WO2018145142A1 - Procédé de traitement combiné incorporant une électrolyse pour solutions contenant du lithium - Google Patents

Procédé de traitement combiné incorporant une électrolyse pour solutions contenant du lithium Download PDF

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WO2018145142A1
WO2018145142A1 PCT/AU2017/050100 AU2017050100W WO2018145142A1 WO 2018145142 A1 WO2018145142 A1 WO 2018145142A1 AU 2017050100 W AU2017050100 W AU 2017050100W WO 2018145142 A1 WO2018145142 A1 WO 2018145142A1
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lithium
solution
brine
adsorbent
sorbent
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Christopher John Reed
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Inneovation Pty Ltd
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Inneovation Pty Ltd
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Priority to ARP170103203A priority patent/AR110169A1/es
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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
    • C22B3/24—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition by adsorption on solid substances, e.g. by extraction with solid resins
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/10—Obtaining alkali metals
    • C22B26/12—Obtaining lithium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
    • B01D67/0002—Organic membrane manufacture
    • B01D67/0004—Organic membrane manufacture by agglomeration of particles
    • B01D67/00046—Organic membrane manufacture by agglomeration of particles by deposition by filtration through a support or base layer
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
    • B01D67/0081—After-treatment of organic or inorganic membranes
    • B01D67/0093—Chemical modification
    • B01D67/00931—Chemical modification by introduction of specific groups after membrane formation, e.g. by grafting
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/10—Supported membranes; Membrane supports
    • B01D69/107—Organic support material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/12—Composite membranes; Ultra-thin membranes
    • B01D69/1213—Laminated layers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/02—Inorganic material
    • B01D71/021—Carbon
    • B01D71/0211—Graphene or derivates thereof
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D15/00—Lithium compounds
    • C01D15/02—Oxides; Hydroxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D15/00—Lithium compounds
    • C01D15/04—Halides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G23/00—Compounds of titanium
    • C01G23/003—Titanates
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G23/00—Compounds of titanium
    • C01G23/003—Titanates
    • C01G23/005—Alkali titanates
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/14—Alkali metal compounds
    • C25B1/16—Hydroxides
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
    • C25B1/46—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis in diaphragm cells
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2684—Electrochemical processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2325/00—Details relating to properties of membranes
    • B01D2325/04—Characteristic thickness
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2325/00—Details relating to properties of membranes
    • B01D2325/16—Membrane materials having positively charged functional groups
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2002/00—Crystal-structural characteristics
    • C01P2002/70—Crystal-structural characteristics defined by measured X-ray, neutron or electron diffraction data
    • C01P2002/72—Crystal-structural characteristics defined by measured X-ray, neutron or electron diffraction data by d-values or two theta-values, e.g. as X-ray diagram
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2004/00—Particle morphology
    • C01P2004/01—Particle morphology depicted by an image
    • C01P2004/04—Particle morphology depicted by an image obtained by TEM, STEM, STM or AFM
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2004/00—Particle morphology
    • C01P2004/10—Particle morphology extending in one dimension, e.g. needle-like
    • C01P2004/13—Nanotubes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/12—Surface area
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present invention relates to a combined processing method incorporating electrolysis for lithium containing solutions.
  • the method of the present invention is intended for use in the extraction of lithium chloride from a lithium containing brine.
  • the extraction of lithium chloride from a lithium containing brine is achieved through the combined action of an adsorbent and/or a filter utilising a graphene based filter medium, with an electrolysis step.
  • the adsorbent is derived from titanium dioxide, and in the form of either sodium titanate (Na 2 Ti 3 O 7 ) or hydrogen titanate (H 2 TiO 3 ).
  • the present invention still further relates to a process for the purification of a lithium chloride solution obtained through either adsorption of lithium on an adsorbent, such as sodium titanate or hydrogen titanate, and/or filtration using a graphene based filter medium, combined with an electrolysis step, to prepare high purity lithium chloride solution for use in battery applications.
  • an adsorbent such as sodium titanate or hydrogen titanate
  • a graphene based filter medium combined with an electrolysis step
  • the graphene based filter medium employed in the process of the present invention is particularly, in one form, graphene oxide (GO) or reduced graphene oxide (rGO). It is envisaged that the graphene based filter medium acts as an ion sieve, allowing ions with smaller sizes than those of the channels to permeate while blocking all other larger species. In this manner it is understood that the graphene based filter medium rejects impurities such as K, Na and Mg, allowing the purification of a LiCI containing solution.
