In some embodiments, the coating on the steel mesh comprises an epoxy, a silicone, a chloropolymer, a fluoropolymer, or a chlorofluoropolymer. 2085695 of 53 polymer, polypropylene, polyetheretherketone (PEEK), polyvinylidenedifluoride (PVDF), polysulfone, polyethylene, a thermal curing epoxy, an air-curing epoxy, a phenolic epoxy, a phenolic polymer, polytetrafluoroethylene, fluorinated ethylene propylene, a ceramic-epoxy composite coating, ethylene chlorotrifluoroethylene, other polymers, combinations thereof, or copolymers thereof. In some embodiments, the mesh comprises an epoxy, a silicone, a chloropolymer, a fluoropolymer, a chlorofluoropolymer, polypropylene, polyetheretherketone (PEEK), polyvinylidenedifluoride (PVDF), polysulfone, polyethylene, a heat-curing epoxy, an air-curing epoxy, a phenolic epoxy, a phenolic polymer, polytetrafluoroethylene, fluorinated ethylene propylene, a ceramic-epoxy composite coating, ethylene chlorotrifluoroethylene, other polymers, combinations thereof, or copolymers thereof.In some embodiments, the filter comprises a mesh comprising polyether ether ketone. In some embodiments, the mesh has a pore size of less than about 200 microns, less than about 100 microns, less than about 50 microns, less than about 25 microns, less than about 10 microns, less than about 2 microns, greater than about 200 microns, or greater than about 400 microns. In some embodiments, the mesh is a woven polymer or a polymeric fabric. In some embodiments, the filter is a mesh with a weave that is plain weave, twill weave, plain Dutch weave, twill Dutch weave, or combinations thereof. In some embodiments, the filter comprises a stainless steel mesh.In some embodiments, the filter comprises a stainless steel mesh coated to enhance acid resistance with a material such as nickel, a nickel alloy, an oxide, or other acid-resistant material. In some embodiments, the filter comprises polyamide, aromatic polyamide, polyvinylamine, polypyrrolidine, polyfuran, polyethersulfone, polysulfone, polypiperazine-amide, polybenzimidazoline, polyoxadiazole, acetylated cellulose, cellulose, a polymer with alternative functionalization of sulfonation, carboxylation, phosphorylation, or combinations thereof, another polymeric layer, or combinations thereof. In some embodiments, the filter further comprises a fabric, polymeric, composite, or metallic support. In some embodiments, the filter comprises a metallic material coated with oxide, epoxy, polymeric material, or combinations thereof that imbue chemical resistance. In some embodiments of the filter, the filters are woven from monofilament or multifilament yarns of material. In some embodiments, the filter fabric weave is square weave, plain twill weave, plain Dutch weave, Dutch twill weave, reverse Dutch weave, duplex Dutch weave, betamesh Dutch weave, basket weave, or combinations thereof. 2085695 of 53 In some embodiments of the ion exchange reactor, the filter is located inside the tank, outside the tank (external to the tank), or is mounted in one or more ports through the tank wall. In some embodiments, the filter is a flat filter, a tubular filter, a hollow fiber tube filter, a cartridge filter, a Scheibler filter, a Vallex filter, a Sweetland filter, a horizontal leaf filter, a centrifugal discharge filter, a compression filter, a Nutsche filter, or a candle filter. In some embodiments, the ion exchange reactor may have more than about one, more than about 5, more than about 20, or more than about 100 filters. In some embodiments, a rotary fan press is used to separate the liquid solution from a slurry comprising a liquid solution and ion exchange particles. In some embodiments, the filters are in the tank. In some embodiments, the filters are mounted in the tank at different heights. In some embodiments, the filters are mounted to a port or flange in the tank wall. In some embodiments, one or more filters are mounted at the bottom of one or more tanks. In some embodiments, one or more filters are mounted at the bottom of one or more columns that are mounted at the bottom of one or more tanks. In some embodiments, the filters are approximately flush with the tank wall. In some embodiments with multiple filters, filters near the top of the tank are used while the ion exchange particles are allowed to settle to the bottom of the tank under the force of gravity.In some embodiments, filters near the bottom of the tank are used after the ion exchange particles have substantially settled. In some embodiments, the filters are arranged vertically or horizontally. In some embodiments, the filters form an array within the volume or along the sides of the tank. In some embodiments, multiple filters are used in series or parallel. In some embodiments, multiple filters are used in series with varying pore sizes. In some embodiments, a filter comprises a smaller mesh mounted over a larger mesh, where the smaller mesh blocks the ion exchange particles and the larger mesh provides firmness to support the smaller mesh. In some embodiments, liquid resources, acid solutions, or wash solutions are removed from the tank through filters. In some embodiments, acid solutions are removed from the tank through filters near the bottom of the tank. In some embodiments, liquid resources are removed from the tank through filters near the top, middle, and bottom of the tank. In some embodiments, 2085695 of 53 embodiment, the wash solutions are removed from the tank through filters near the top, middle and bottom of the tank. In some embodiments, broken filters, or filters that no longer perform within the acceptable range of their original specifications, are replaced during operation of the ion exchange reactor or upon shutdown of the ion exchange reactor. In some embodiments, multiple candle filters are inserted into the tank, and when one filter fails, pumping through the filter is suspended while pumping through the other filters is maintained. In some embodiments, the presence of ion exchange particles in a tube or pipe connected to a filter is used to detect filter failure. In some embodiments, one or more pressure sensors are used to detect failure of a filter, a particle trap, a solid-liquid separation apparatus, or combinations thereof. In some embodiments, the ion exchange material is contained in a compartment with filters that allow liquid solutions to enter the compartment. In some embodiments, the ion exchange material is contained in a rotating compartment. In some embodiments, the compartment may have baffles or other fittings designed to guide liquid solutions through the compartment. In some embodiments, the reactor is a rotating bed reactor. In some embodiments, the filter is a belt filter, a plate and frame filter press, a pressure vessel containing filter elements, a rotary drum filter, a rotary disc filter, a cartridge filter, a centrifugal filter with a fixed or moving bed, a metal screen, a perforated basket centrifuge, a three-point centrifuge, a peeler-type centrifuge, or a pusher centrifuge. In some embodiments, the filter may use a displacement or vibrating device. In some embodiments, the filter is horizontal, vertical, or may use a siphon. In some embodiments, a filter cake is prevented, limited, or eliminated by the use of gravity, centrifugal force, electric field, vibration, brushes, liquid jets, scrapers, intermittent reverse flow, vibration, cross-flow filtration, or pumping slurries across the filter surface. In some embodiments, the slurry of ion exchange particles and liquid is moved tangentially to the filter to limit cake growth. In some embodiments, gravitational, magnetic, centrifugal settling, or other solid-liquid separation means are used before, during, or after filtration to prevent cake formation. 2085695 of 53 In some embodiments, a filter comprises a screen, a metal screen, a sieve, a curved sieve, a bent sieve, a high frequency electromagnetic screen, a resonance screen, or combinations thereof. In some embodiments, a deep bed filter is used to remove ion exchange particles from a liquid resource stream before it is re-injected into the ground. Other particle traps In some embodiments, one or more particle traps are a solid-liquid separation apparatus. In some embodiments of the ion exchange reactor, one or more particle traps are external particle traps located externally to the tank. In some embodiments, a dilute slurry is removed from the tank, transferred to an external particle trap, and separated into a concentrated slurry and a solution with low or no suspended solids. In some embodiments, the concentrated slurry is returned to the tank or transferred to a different tank. In some embodiments, the ion exchange particles are transferred from a brine tank to another brine tank, from an acid tank to another acid tank, from a wash tank to another wash tank, from a brine tank to a wash tank, from a wash tank to an acid tank, from an acid tank to a wash tank, or from an acid tank to a brine tank. In some embodiments, the particulate traps may use gravitational settling. In some embodiments, the particulate traps may include a settling tank, a thickener, a clarifier, a gravity thickener. In some embodiments, the particulate traps are operated in batch or discontinuous mode, semi-batch mode, semi-continuous mode, or continuous mode. In some embodiments, the particulate traps include a circular bucket thickener where the slurry enters through a central inlet such that the slurry is dispersed in the thickener with one or more raking components that spin and concentrate the ion exchange particles in a zone where the particles can exit through the bottom of the thickener. In some embodiments, the particulate traps include a deep cone, a deep cone tank, a deep cone compression tank, or a tank in which the slurry is compacted by weight. In some embodiments, the particulate traps include a tray thickener with a plurality of vertically oriented thickeners with a central axis and raking components. In some embodiments, the particulate traps include a deep cone, a deep cone tank, a deep cone compression tank, or a tank in which the slurry is compacted by weight. 