  • the electrolysis step is intended to provide a lithium hydroxide monohydrate product.
  • Lithium salts have widespread commercial application. They are used in the production of lithium metal, lithium carbonate and lithium hydroxide monohydrate for various battery applications. Due to the requirement for high purity in many of these applications, particularly when used as a cathode material in lithium ion batteries, there is an ever increasing need for high purity lithium chloride.
  • lithium chloride from a brine source is purified by solar evaporation technology to concentrate the brine solution and thereby remove sodium and potassium impurities.
  • Other impurities such as boron, may be removed by solvent extraction technology, whereas calcium, magnesium and other similar impurities may be removed by increasing the pH of the brine solution. This is typically achieved through the addition of lime and the formation and precipitation of insoluble salts, including calcium carbonate. This is very time consuming and highly dependent on the weather.
  • a purification means is needed to remove the majority of the impurities from a LiCI solution derived from a brine source, such that the concentration of each impurity is reduced to less than about 20 ppm.
  • An impurity concentration of less than about 20 ppm makes the resulting LiCI solution suitable for use in lithium metal extraction or the preparation of other lithium compounds, including lithium carbonate and lithium hydroxide monohydrate, for use in lithium ion battery applications.
  • the processes of the present invention have as one object thereof to overcome substantially one or more of the above mentioned problems associated with prior art, or to at least provide a useful alternative thereto.
  • brine or brines, or variations thereof, is to be understood to include a solution of alkali and/or alkaline earth metal salt(s) in water, of a natural or possibly industrial source.
  • concentrations of the various salts can vary widely.
  • the ions present in brine may include a combination of one or more of a monovalent cation, such as lithium, multivalent cations, monovalent anions, and multivalent anions.
  • high purity lithium chloride is to be understood, unless the context requires otherwise, as requiring any impurity present to be present in amounts of less than about 20 ppm.
  • graphene graphene sheet or graphene material
  • FLG few layer graphene
  • graphene nano-platelets graphene nanotubes
  • graphene nanotubes graphene
  • nanoribbons graphene nano-sheets and the like.
  • processing method for the purification of lithium containing solutions comprising the method steps of: a) passing a lithium containing solution to one or more purification steps to
  • step a) passing the substantially purified lithium chloride solution of step a) to an
  • the electrolysis step in which a lithium hydroxide product is produced, wherein the one or more purification steps comprises either or both of a first purification step in which the lithium containing solution is contacted with a titanate adsorbent whereby lithium ions are adsorbed thereon whilst rejecting substantially all other cations, the recovery of the lithium from the adsorbent providing a part-purified lithium containing solution, and a second purification step in which a graphene based filter medium is utilised to provide a further purified lithium containing solution.
  • the lithium containing solution is a lithium containing brine.
  • the part-purified lithium containing solution produced in the first purification step is passed in whole or part to the second purification step.
  • the adsorbent is provided in the form of either a hydrated titanium dioxide or a sodium titanate.
  • the hydrated titanium dioxide is produced from titanium dioxide.
  • the process in turn produces a substantially pure lithium chloride solution.
  • the brine preferably contains impurities from the group of sodium, potassium, magnesium, calcium and borate.
  • the impurity concentration of the substantially pure lithium chloride solution does not exceed about 20 ppm.
  • the brine contains lithium in the range of about 500 to 1500 ppm, and impurities including magnesium in the range of about 0.15% to 0.30%, calcium in the range of about 0.05% to 0.1 %, sodium in the range of about 8 to 10%, potassium in the range of about 0.7% to 1 .0%, and borate in the range of about 0.15% to 0.20%.
  • the brine contains about 700 ppm lithium, about 0.19% magnesium, about 0.09% calcium, about 8.8% sodium, about 0.8% potassium and about 0.18% borate.
  • the brine solution is preferably adjusted to a pH of 7 through the addition of a base.
  • the base is preferably provided in the form of sodium hydroxide.
  • the contact between the brine solution and the adsorbent preferably takes place at or about room or ambient temperature.
  • the brine is collected into a vessel and cooled to room temperature prior to its exposure to the adsorbent.
  • room temperature is understood to be between about 20°C to 28°C.
  • the contact or residence time between the brine solution and the adsorbent is between about 4 to 24 hours.
  • the contact or residence time between the brine solution and the adsorbent is: a) between about 8 to 24 hours; b) between about 20 to 24 hours; or c) between about 8 to 16 hours.
  • the recovery of lithium from the adsorbent is achieved through the regeneration of the adsorbent by the addition of an acid solution and the adsorbed lithium is extracted to provide the part purified lithium containing solution.
  • the acid solution is a solution of hydrochloric acid.
  • the amount of lithium extracted from the adsorbent through exposure to the acid solution is greater than about 90%. Yet still preferably, the amount of lithium extracted from the adsorbent through exposure to the acid solution is about 100% of the adsorbed lithium.
  • the graphene based filter medium of the second purification step preferably comprises a graphene membrane formed of one or more graphene, graphene oxide and/or reduced graphene oxide and to which the part-purified lithium containing solution is presented.
  • the passing of lithium containing solution to the second purification step produces a filtrate or permeate that is enriched in relative terms in lithium ions, providing the further purified lithium containing solution.
  • the second purification step is conducted under pressure.
  • the pressure may be 10 bar.
  • the further purified lithium containing solution is suitable is suitable for use in the production of battery grade lithium chemicals.
  • the graphene is provided as a graphene oxide membrane formed in turn from graphite oxide powder.
  • the graphene oxide membrane may preferably be supported on a first support that is in turn located in an aperture of a second support.
  • the first support is an anodic alumina disc.
  • the second support is a copper plate.
  • the graphene is provided as a reduced graphene oxide membrane.
  • the graphene oxide membrane may preferably be reduced by way of exposure to ascorbic acid.
  • the area used for pressure filtration is preferably about 1 - 2 cm 2 .
  • the membranes may be further supported by a porous substrate.
  • the porous substrate may be provided in the form of polyether sulfone (PES).
  • an adhesive material is applied to the porous substrate to increase the bond between the substrate and the graphene material.
  • the adhesive material is provided in the form of a polymer.
  • the polymer is a positively charged polymer.
  • the positively charged polymer is polydiallyldimethulammonium chloride.
  • the graphene membrane has a thickness of between 30 to 200 nm. Still preferably, the thickness of the graphene membrane is 150 to 200 nm.
  • the salt rejection achieved by the second purification step is 20% or greater as measured by the conductivity of the permeate relative to that of the part- purified lithium containing solution.
  • lithium is the least rejected ion or salt of the second purification step.
  • the first and second purification steps may comprise one or more stages, passes or repeats of contact or exposure between the lithium containing solution passed to them and the adsorbent or filter medium, respectively.
  • the lithium hydroxide product produced in the electrolysis step is passed to a crystallisation step in which lithium hydroxide monohydrate is crystallised.
  • the electrolysis step is preferably conducted by passing the substantially purified lithium solution to one or more electrolytic cells or electrolysers to convert the lithium present to lithium hydroxide.
  • substantially only lithium chloride and water are consumed in the electrolysis step, thereby producing substantially only lithium hydroxide, chlorine and hydrogen as products.
  • electrolysers are preferably provided in the electrolysis step.
  • the chlorine and hydrogen produced in the electrolysis step are preferably combined to produce HCI acid.
  • the electrolysis step of the present invention is conducted using chlor-alkali technology at about or less than 50oC and a current efficiency of greater than about 70%.
  • the titanate adsorbent is provided in the form of sodium titanate (Na2Ti 3 O7) and hydrogen titanate (H 2 TiO3).
  • the titanate adsorbent formed in accordance with this process is suitable for the extraction of lithium from a lithium containing solution.
  • the lithium containing solution may be a brine.
  • the brine may contain impurities from the group of sodium, potassium, magnesium, calcium and borate.