2085695 of 53 particles include a laminar thickener with inclined plates or tubes that may be smooth, flat, rough, or corrugated. In some embodiments, the particulate traps include a gravity clarifier that may be a rectangular basin with a feed at one end and an overflow at the opposite end, optionally with paddles and / or a chain mechanism to move the particles. In some embodiments, particulate traps use centrifugal sedimentation. In some embodiments, particulate traps may include a tubular centrifuge, a multi-chamber centrifuge, a conical basket centrifuge, a volute-type centrifuge, a settling centrifuge, or a disc centrifuge. In some embodiments, particles are discharged continuously or intermittently from the centrifuge. In some embodiments, the particulate trap is a hydrocyclone. In some embodiments, the particulate trap is an array of hydrocyclones or centrifuges in series and / or parallel. In some embodiments, sumps are used to resuspend the ion exchange particles. In some embodiments, hydrocyclones may have multiple feed points. In some embodiments, a hydrocyclone is used upside down.In some embodiments, liquid is injected near the apex of a hydrocyclone cone to improve shear accuracy. In some embodiments, a weir rotates in the center of the particle trap with a feed of suspended ion exchange particles entering near the middle of the particle trap, and the ion exchange particles are trapped at the bottom and center of the particle trap due to a “teacup effect.” In some embodiments, the particle trap may use magnetic separation. In some embodiments, the ion exchange particles are magnetic. In some embodiments, acid-resistant magnetic particles, such as SiO2-coated magnetite or other coated or uncoated magnetic materials, are bonded to the surface of the ion exchange particles to enable magnetic separation. In some embodiments, the particle trap is a collection of particle traps with similar or different mechanisms. In some embodiments, particle traps based on gravity, magnetism, centrifugal forces, or combinations thereof, are located inside or outside the ion exchange reactor vessel. In some embodiments, the ion exchange particles are washed using countercurrent flows of the ion exchange particles and a washing liquid. In some embodiments, the ion exchange particles are treated with brine or acidic liquids using countercurrent flows of the ion exchange particles and the washing liquid. 2085695 of 53 liquids. In some embodiments, backwashing of solids is performed using a series of particle traps or separators. In some embodiments, the additional particle trap or separator is located at the end of the liquid flow of the countercurrent circuit to limit particle loss. In some embodiments, backwashing is used to minimize the use of fresh water. Staged flows One aspect of the invention described herein is a staged ion exchange reactor for extracting lithium from liquid resources, comprising: a) a tank containing ion exchange particles with associated particle traps; b) one or more tanks containing brine at various stages of delithiation; and c) one or more tanks containing acid at various stages of lithiation. One aspect of the invention described herein is a staged ion-exchange reactor for extracting lithium from liquid resources, comprising: a) a tank containing ion-exchange particles with associated particle traps; and b) one or more tanks containing brine in various stages of delithiation. One aspect of the invention described herein is a staged ion-exchange reactor for extracting lithium from liquid resources, comprising: a) a tank containing ion-exchange particles with associated particle traps; and b) one or more tanks containing acid in various lithiation stages. In some embodiments, the staged ion exchange reactor contacts hydrogen-saturated ion exchange particles with partially delithiated brine to maximize lithium recovery from the brine. In some embodiments, the staged ion exchange reactor contacts lithium-saturated ion exchange particles with partially lithiated acid to maximize the conversion of protons in the acid to lithium ions. In some embodiments, the staged ion exchange reactor contacts ion exchange particles that are nearly saturated with lithium with fresh brine to fully saturate the ion exchange particles with lithium and maximize lithium uptake by the particles. In some embodiments, the staged ion exchange reactor contacts ion exchange particles that are nearly saturated with protons with fresh acid to fully saturate the ion exchange particles with protons and maximize lithium elution from the particles. Exchange network In some embodiments, a plurality of ion exchange reactors are joined together to form an exchange network comprising brine circuits, 2085695 of 53 wash or acid circuits. In some embodiments of the brine circuit, brine flows through a first reactor in the brine circuit, then to a next reactor in the brine circuit, and so on, such that lithium is removed from the brine as the brine flows through one or more reactors. In some embodiments of the acid circuit, acid flows through a first reactor in the acid circuit, then to the next reactor in the acid circuit, and so on, such that lithium is eluted from the columns with acid to produce a lithium eluate. In some embodiments of the water wash circuit, water flows through a first reactor in the water wash circuit, then optionally to a next reactor in the water wash circuit, and so on, such that residual brine or other impurities are removed.In some embodiments, particle traps are used to retain ion exchange particles within individual reactors in a circuit. In some embodiments, particle traps are used to move ion exchange particles countercurrently through a series of reactors within the brine, wash, and / or acid circuits, or to move ion exchange particles between different circuits. In some embodiments of the exchange network, the ion exchange reactors are exchanged between the brine circuit, the water wash circuit, and the acid circuit. In some embodiments, the first reactor in the brine circuit is charged with lithium and then exchanged into the water wash circuit to remove residual brine. In some embodiments, the first reactor in the water wash circuit is washed to remove residual brine and then exchanged into the acid circuit, where the lithium is eluted with acid to form a lithium eluate. In some embodiments, the first reactor in the acid circuit is eluted with acid and then exchanged into the brine circuit to absorb lithium from the brine. In some embodiments, two water wash circuits are used to wash the reactors after the brine circuit and the acid circuit.In some embodiments of the column exchange reactor, only a water wash circuit is used to wash the columns after the brine circuit, while excess acid is neutralized with the base or washed from the reactors in the brine circuit. In some embodiments of the exchange network, the first reactor in the brine circuit is exchanged to become the last reactor in the water wash circuit. In some embodiments, the first reactor in the water wash circuit is exchanged to become the last reactor in the acid circuit. In some embodiments, the first reactor in the acid circuit is exchanged to become the last reactor. 2085695 of 53 reactor in the brine circuit or the last reactor in a water wash circuit for acid removal. Other aspects In some embodiments, brine flows through the reactor are operated in batch, semi-batch, semi-continuous, or continuous operation modes. In some embodiments, wash solution flows through the reactor are operated in batch, semi-continuous, or continuous operation modes. In some embodiments, acid solution flows through the reactor are operated in batch, semi-continuous, or continuous operation modes. In some embodiments, ion exchange particles are moved between a plurality of reactors. In some embodiments, the ion exchange particles move between a plurality of reactors in the opposite direction to the brine, wash solution, and acid flows. In some embodiments, air pumps, water pumps, or vacuum pumps are used to move water, brine, acid, slurries, or other solutions. In some embodiments, a vacuum system is used to move water, brine, acid, slurries, or other solutions. In some embodiments, one or more tanks, columns, or other vessels are pressurized to move water, brine, acid, slurries, or other solutions. In some embodiments, one or more tanks, columns, or other vessels are pressurized to move water, brine, acid, or other solutions through a filter, particle trap, or other solid-liquid separation apparatus. In some embodiments, a vacuum is applied to the filters in contact with the ion exchange material / fluid slurry to draw the fluid out of the reactor while leaving the ion exchange material inside the reactor.In some embodiments, a vacuum valve is installed approximately 6 inches from the filter within the line that closes when the filter is backwashed. In some embodiments, a vacuum valve is installed approximately 4 inches from the filter within the line that closes when the filter is backwashed. In some embodiments, a vacuum valve is installed approximately 8 inches from the filter within the line that closes when the filter is backwashed. In some embodiments, for backwashing, pressurized air is pumped through the filter to break up the cake on the other side of the filter. In some embodiments, to resume filtration of the slurry fluid, the vacuum valve is opened again to re-expose the filter to the vacuum.In some embodiments, a series of vacuum valves are used to minimize vacuum loss from the vacuum / drain lines. 2085695 of 53 In some embodiments, a wash solution is used to remove residual brine, residual acid, or other impurities from the ion exchange particles. In some embodiments, the wash solution is water, pH-adjusted water, an aqueous solution, or a non-aqueous solution. In some embodiments, the ion exchange particles are removed from the tank and loaded into a column where they are washed. In some embodiments, the ion exchange particles are removed from the tank and loaded into a column where they are washed to remove residual brine. In some embodiments, the ion exchange particles are removed from the tank and loaded into a column where they are washed to remove residual acid. In some embodiments, the ion exchange particles form a packed bed, a settled bed, a fluidized bed, or combinations thereof.In some embodiments, the ion exchange particles move between a tank and a column. In some embodiments, the ion exchange particles move between a tank where they are fluidized and a column where they form a packed or settled bed. In some embodiments, one or more columns are directly attached to one or more tanks. In some embodiments, one or more columns are mounted at the bottom of one or more tanks so that the ion exchange particles can settle from the tank into the column. In some embodiments, one or more columns are mounted at the bottom of one or more conical-bottom tanks so that the ion exchange particles can settle from the tank into the column.In some embodiments, one or more columns are mounted at the bottom of one or more tanks so that ion exchange particles can settle from the tank into the column under the force of gravity and / or with the flow of solution. In some embodiments, a wash solution containing EDTA, disodium EDTA, or other antiscalants is used to remove CaSO, MgSO, SrSO, BaSO, MgCO, CaCO, BaCO, SrCO, sulfate scale, carbonate scale, or other scale from the ion exchange reactor. In some embodiments, an antiscalant wash is performed before or after each brine, water, or acid treatment. In some embodiments, an antiscalant wash is performed after a number of ion exchange cycles that is less than about 10, less than about 50, or less than about 200. In some embodiments, the ion exchange particles are replaced from the reactor once the performance of these ion exchange particles has degraded in terms of lithium uptake capacity, lithium selectivity, lithium uptake kinetics, chemical stability, or mechanical stability. In some embodiments, the particles 2085695 of 53 ion exchange reactors are replaced in one or more ion exchange reactors in an ion exchange reactor network with minimal disruption to operations. In some embodiments, base is added to the ion exchange reactor before, during, or after lithium capture from a liquid resource. In some embodiments, base is added as a solution, as an aqueous solution, as a component of a slurry, or as a solid. The base serves to neutralize the release of protons by the ion exchange material and maintain the pH of the liquid resource within a range of about 5-7, about 3-8, or about 1-9. In some embodiments, the ion exchange reactor has a plunger, piston, or other mechanical device that compacts the ion exchange particles on a filter while forcing the liquid solution through the filter. In some embodiments, the ion exchange reactor is pressurized to force the fluid through the filter at a higher rate. In some embodiments, a vacuum is used on the effluent side of the filter to promote higher filtration rates. In some embodiments, the flows of liquid resources, wash solution, or acid solution are recirculated through an ion exchange reactor. In some embodiments, the recirculation of brine from the bottom of the reactor serves to create a fluidized bed, or partially fluidized bed, of ion exchange particles. In some embodiments, flows of acid, brine, water, or other solutions are injected into the bottom of the tank to fluidize or suspend the ion exchange particles from the bottom of the tank. In some embodiments, the flows of acid, brine, water, or other solutions are injected into the bottom of the tank and withdrawn at the top of the tank.In some embodiments, streams of acid, brine, water, or other solutions move as part of a reactor network and are injected into the bottom of the tank to fluidize or suspend ion exchange particles from the bottom of the tank. In some embodiments, streams of acid, brine, water, or other solutions move as part of a continuously or semi-continuously operating reactor network and are injected into the bottom of the tank to fluidize or suspend ion exchange particles from the bottom of the tank. In some embodiments, the ion exchange reactor is equipped with a spray system to wash the ion exchange particles from the internal surfaces of the tank and move the ion exchange particles to the bottom of the tank. In some embodiments, lithium is eluted from the ion exchange particles using acid added all at once, titrated to several aliquots of similar or different concentrations. In some embodiments, the elution of lithium from 2085695 of 53 ion exchange particles are controlled or monitored using pH measurement and acid titration. In some embodiments, acid is added to a slurry comprising water and ion exchange particles, and the concentration of acid added to the slurry is higher than the final acid concentration of the slurry after the acid is added. In some embodiments, pH changes in the brine, acid, or water solutions are monitored to synchronize lithium uptake, lithium elution, or washing processes. In some embodiments, the ion exchange particles are added or removed at the top or bottom of a tank or column in the ion exchange reactor. In some embodiments, the brine, water, or acid solutions are added or removed at the top or bottom of a tank or column in the ion exchange reactor. In some embodiments, the ion exchange particles are added to the top of a tank or column in the ion exchange reactor and may settle to the bottom. In some embodiments, the ion exchange particles are added to the top of a tank or column in the ion exchange reactor and may settle to the bottom as the brine moves up through the tank or column.In some embodiments, the ion exchange particles are added to the top of a tank or column in the ion exchange reactor and may settle to the bottom at a rate controlled by the upward flow of brine, water, or acid solutions being added to the bottom of the column and withdrawn from the top of the column. In some embodiments, the tank is composed of a material that is a polymer, a metal, a ceramic, an alloy, stainless steel, a plastic-coated alloy, an oxide-coated alloy, fiberglass, composite materials, or combinations thereof. In some embodiments, the tank is composed of PVDF, PE, PP, PVC, PTFE, other acid-resistant materials, or combinations thereof. In some embodiments, the pH of the brine resource decreases when the brine resource is contacted with the ion exchange particles due to lithium uptake and proton release by the ion exchange particles. In some embodiments, base is added to the liquid resource to control the pH in the range of about 5-7, about 4-8, or about 1-9. In some embodiments, base is added as a solid, as a slurry, as a liquid solution, or as an aqueous solution. In some embodiments, the base may comprise CaO, Ca(OH)2, Mg(OH)2, NaOH, KOH, Sr(OH)2, Ba(OH)2, or combinations thereof. 2085695 of 53 In some embodiments of the ion exchange reactor or reactor system, flocculants are used to aid in settling or separation. Ion exchange particles In some embodiments, the ion exchange particles are coated or uncoated ion exchange particles. In some embodiments, the ion exchange particles comprise an ion exchange material selected from the following list: LiFePO, LiMnPO, LiMnPO (M = Ti, Mn, Sn), LiTiO, LiMnO, Li.6Mn.6O, LiMO (M = Al, Cu, Ti), LiTiO, LiTiO, LiVO, LiSiO, LiCuPO, Al(OH), LiCl.xAl(OH),H2O, SnO.xSbO,H2O, TiO.xSbO,H2O, solid solutions thereof, and combinations thereof. In some embodiments, an ion exchange material comprises LiFePO4, Li2SnO3, Li2MnO3, Li2TiO3, Li4Ti5O12, Li4Mn5O12, Li1.6Mn1.6O4, solid solutions thereof, or combinations thereof. In some embodiments, the ion exchange particles have a coating comprising Nb2O5, Ta2O5, MoO2, TiO2, ZrO2, SnO2, SiO2, Li2O, Li2TiO3, Li2ZrO3, Li2MoO3, LiNbO3, LiTaO3, Li2SiO3, Li2Si2O5, Li2MnO3, ZrSiO4, AlPO4, LaPO4, ZrP2O7, MoP2O7, Mo2P3O12, BaSO4, AlF3, SiC, TiC, ZrC, Si3N4, ZrN, BN, carbon, graphitic carbon, amorphous carbon, hard carbon, diamond-like carbon, solid solutions thereof, or combinations thereof. In some embodiments, a coating material comprises TiO2, ZrO2, SiO2, Li2TiO3, Li2ZrO3, Li2MnO3, ZrSiO4, LiNbO3, or combinations thereof. In some embodiments, the ion exchange particles are porous, non-porous, or composite. In some embodiments, the ion exchange particles are comprised of a coated or uncoated ion exchange material incorporated into a matrix. In some embodiments, the matrix is ​​PVDF, polystyrene, another acid-resistant polymer, ceramic binder, silica binder, or combinations thereof. In another aspect, a coating material comprises a chloropolymer, a fluoropolymer, a chlorofluoropolymer, a hydrophilic polymer, a hydrophobic polymer, copolymers thereof, blends thereof, or combinations thereof. In a further aspect, a coating material comprises a copolymer, a block copolymer, a linear polymer, a branched polymer, a crosslinked polymer, a heat-treated polymer, a solution-processed polymer, copolymers thereof, blends thereof, or combinations thereof. In a further aspect, a coating material comprises polyethylene, low-density polyethylene, high-density polyethylene, polypropylene, polyester, polytetrafluoroethylene (PTFE), polyamide types, polyetheretherketone (PEEK), 2085695 of 53 polysulfone, polyvinylidene fluoride (PVDF), poly(4-vinyl pyridine-co-styrene (PVPCS), polystyrene (PS), polybutadiene, acrylonitrile butadiene styrene (ABS), polyvinyl chloride (PVC), polymer ethylene tetrafluoroethylene (ETFE), poly(chlorotrifluoroethylene) (PCTFE), ethylene chlorotrifluoro (Halar), polyvinyl fluoride (PVF), fluorinated ethylene-propylene (FEP), perfluorinated elastomer, chlorotrifluoroethylenevinylidene fluoride (FKM), perfluoropolyether (PFPE), perfluorosulfonic acid (Nafion), polyethylene oxide, polyethylene glycol, sodium polyacrylate, polyethylene-block-poly(ethylene glycol), polyacrylonitrile (PAN), polychloroprene (neoprene), polyvinyl butyral (PVB), expanded polystyrene (EPS), polydivinylbenzene, copolymers thereof, mixtures thereof, or combinations thereof.In a further aspect, a coating material comprises polyvinylidene fluoride (PVDF), polyvinyl chloride (PVC), ethylene chlorotrifluoroethylene (Halar), poly(4-vinyl pyridine-co-styrene) (PVPCS), polystyrene (PS), acrylonitrile butadiene styrene (ABS), expanded polystyrene (EPS), polyphenylene sulfide, sulfonated polymer, carboxylated polymer, other polymers, copolymers thereof, mixtures thereof, or combinations thereof. In some embodiments, the coated particle comprises an ion exchange material selected from the group consisting of LiFePO, LiSnO, LiMnO, LiTiO, LiTiO, LiMnO, Li.6Mn.6O, solid solutions thereof, or combinations thereof, and a coating material comprising TiO, ZrO, SiO, LiTiO, LiZrO, LiMnO, ZrSiO, LiNbO, polyvinylidene fluoride (PVDF), polyvinyl chloride (PVC), e.g., ethylene chlorotrifluoroethylene (Halar) (PS), acrylonitrile butadiene styrene (ABS), expanded polystyrene (EPS), polyphenylene sulfide, sulfonated polymer, carboxylated polymer, other polymers, copolymers thereof, mixtures thereof. same, or combinations thereof. In a further aspect, a coating is deposited on an ion exchange particle by dry mixing, solvent mixing, emulsification, extrusion, bubbling one solvent into another, casting, heating, evaporation, vacuum evaporation, spray drying, vapor deposition, chemical vapor deposition, microwaves, hydrothermal synthesis, polymerization, co-polymerization, crosslinking, irradiation, catalysis, foaming, other deposition methods, or combinations thereof. In a further aspect, a coating is deposited using a solvent comprising n-methyl-2-pyrrolidone, dimethyl sulfoxide, tetrahydrofuran, dimethylformamide, dimethylacetamide, methyl ethyl ketone, ethanol, acetone, other solvents, or combinations thereof. Liquid resource In some embodiments, the liquid resource is selected from the following list: a natural brine, a dissolved salar salt, a geothermal brine, seawater, water2085695 of 53 concentrated sea salt, desalination effluent, a concentrated brine, a processed brine, liquid from an ion exchange process, liquid from a solvent extraction process, a synthetic brine, ore leach, mineral leach, clay leach, recycled product leach, recycled material leach, or combinations thereof. In some embodiments, a liquid resource is selected from the following list: a natural brine, a dissolved salt marsh salt, a concentrated brine, a processed brine, a synthetic brine, a geothermal brine, liquid from an ion exchange process, liquid from a solvent extraction process, mineral leach, clay leach, recycled product leach, recycled material leach, or combinations thereof.In some embodiments, the liquid resource is optionally pretreated prior to entering the ion exchange reactor to remove suspended solids, hydrocarbons, organic molecules, or other chemical or ionic species. In some embodiments, the liquid resource is optionally fed into the ion exchange reactor without any pretreatment from its source. In some embodiments, the liquid resource is injected into a reservoir, salt flat, salt mine, basin, or other geological deposit after lithium has been removed from the liquid resource. In some embodiments, other species are recovered from the liquid resource before or after lithium recovery. In some embodiments, the pH of the liquid resource is adjusted before, during, or after lithium recovery. Processing of the eluate In some embodiments, the lithium eluate solution obtained from the ion exchange reactor is further processed into lithium chemicals selected from the following list: lithium sulfate, lithium chloride, lithium carbonate, lithium phosphate, lithium hydroxide, lithium metal, lithium metal oxide, lithium metal phosphate, lithium sulfide, or combinations thereof. In some embodiments, the lithium eluate solution obtained from the ion exchange reactor is further processed into lithium chemicals that are solid, aqueous, liquid, slurry, hydrated, or anhydrous. In some embodiments, the lithium eluate solution obtained from the ion exchange reactor is further processed using acid recovery, acid recycling, acid regeneration, distillation, reverse osmosis, evaporation, purification, chemical precipitation, membrane electrolysis, or combinations thereof. Methods An aspect of the invention described herein is a method for generating a lithium eluate solution from a liquid resource, comprising: providing an ion exchange reactor comprising a tank, ion exchange particles that absorb 2085695 of 53 selectively absorb lithium from a liquid resource and elute a lithium eluate solution when treated with an acidic solution after absorbing lithium ions from said liquid resource, one or more particle traps, and provision for modulating the pH of said liquid resource; flowing a liquid resource to said ion exchange reactor, thereby allowing said ion exchange particles to selectively absorb lithium from said liquid resource; treating said ion exchange particles with an acidic solution to produce said lithium eluate solution; and passing said lithium eluate solution through said one or more particle traps to collect said lithium eluate solution. An aspect of the invention described herein is a method for generating a lithium eluate solution from a liquid resource, comprising: providing an ion exchange reactor comprising (i) a conical shaped tank, wherein said conical shape allows said ion exchange particles to settle into a settled bed so that liquid can be removed from said settled bed; (ii) ion exchange particles that selectively adsorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acid solution after adsorbing lithium from said liquid resource; (iii) one or more particle traps located at the bottom of said tank, wherein said one or more particle traps comprise one or more meshes;and (iv) provision for modulating the pH of said liquid resource, wherein said modulation of said pH of said liquid resource is configured to take place in the tank or prior to injection of said liquid resource into the tank; flowing a liquid resource to said ion exchange reactor, thereby allowing said ion exchange particles to selectively adsorb lithium from said liquid resource; treating said ion exchange particles with an acidic solution to produce said lithium eluate solution; and passing said lithium eluate solution through said one or more particle traps to collect said lithium eluate solution. An aspect of the invention described herein is a method for generating a lithium eluate solution from a liquid resource, comprising: providing an ion exchange reactor comprising: (i) a conical shaped tank, wherein said conical shape allows said ion exchange particles to settle onto a settled bed so that liquid can be removed from said settled bed; (ii) ion exchange particles that selectively adsorb lithium from said liquid resource and elute said lithium eluate solution when treated with an acidic solution after adsorbing lithium from said liquid resource; (iii) one or more particle traps located at the bottom of said tank, wherein said one or more particle traps comprise multi-layered meshes;and (iv) provision for modulating the pH of said liquid resource, wherein said modulation of said pH of said liquid resource is configured to take place in the tank or prior to injection of; 2085695 of 53 said liquid resource in the tank; flowing a liquid resource to said ion exchange reactor, thereby allowing said ion exchange particles to selectively absorb lithium from said liquid resource; treating said ion exchange particles with an acid solution to produce said lithium eluate solution; and passing said lithium eluate solution through said one or more particle traps to collect said lithium eluate solution. In some embodiments, the tank is conical in shape. In some embodiments, the tank is partially conical in shape. In some embodiments, the conical shape allows the ion exchange particles to settle into a settled bed such that liquid can be removed from above the settled bed. In some embodiments, the partially conical shape allows the ion exchange particles to settle into a settled bed such that liquid can be removed from above the settled bed. In some embodiments, the pH modulation of the liquid resource occurs in the tank. In some embodiments, the pH modulation of the liquid resource occurs before injection into the tank. In some embodiments, one or more particulate traps comprise one or more filters within the tank. In some embodiments, one or more embodiments, one or more particle traps comprise a filter. comprise a filter. In some forms of In some embodiments, one or more particle traps comprise two filters. In some embodiments, one or more particle traps comprise three filters. In some embodiments, one or more particle traps comprise four filters. In some embodiments, one or more particle traps comprise five filters. In some embodiments, one or more traps are located at the bottom of the tank. In some embodiments, one or more traps are located near the bottom of the tank. In some embodiments, one or more traps are located above the bottom of the tank. In some embodiments, one or more particle traps comprise one or more meshes. In some embodiments, one or more particle traps comprise one mesh. In some embodiments, one or more particle traps comprise two meshes. In some embodiments, one or more particle traps comprise three meshes. In some embodiments, one or more particle traps comprise four meshes. In some embodiments, one or more particle traps comprise five meshes. In some embodiments, all meshes of one or more particle traps are identical. In some embodiments, at least one of the meshes of the one or more particle traps is not identical to the rest of the meshes of the one or more particle traps. 2085695 of 53 In some embodiments, one or more meshes comprise a pore space of less than about 200 microns, less than about 175 microns, less than about 150 microns, less than about 100 microns, less than about 75 microns, less than about 50 microns, less than about 25 microns, less than about 10 microns, more than about 1 micron, more than about 5 microns, more than about 10 microns, more than about 20 microns, more than about 30 microns, more than about 40 microns, more than about 50 microns, more than about 60 microns, more than about 70 microns, more than about 80 microns, more than about 90 microns, more than about 100 microns, more than approximately 125 micrometers, more than approximately 150 micrometers,more than about 175 micrometers from about 1 micrometer to about 200 micrometers, from about 5 micrometers to about 175 micrometers, from about 10 micrometers to about 150 micrometers, from about 10 micrometers to about 100 micrometers, from about 10 micrometers to about 90 micrometers, from about 10 micrometers to about 80 micrometers, from about 10 micrometers to about 70 micrometers, from about 10 micrometers to about 60 micrometers, or from about 10 micrometers to, approximately 50 micrometers. In some embodiments, one or more particulate traps comprise multi-layered meshes. In some embodiments, the multi-layered meshes comprise at least one finer mesh for filtration and at least one coarser mesh for structural support. In some embodiments, one or more particulate traps comprise one or more meshes supported by a structural support. In some embodiments, one or more particulate traps comprise one or more polymeric meshes. In some embodiments, the one or more polymeric meshes are selected from the group consisting of polyetheretherketone, ethylenetetrafluoroethylene, polyethylene terephthalate, polypropylene, and combinations thereof. In some embodiments, one or more particle traps comprise one or more meshes comprising a metal wire mesh. In some embodiments, the metal wire mesh is coated with a polymer. In some embodiments, the ion exchange reactor is configured to move said exchange particles. 2085695 of 53 ionic in one or more washing columns. In some embodiments, the ion exchange reactor is configured to allow ion exchange particles to settle in one or more washing columns. In some embodiments, the columns are fixed to the bottom of said tank. In some embodiments, the one or more particle traps comprise one or more filters mounted in one or more ports through the wall of said tank. In some embodiments, the one or more particulate traps comprise one or more filters external to said tank, and with provision for fluid communication between said one or more filters and said tank. In some embodiments, the one or more particulate traps comprise one or more gravity settling devices external to said tank, and with provision for fluid communication between said one or more gravity settling devices and said tank. In some embodiments, the one or more particle traps comprise one or more gravity settling devices internal to said tank. In some embodiments, the one or more particle traps comprise one or more centrifugal settling devices external to said tank, and with provision for fluid communication between said one or more centrifugal settling devices and said tank. In some embodiments, the one or more particle traps comprise one or more centrifugal settling devices internal to said tank.In some embodiments, the one or more particulate traps comprise one or more settling tanks, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more settling tanks, centrifugation devices, or combinations thereof, and said tank. In some embodiments, the one or more particulate traps comprise one or more screens, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more screens, centrifugation devices, or combinations thereof, and said tank.In some embodiments, the one or more particulate traps comprise one or more settling tanks, one or more screens, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more settling tanks, screens, or combinations thereof, and said tank. In some embodiments, the one or more particulate traps comprise one or more screens, one or more settling tanks, one or more centrifugation devices, or combinations thereof, external to said tank, and with provision for fluid communication between said one or more. 2085695 of 53 mesh, one or more sedimentation tanks, centrifugation devices, or combinations thereof, and said tank. In some embodiments, the ion exchange particles are agitated. In some embodiments, the ion exchange particles are agitated by a mixer. In some embodiments, the ion exchange particles are agitated by an impeller. In some embodiments, the ion exchange particles are fluidized by pumping a solution into the tank near the bottom of the tank. In some embodiments, the ion exchange particles are fluidized by pumping a solution from the tank back into the tank near the bottom of the tank. In some embodiments, the ion exchange particles are fluidized by pumping a slurry of ion exchange particles from near the bottom of the tank to a higher level in the tank. In some embodiments, the method further comprises one or more stepwise elution tanks, wherein intermediate eluate solutions comprising mixtures of protons and lithium ions are stored and further used to elute lithium from said freshly lithiated ion exchange particles. In some embodiments, the method further comprises one or more stepwise elution tanks, wherein intermediate eluate solutions comprising mixtures of protons and lithium ions are mixed with additional acid and further used to elute lithium from said ion exchange particles. In some embodiments, the ion exchange particles further comprise a coating material. In some embodiments, the coating material is a polymer. In some embodiments, the coating material comprises a chloropolymer, a fluoropolymer, a chlorofluoropolymer, a hydrophilic polymer, a hydrophobic polymer, copolymers thereof, mixtures thereof, or combinations thereof. EXAMPLES Example 1: Ion exchange reactor with conical bottom and mounted filters Lithium is extracted from a brine using coated ion exchange particles. The brine is an aqueous solution containing 50,000 mg / L Na, 20,000 mg / L Ca, 3,000 mg / L Mg, and 500 ppm Li. The coated ion exchange particles consist of an ion exchange material and a coating material. The ion exchange material is Li,Vln,O, and the coating material is ZrO. The particles consist of 96% by weight of active material and 4% by weight of coating material. The particles have an average diameter of 30 micrometers, and the coating thickness is 2085695 of 53 approximately 100 nm. The particles are created by first synthesizing Li4Mn5Üi2 by a solid-state method and then depositing the coating on the surface of the Li4Mn5Üi2 using Zr(IV) propoxide as a precursor. Ion exchange particles are loaded into an ion exchange reactor illustrated in FIG. 1. The ion exchange reactor comprises a conical tank (101), a 12 um PEEK mesh mounted on a flange in an opening in the tank wall such that the mesh is approximately flush with the tank wall (102) fitted to PVC pipe to allow fluid to flow in and out of the tank through the mesh while the ion exchange particles are retained within the tank, an overhead agitator (103), a pH controller (104), and a spray (non-spray) system on top of the tank with one or more nozzles positioned to spray water to wash the ion exchange particles off the sides of the tank and down to the bottom of the tank. The particles are loaded into the tank in an aqueous suspension. 1.5N H2SÜ4 acid is pumped into the tank through the PEEK mesh to create a slurry with H2SÜ4 at a normality of 0.75N. The acid is agitated with the ion exchange particle to produce Li2SÜ4 in solution. During the acid treatment, the particles absorb hydrogen while releasing lithium. The Li4Mn5Ü12 active material converts to a protonated state with a hydrogen-enriched composition. The ZrÜ2 coating allows diffusion of hydrogen and lithium, respectively, to and from the active material while providing a protective barrier that limits the dissolution of manganese and oxygen from the active material. After 40 minutes, the eluate solution is collected from the tank through the PEEK mesh for elemental analysis to measure the eluate composition. After acid treatment, the protonated particles are treated with brine, where they absorb lithium while releasing hydrogen. The brine is pumped into the tank through the PEEK mesh. The particles are converted from a protonated to a lithiated state with a lithium-enriched composition. An aqueous solution of NaOH is added to the tank to maintain the brine pH at 6°C. After 4 hours, the depleted brine is removed from the tank through the PEEK mesh. The ion-exchange particles are washed with water via a spray system. The particles are washed three times with water, and the water is drained from the tank through the PEEK mesh, leaving an aqueous suspension of the ion-exchange particles at the bottom of the tank. The lithiated material is then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle is repeated to extract the lithium from the brine and obtain a Li2SÜ4 solution. Dissolution and degradation of the active material in acid is limited because the coating provides a protective barrier. 2085695 of 53 The dissolution of the active material is measured through elemental analysis of the acid solution after shaking. After 25 ion exchange cycles, no measurable loss of lithium absorption capacity is observed in the ion exchange material, and lithium recovery from the brine solution is approximately 65% ​​for each cycle. Example 2: Ion exchange reactor with conical bottom and internal filters Lithium is extracted from a brine using coated ion exchange particles. The brine is an aqueous solution containing 50,000 mg / L Na, 20,000 mg / L Ca, 3,000 mg / L Mg, and 500 ppm Li. The coated ion exchange particles consist of an ion exchange material and a coating material. The ion exchange material is LiO2VImO and the coating material is SiO2. The particles consist of 94% by weight of active material and 6% by weight of coating material. The particles have an average diameter of 30 micrometers, and the coating thickness is approximately 400 nm. The particles are created by first synthesizing LiO2MmO by a solid-state method and then depositing the coating onto the surface of LiO2MnO using tetraethyl orthosilicate (TEOS) as a precursor. Ion exchange particles are loaded into an ion exchange reactor illustrated in FIG. 2. The ion exchange reactor comprises a conical tank (201), two internal candle filters comprising a 12 um PEEK mesh (202) attached to a PVC pipe to allow fluid to flow in and out of the tank through the mesh while the ion exchange particles are retained within the tank, an overhead agitator (203), a pH controller (204), and a spray (non-spray) system on top of the tank with one or more nozzles positioned to spray water to wash the ion exchange particles off the sides of the tank and down to the bottom of the tank. The particles are loaded into the tank in an aqueous suspension. 1.5N HCl acid is pumped into the tank through the PEEK mesh to create a slurry with HCl at a normal of 0.75N. The acid is agitated with the ion exchange particle to produce LiCl in solution. During the acid treatment, the particles absorb hydrogen while releasing lithium. The LiiMmOn active material converts to a protonated state with a hydrogen-enriched composition. The SiO2 coating allows diffusion of hydrogen and lithium, respectively, to and from the active material while providing a protective barrier that limits the dissolution of manganese and oxygen from the active material. After 40 minutes, the eluate solution is collected from the tank through the PEEK mesh for elemental analysis to measure the eluate composition. After acid treatment, the protonated particles are treated with brine, where the particles absorb lithium while releasing hydrogen. The brine is pumped to tank 39. 2085695 of 53 through an opening in the top of the tank. The particles are converted from a protonated to a lithiated state with a lithium-enriched composition. An aqueous NaOH solution is added to the tank to maintain the brine pH at 7 °C. After 6 hours, the spent brine is removed from the tank through the PEEK mesh. The ion-exchange particles are washed with water via the spray system. The particles are washed three times with water, and the water is drained from the tank through the PEEK mesh, leaving an aqueous suspension of the ion-exchange particles at the bottom of the tank. The lithiated material is then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle is repeated to extract the lithium from the brine and obtain a LiCl solution. Dissolution and degradation of the active material in acid is limited because the coating provides a protective barrier. Example 3: Ion exchange reactor with conical bottom and external filter Lithium is extracted from a brine using coated ion exchange particles. The brine is an aqueous solution containing 70,000 mg / L Na, 1,000 mg / L Ca, 5,000 mg / L Mg, and 200 ppm Li. The coated ion exchange particles consist of an ion exchange material and a coating material. The ion exchange material is Li(IV)Mn(5012) and the coating material is ZrO(2). The particles consist of 96% by weight of active material and 4% by weight of the coating. The particles have an average diameter of 30 micrometers, and the coating thickness is approximately 100 nm. The particles are created by first synthesizing Li(IV)Mn(5012) by a solid-state method and then depositing the coating onto the surface of the Li(IV)Mn(5012) using Zr(IV) propoxide as a precursor. Ion exchange particles are loaded into an ion exchange reactor illustrated in FIG. 3. The ion exchange reactor comprises a conical tank (301), an external settling tank (302) with an inlet taking diluted slurry from the tank and an outlet returning concentrated slurry to the tank and another outlet removing liquid from the system, an overhead agitator (303), a pH controller (304), and a spray (non-spray) system on top of the tank with one or more nozzles positioned to spray water to wash the ion exchange particles off the sides of the tank and down to the bottom of the tank. The particles are loaded into the tank in an aqueous suspension. 1.5N H2SO4 acid is pumped into the tank to create a suspension with H2SO4 at a normal content of 0.75N. The acid is agitated with the ion exchange particle to produce Li2SO4 in solution. During the acid treatment, the particles absorb hydrogen while releasing lithium. The active material Li2Mn5012 converts to a protonated state with a composition enriched by 40%. 2085695 of 53 hydrogen. The ZrO2 coating allows diffusion of hydrogen and lithium, respectively, to and from the active material while providing a protective barrier that limits the dissolution of manganese and oxygen from the active material. After 40 minutes, the eluate solution is collected from the tank via the settling tank for elemental analysis to measure the eluate composition. After acid treatment, the protonated particles are treated with brine, where the particles absorb lithium while releasing hydrogen. The particles are converted from a protonated to a lithiated state with a lithium-enriched composition. An aqueous solution of NaOH is added to the tank to maintain the brine pH at 6°C. After 4 hours, the depleted brine is removed from the tank via the settling tank. The ion-exchange particles are washed with water through the spray system. The particles are washed three times with water, and the water is drained from the tank via the settling tank, leaving a concentrated aqueous suspension of the ion-exchange particles at the bottom of the tank. The lithiated material is then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle is repeated to extract the lithium from the brine and obtain a Li2SÜ4 solution. Example 4: Ion exchange reactor with external sedimentation tank Lithium is extracted from a brine using ion exchange particles. The brine is an aqueous solution containing 70,000 mg / L of Na, 1,000 mg / L of Ca, 5,000 mg / L of Mg, and 200 ppm of Li. The ion exchange particles are composed of an ion exchange material called Li4Mn5Üi2. The particles have an average diameter of 30 micrometers. The Li4Mn5Üi2 is synthesized using a solid-state method. Ion exchange particles are loaded into an ion exchange reactor illustrated in FIG. 4. The ion exchange reactor comprises a cylindrical tank (401), an external settling tank (402) with an inlet taking diluted slurry from the tank and an outlet returning concentrated slurry to the tank and another outlet removing liquid from the system, an overhead agitator (403), a pH controller (404), and a spray (non-spray) system on top of the tank with one or more nozzles positioned to spray water to wash the ion exchange particles off the sides of the tank and down to the bottom of the tank. The particles are loaded into the tank in an aqueous suspension. 1.5N H2SÜ4 acid is pumped into the tank to create a suspension with H2SÜ4 at a normal content of 0.75N. The acid is agitated with the ion exchange particle to produce Li2SÜ4 in solution. During the acid treatment, the particles absorb hydrogen while releasing lithium. The material 41 2085695 of 53 active LÍ4Mn5Üi2 converts to a protonated state with a hydrogen-enriched composition. After 40 minutes, the eluate solution is collected from the tank via the settling tank for elemental analysis to measure the eluate composition. After acid treatment, the protonated particles are treated with brine, where the particles absorb lithium while releasing hydrogen. The particles are converted from a protonated to a lithiated state with a lithium-enriched composition. An aqueous solution of NaOH is added to the tank to maintain the brine pH at 6°C. After 4 hours, the depleted brine is removed from the tank via the settling tank. The ion-exchange particles are washed with water through the spray system. The particles are washed three times with water, and the water is drained from the tank via the settling tank, leaving a concentrated aqueous suspension of the ion-exchange particles at the bottom of the tank. The lithiated material is then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle is repeated to extract the lithium from the brine and obtain a Li₂S₄ solution. Example 5: Ion exchange system with external filters Lithium is extracted from a brine using ion exchange particles. The brine is an aqueous solution containing 70,000 mg / L of Na, 1,000 mg / L of Ca, 5,000 mg / L of Mg, and 200 ppm of Li. The ion exchange particles are composed of an ion exchange material called Li4Mn5Üi2. The particles have an average diameter of 30 micrometers. The Li4Mn5Üi2 is synthesized using a solid-state method. Ion exchange particles are loaded into an ion exchange reactor illustrated in FIG. 5. The ion exchange reactor comprises a larger cylindrical brine tank for brine mixing and water washing (501), a smaller cylindrical acid tank for acid mixing (502), a settling tank for removing liquid from the acid tank (503), a settling tank for removing liquid from the brine tank (504), and a settling tank for moving the ion exchange particles between the acid tank and the brine tank (505) while removing water to form a more concentrated slurry prior to acid elution.Each tank is equipped with an overhead agitator, a pH controller (not shown), and a spray system (not shown) on top of the tank with one or more nozzles positioned to spray water to wash the ion exchange particles from the sides of the tank and to the bottom of the tank. The particles are loaded into the acid tank in an aqueous suspension. 1.5N HCl acid is pumped into the tank to create a suspension with HCl at a normal concentration of 0.75N HCl. 2085695 of 53 The acid is agitated with the ion exchange particles to produce LiCl in solution. During the acid treatment, the particles absorb hydrogen while releasing lithium. The active material LiCl: is converted to a protonated state with a hydrogen-enriched composition. After 30 minutes, the suspension of acid eluate and ion exchange particles is separated into a concentrated suspension and an eluate solution using an external settling tank (503). The concentrated suspension is re-injected into the acid tank for washing. The suspension is then washed with water using the external settling tank (503) to remove most of the water. The suspension is then transferred to the brine tank using an external settling tank (505) while removing some water containing residual acid. In the brine tank, the protonated particles are treated with brine, where the particles absorb lithium while releasing hydrogen. The particles are converted from a protonated state to a lithiated state with a lithium-enriched composition. An aqueous suspension of Ca(OH)2 is added to the tank to maintain the brine pH at 7 °C. After 6 hours, the spent brine is removed from the tank through the sedimentation tank (504), while the ion exchange particles are returned to the brine tank. The ion exchange particles are washed with water through the spray system. The particles are washed three times with water and the water is removed using the external sedimentation tank (504) connected to the brine tank, leaving an aqueous suspension of the ion exchange particles at the bottom of the tank.The slurry is then moved to the acid tank through an external settling tank (505) while excess water is removed to increase the concentration of the slurry being loaded into the acid tank. The lithiated material is then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle is repeated to extract the lithium from the brine and obtain a LiCl solution. Example 6: Ion exchange system with multiple brine reactors sharing an acid reactor Lithium is extracted from a brine using ion exchange particles. The brine is an aqueous solution containing 60,000 mg / L of Na, 20,000 mg / L of Ca, 5,000 mg / L of Mg, and 120 ppm of Li. The ion exchange particles are composed of an ion exchange material called LiMnO. The particles have an average diameter of 40 micrometers. IiMnO is synthesized using a solid-state method. Ion exchange particles are loaded into an ion exchange system illustrated in FIG. 6. The ion exchange system comprises four brine reactors. 2085695 of 53 for brine mixing and water washing (601, 602, 603, 604) with large conical tanks incorporating internal candle filters, overhead stirrers and pH controllers; and an acid reactor for acid elution (605) with a smaller conical tank incorporating internal candle filters and an overhead stirrer. Each tank is equipped with a spray system on top of the tank with one or more nozzles positioned to spray the wash solution to wash the ion exchange particles from the sides of the tanks and to the bottom of the tanks while removing soluble species from the tank. In the brine tanks, the protonated particles are treated with brine, where the particles absorb lithium while releasing hydrogen. The particles are converted from a protonated state to a lithiated state with a lithium-enriched composition. An aqueous suspension of Ca(OH)2 is added to the tank to maintain the brine pH at 6.5°C. Lithium uptake from the brine is staggered across reactors, with each brine reactor initiating lithium uptake approximately two hours after the next. After each brine reactor has agitated the ion-exchange particles in brine for eight hours, the depleted brine is removed through candle filters. The ion-exchange particles are then washed five times with water, where the water is removed through the candle filters. The remaining water and ion-exchange particle suspension are then transferred to the acid reactor. The particles are loaded into the acid tank in an aqueous slurry. 1.5N HCl acid is pumped into the tank to create a slurry with HCl at a normal of 0.75N. During the elution process, an additional 1.5N HCl acid solution is added to encourage further elution of lithium from the ion exchange particles. The acid is agitated with the ion exchange particle to produce a LiCl eluate solution. During the acid treatment, the particles absorb hydrogen while releasing lithium. The active material Li4Mn5O2 is converted to a protonated state with a hydrogen-enriched composition. After 45 minutes, the acid eluate is removed through candle filters and sent to an eluate processing unit to form battery-grade lithium carbonate. The remaining acid slurry is washed with water once, and the water is removed through the candle filters. The slurry is then transferred to the brine tank.After the slurry has been transferred back to the brine tank, the next brine reactor is washed and the slurry from that next brine reactor is transferred to the acid reactor for elution. Example 7: Continuous ion exchange system with multiple reactors Lithium is extracted from a brine using ion exchange particles. The brine is an aqueous solution containing 70,000 mg / L of Na, 30,000 mg / L of Ca, 4,000 mg / L of Nitrogen, and 2,000 mg / L of Nitrogen. 2085695 of 53 Mg, and 80 ppm Li. The ion-exchange particles are composed of an ion-exchange material called LiMrOc. The particles have an average diameter of 30 micrometers. LiMmOc is synthesized using a solid-state method. Ion exchange particles are loaded into an ion exchange system illustrated in FIG. 7. The ion exchange system comprises a brine circuit comprising four brine reactors for brine mixing and water washing (701, 702, 703, 704) incorporating large conical tanks, external settling tanks, overhead stirrers, and pH controllers; a water wash circuit; and an acid circuit comprising two acid reactors for acid elution (705, 706) incorporating smaller conical tanks, external settling tanks, and overhead stirrers. Each tank is equipped with a spray system at the top of the tank with one or more nozzles positioned to spray the aqueous wash solution to wash the ion exchange particles from the sides of the tanks and to the bottom of the tanks. In the brine tanks, the protonated particles are treated with brine, where the particles absorb lithium while releasing hydrogen. The particles are converted from a protonated state to a lithiated state with a lithium-enriched composition. An aqueous suspension of Ca(OH)2 is added to the tank to maintain the brine pH at 6.5°C. The brine flows continuously through the series of four brine reactors as the ion exchange particles flow countercurrently. The ion exchange particles move in an aqueous suspension. The brine and ion exchange particles are separated using external settling tanks. The correct relative velocities of brine and ion exchange particles through the system are maintained by reinjecting the brine or ion exchange particles back into a reactor from which they are removed as needed.When the ion exchange particles reach the end of the brine circuit, they are transferred to a water wash circuit where the residual brine is removed from the particles. After washing, excess water is removed through a filter to form a concentrated slurry, which is then transferred to the acid circuit. The particles are then transferred to the acid circuit. The particles move through the acid circuit while the acid solution enters the acid circuit at the other end and moves through the acid circuit in a countercurrent direction. External settling tanks are used to separate the ion-exchange particles from the acid eluate. 1.5 N HCl acid is pumped into the tank where the acid solution enters the acid circuit to create a slurry with HCl at a normal level of 0.75 N. The ion-exchange particles release lithium into the acid solution to form an acid-eluate solution. 2085695 of 53 The eluate-acid solution is transferred to the next acid reactor, where the eluate-acid solution is further converted into an eluate solution. The eluate solution is removed from the acid circuit and processed to form battery-grade lithium hydroxide by membrane electrolysis. The ion-exchange particles exiting the acid circuit are washed in a scrubbing circuit and returned to the start of the brine circuit. Example 8: Ion exchange reactor with step elution Lithium is extracted from a brine using coated ion exchange particles. The brine is an aqueous solution containing 70,000 mg / L Na, 12,000 mg / L Ca, 3,000 mg / L Mg, and 200 ppm Li. The coated ion exchange particles consist of an ion exchange material and a coating material. The ion exchange material is I.i.iVIibOi: ​​and the coating material is SiO2. The particles consist of 94% by weight of active material and 6% by weight of coating material. The particles have an average diameter of 30 micrometers, and the coating thickness is approximately 400 nm. The particles are created by first synthesizing I.i.iVIibOi: ​​by a solid-state method and then depositing the coating onto the surface of LiiMn5Oi2 using (TEOS) as the precursor. Ion exchange particles are loaded into an ion exchange system illustrated in FIG. 8. The ion exchange system comprises an ion exchange reactor (801) comprising a plurality of internal candle filters with 12 um PEEK mesh secured to PVC pipe to allow fluid to flow in and out of the tank through the mesh while retaining the ion exchange particles within the tank, an overhead agitator, a pH controller, and a spray system on top of the tank with multiple nozzles for spraying water to wash the ion exchange particles from the sides of the tank and to the bottom of the tank; an acid feed tank (802); and a staged eluate tank (803). The reactor is operated as described in Example 2, but during elution, the ion exchange particles that are saturated with lithium are first eluted with an eluate-acid solution that is an approximately 50 / 50 mixture of lithium ions and protons so that the eluate-acid solution becomes an eluate solution with 90% lithium ions and only 10% protons, maximizing the conversion of the protons to lithium ions. The eluate solution is removed from the tank and further processed into battery grade lithium hydroxide. Fresh acid then flows into the tank, becomes an eluate-acid solution that is an approximately 50 / 50 mixture of lithium ions and protons, and this eluate-acid solution then flows to the eluate tank in stages for storage until the next elution step. The ion exchange particles are washed with water, 46 2085695 of 53 are treated with brine with pH controlled at 6.5, washed with water again and then returned to elution as described above. Example 9: Ion exchange reactor Lithium was extracted from a brine using coated ion-exchange particles. The brine was an aqueous solution containing 100,000 mg / L of Na and 300 ppm of Li. The particles consisted of 85% by weight of active material and 15% by weight of coating material. The particles had an average diameter of 40 micrometers. Ion exchange particles were loaded into an ion exchange reactor illustrated in FIG. 9A. The ion exchange reactor comprised a conical bottom tank (901), a 12 micron pore size polyetheretherketone screen mounted at the bottom of the conical bottom tank (902) to allow fluid to be pumped in and out of the tank through the screen while retaining the ion exchange particles within the tank, an overhead agitator (903), a pH controller (904), an internal filter comprising a 35 micron pore size polyetheretherketone screen (905), and a spray system (not shown) at the top of the tank with one or more nozzles located to spray water to wash the ion exchange particles off the sides of the tank and down to the bottom of the tank. The particles were loaded into the tank as dry material. 2.0 N HCl acid was pumped into the tank and agitated with the ion exchange particle to produce a LiCl eluate solution. During the acid treatment, the particles absorbed hydrogen while releasing lithium. The active material converted to a protonated state with a hydrogen-enriched composition. The coating allowed diffusion of hydrogen and lithium, respectively, to and from the active material while providing a protective barrier. After 40 minutes, the eluate solution was collected from the tank through the meshes, dehydrated, purified using sodium carbonate precipitation and resin ion exchange beads to remove trace Mg / Ca, and processed into lithium carbonate through the addition of sodium carbonate solution at 90 degrees Celsius. After acid treatment, the protonated particles were treated with brine, where the particles absorbed lithium while releasing hydrogen. The brine was pumped into the tank and agitated with the ion exchange particles, and the particles were converted from a protonated state to a lithiated state with a lithium-enriched composition. An aqueous NaOH solution was added to the tank to maintain the brine pH at 6 °C. After 4 hours, the depleted brine was removed from the tank through the screens. The ion exchange particles were then washed with water through the spray system. The particles were washed 2085695 of 53 three times with water and the water drained from the tank through the screens, leaving a wet bed of ion exchange particles at the bottom of the tank with low water content. The lithiated material was then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle was repeated to extract lithium from the brine and obtain a LiCl solution. Degradation of the ion exchange particles was limited because the coating provides a protective barrier. FIG. 9B shows the lithium recovery (the amount of lithium produced in the LiCl solution as a percentage of the total lithium in the brine) from the brine over multiple cycles between brine and acid. Example 10: Ion exchange reactor with attached column Lithium is extracted from a brine using coated ion exchange particles. The brine is an aqueous chloride solution containing 100,000 mg / L Na, 200 ppm Li, and other species including Ca, Mg, and B. The coated ion exchange particles comprise an ion exchange material and a coating material. The ion exchange material is Li₁₆MnO, and the coating material is titanium dioxide. The particles consist of 95% by weight of active material and 5% by weight of coating material. The particles have an average diameter of 200 micrometers. The particles are created by first synthesizing Li₂MnO using a solid-state method, and then the coating is deposited from a Tipropoxide precursor onto the surface of the Li₂MnO material. Ion exchange particles are loaded into an ion exchange reactor illustrated in FIG. 10. The ion exchange reactor comprises a conical bottom tank with a thinner cylindrical column connected to and mounted at the bottom of the conical bottom tank (1001), a 100 um polypropylene mesh mounted at the bottom of the column (1002) to allow fluid to be pumped in and out of the tank through the mesh while the ion exchange particles are retained within the tank, an overhead agitator (1003), a pH controller (1004), an internal filter comprising a 100 micron pore size polypropylene mesh (1005), and a spray system (not shown) at the top of the tank with one or more nozzles positioned to spray water to wash the ion exchange particles off the sides of the tank and down to the bottom of the tank. The particles are loaded into the tank as dry material. 1.5 N sulfuric acid is pumped into the tank and stirred with the ion exchange particle to produce a lithium sulfate eluate solution. During the acid treatment, the particles absorb hydrogen. 2085695 of 53 while releasing lithium. The coating allows diffusion of hydrogen and lithium, respectively, to and from the active material while providing a protective barrier that protects the active material. After 40 minutes, the eluate solution is collected from the tank through the mesh, dehydrated, purified using sodium carbonate precipitation and resin ion exchange beads to remove trace Mg / Ca, and processed into lithium carbonate through the addition of a sodium carbonate solution at 90 degrees Celsius. After acid treatment, the protonated particles are treated with brine, where the particles absorb lithium while releasing hydrogen. The brine is pumped into the tank and agitated with the ion exchange particles, and the particles are converted from a protonated to a lithiated state with a lithium-enriched composition. An aqueous NaOH solution is added to the tank to maintain the brine pH at 6°C. After 4 hours, the spent brine is removed from the tank through the screens. The ion exchange particles form a settled bed in the column. The ion exchange particles are continuously washed with water, which flows through the column to efficiently remove residual brine from the ion exchange particles.After washing, the residual wash water is drained from the bottom of the column through the mesh, leaving a wet bed of ion exchange particles at the bottom of the column with minimal brine carryover and minimal water carryover. The lithiated material is then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle is repeated to extract the lithium from the brine and obtain a lithium sulfate solution. Degradation of the ion exchange particles is limited because the coating provides a protective barrier. Example 11: Ion exchange reactor with attached column and fluidizing pump Lithium is extracted from a brine using ion exchange particles. The brine is an aqueous chloride solution containing 60,000 mg / L of Ca, 100 ppm of Li, and other species including Na, Mg, and B. The coated ion exchange particles comprise an active ion exchange material and a polymer coating. The particles have an average diameter of 30 micrometers. Ion exchange particles are loaded into an ion exchange reactor illustrated in FIG. 11. The ion exchange reactor comprises a conical bottom tank with a thinner cylindrical column connected to and mounted at the bottom of the conical bottom tank (1101), a polymer coated steel mesh with a pore size of 5 microns mounted at the bottom of the column (1102) to allow fluid to be pumped in and out of the tank through the mesh while the ion exchange particles are pumped into the tank. 2085695 of 53 ionic are retained within the tank, an overhead stirrer (1103), a pH controller (1104), a pumping unit for pumping the liquid out of the tank and back to the bottom of the column (1105) where the inlets and outlets of the pumping unit are covered with a polymer coated steel mesh with a pore size of 5 microns, an internal filter comprising a polymer coated steel mesh with a pore size of 5 microns (1106), and a spray system (not shown) on top of the tank with one or more nozzles positioned to spray water to wash the ion exchange particles from the sides of the tank and down to the bottom of the tank. The particles are loaded into the tank as dry material. 1.0 N hydrochloric acid is pumped into the tank and agitated with the ion exchange particle to produce a lithium chloride eluate solution. During the acid treatment, the particles absorb hydrogen while releasing lithium. After 10 minutes, the eluate solution is collected from the tank through the mesh, dehydrated, purified using sodium carbonate precipitation and resin ion exchange beads to remove trace Mg / Ca, and processed into lithium carbonate through the addition of a sodium carbonate solution at 90 degrees Celsius. After acid treatment, the protonated particles are treated with brine, where the particles absorb lithium while releasing hydrogen. The brine is pumped into the tank and agitated with the ion exchange particles. While the tank is agitated, brine is pumped from the tank by the pumping unit and injected into the bottom of the column to fluidize any particles that settle on the column and suspend the particles in the agitated brine in the tank. The particles are converted from a protonated state to a lithiated state with a lithium-enriched composition. An aqueous suspension of Ca(OH)2 is added to the tank to maintain the brine pH at 6°C. After 3 hours, the spent brine is removed from the tank through the screens. The ion exchange particles form a settled bed in the column.The ion exchange particles are continuously washed with water, which flows through the column to efficiently remove residual brine from the ion exchange particles. After washing, the residual wash water drains from the bottom of the column through the screens, leaving a wet bed of ion exchange particles at the bottom of the column with minimal brine carryover and minimal water carryover. The lithiated material is then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle is repeated to extract the lithium from the brine and obtain a lithium chloride solution. Degradation of the ion exchange particles is limited because the coating provides a protective barrier. 2085695 of 53 Example 12: Ion exchange reactor with fluidizing pump Lithium is extracted from a brine using coated ion exchange particles. The brine is an aqueous solution containing 100,000 mg / L of Na and 500 ppm of Li. The coated ion exchange particles consist of an ion exchange material and a coating material. The ion exchange material is Li4Ti5O12 and the coating material is TiO2. The particles consist of 90% by weight of active material and 10% by weight of coating material. The particles have an average diameter of 80 micrometers. The particles are created by first synthesizing Li4Ti5O12 and then the coating is deposited on the surface of the Li4Ti5O12 material. Ion exchange particles are loaded into an ion exchange reactor illustrated in FIG. 12. The ion exchange reactor comprised a conical bottom tank (1201), a 35 micron pore size polyetheretherketone mesh mounted on the bottom of the conical bottom tank (1202) to allow fluid to be pumped in and out of the tank through the mesh while the ion exchange particles are retained within the tank, an overhead agitator (1203), a pH controller (1204), an internal filter comprising a 35 micron pore size polyetheretherketone mesh (1206), a pumping unit for pumping liquid out of the tank and back to the bottom of the tank (1205) where the inlets and outlets of the pumping unit are covered with a 35 micron pore size polyetheretherketone mesh,and a spray system (not shown) on top of the tank with one or more nozzles located to spray water to wash the ion exchange particles off the sides of the tank and down to the bottom of the tank. The particles are loaded into the tank as dry material. 1.5 N HCl acid is pumped into the tank and agitated with the ion exchange particle to produce a LiCl eluate solution. During the acid treatment, the particles absorb hydrogen while releasing lithium. The LiCl active material is converted to a protonated state with a hydrogen-enriched composition. The coating allows diffusion of hydrogen and lithium, respectively, to and from the active material while providing a protective barrier that protects the active material. After 15 minutes, the eluate solution is collected from the tank through the meshes, dehydrated, purified using sodium carbonate precipitation and resin ion exchange beads to remove trace Mg / Ca, and processed into lithium carbonate through the addition of sodium carbonate solution at 90 degrees Celsius. After acid treatment, the protonated particles are treated with brine, where they absorb lithium while releasing hydrogen. The brine is pumped into the tank. 2085695 of 53 and stirred with the ion exchange particles, the particles convert from a protonated state to a lithiated state with a lithium-enriched composition. An aqueous NaOH solution is added to the tank to maintain the brine pH at 6 °C. After 4 hours, the spent brine is removed from the tank through the screens. The ion exchange particles are washed with water through the spray system. The particles are washed three times with water, and the water is drained from the tank through the screens, leaving a wet bed of ion exchange particles at the bottom of the tank with low water content. The lithiated material is then treated again with acid to produce lithium in solution as described above. The protonation and lithiation cycle is repeated to extract the lithium from the brine and obtain a LiCl solution. Degradation of the ion exchange particles is limited due to the coating, which provides a protective barrier. 2085695 of 53 CLARKE MODET & CO. (ARGENTINA) SA - 30540437455 Digitally signed by PORTALTRAMITES - INPI Date: 2022.12.15 12:28:58 -03:00 Reason: Digitally signed by the INPI Location: Buenos Aires, Argentina 2085695

Claims

1. A method for generating a lithium eluate solution from a liquid resource, characterized in that it comprises: a) using an ion exchange system comprising one or more tanks and ion exchange particles, wherein the ion exchange particles selectively absorb lithium from a liquid resource and elute a lithium eluate solution when treated with an acidic solution after absorbing lithium ions from said liquid resource, one or more particle traps, and provision for modulating the pH of said liquid resource; b) flowing a liquid resource into said ion exchange system, thereby enabling said ion exchange particles to selectively absorb lithium from said liquid resource; c) treating said ion exchange particles with an acidic solution to produce said lithium eluate solution;(yd) passing said lithium eluate solution through said particle traps to collect said lithium eluate solution, wherein said particle traps are configured to (i) retain the ion exchange particles while allowing flows of said liquid resource, said lithium eluate solution, water, or said acid solution; or (ii) recirculate the ion exchange particles while allowing flows of said liquid resource, said lithium eluate solution, water, or said acid solution. 64 Claims follow;