  • Figure 1 is an XRD pattern of a pristine TiO 2 powder
  • Figure 2 is a TEM image of pristine Ti0 2 ;
  • Figure 3 is an XRD Pattern of a Na 2 Ti 3 O 7 prepared at 120°C;
  • Figure 4 is an XRD Pattern of an Na2Ti3O7 prepared at 150°C;
  • Figure 5 is a an XRD Pattern of Na 2 Ti 3 O 7 prepared at 1 80°C;
  • Figure 6 is a TEM image of Na 2 Ti 3 O 7 Prepared at 120°C;
  • Figure 9 is the XRD patterns of Li 2 TiO 3 and H 2 TiO 3 as per Example 3;
  • Figure 10 is a TEM image of Li 2 TiO 3 ;
  • Figure 1 1 is a TEM image of H 2 TiO 3 ;
  • Figure 12 is an XRD pattern of Na 2 Ti 3 O 7 (Synthesised at 120°C) after Adsorption Test;
  • Figure 13 is an XRD pattern of Na 2 Ti 3 O 7 (Synthesised at 120°C) after Adsorption Test;
  • Figure 14 is a TEM image of Na 2 Ti 3 O 7 (Synthesised at 120°C) after Adsorption Test
  • Figure 15 is an XRD pattern of Na2 ⁇ n 3 O7 (Synthesised at 150°C) after Adsorption Test
  • Figure 16 is an XRD pattern of Na 2 Ti 3 O 7 (Synthesised at 150°C) after Adsorption Test;
  • Figure 17 is TEM image of Na2Ti 3 O 7 (Synthesised at 150°C) after Adsorption Test;
  • Figure 18 is an XRD pattern of Na 2 Ti 3 O 7 (Synthesised at 180°C) after Adsorption Test;
  • Figure 19 is an XRD pattern of Na2Ti 3 O 7 (Synthesised at 180°C) after Adsorption Test;
  • Figure 20 is TEM image of Na 2 Ti 3 O 7 (Synthesised at 180°C) after Adsorption Test;
  • Figure 21 is a kinetic adsorption test of sodium titanate Na 2 Ti 3 O 7 sorbent synthesizes at 150°C in 100 ml brine solution (-300 ppm Li);
  • Figure 22 is a kinetic adsorption test of sodium titanate Na 2 Ti 3 O 7 sorbent synthesizes at 150°C in 100 ml brine solution (-300 ppm Li);
  • Figures 23(a) to 23(d) are the XRD characterisations for sodium titanate
  • Figure 24 shows BET surface areas of sodium titanate synthesizes at 120°C, 150°C and 180°C observed before and after adsorption
  • Figure 25 shows the kinetics of 3g sodium titanate sorbent prepared at 150°C (Na 2 Ti 3 O 7 150) for 100 imL brine solution with different concentrations of Li + ions and at different times of adsorption;
  • Figure 26 shows the kinetics of 10g sodium titanate sorbent prepared at 150°C (Na 2 Ti 3 O 7 150) for 100 imL brine solution with different concentrations of Li + ions and at different times of adsorption;
  • Figure 27 shows an increased in amount of sorbent to 100 g/100 mL of brine solution (sorbent prepared at 150°C - Na2 ⁇ n 3 O7 150) for different concentrations of Li + ions and at different times of adsorption;
  • Figure 28 shows the results of the kinetic adsorption tests of hydrogen titanate sorbent (H2T1O3) in sorbent to solution ratio: 3g - 100ml_ brine solution (-300 ppm Li);
  • Figure 29 shows the results of the kinetic adsorption tests of hydrogen titanate sorbent (H 2 TiO 3 ) in sorbent to solution ratio: 10g - 100ml_ brine solution (-300 ppm Li);
  • Figure 30 shows the results of the kinetic adsorption tests of hydrogen titanate sorbent (H 2 TiO 3 ) in sorbent to solution ratio: 100g - l OOOmL brine solution (-300 ppm Li);
  • Figure 31 shows XRD data of the sorbent hydrogen titanate sorbent (H 2 TiO 3 ) before and after adsorption at different times;
  • Figure 32 shows BET surface area data of the sorbent hydrogen titanate sorbent (H2T1O3) before and after adsorption;
  • Figure 33 shows the reaction kinetics of 3 g hydrogen titanate sorbent (H 2 TiO 3 ), 100 mL brine solution with different concentrations of with different
  • Figure 34 shows the reaction kinetics of 10 g hydrogen titanate sorbent (H2T1O3), 100 mL brine solution with different concentrations of with different
  • Figure 35 shows the reaction kinetics of 100 g hydrogen titanate sorbent
  • Figure 36 shows the results of kinetic desorption testing for TNT-120
  • Figure 37 shows the results of kinetic desorption testing for TNT-150
  • Figure 38 shows the results of kinetic desorption testing for TNT-180;
  • Figure 39 shows the desorption data for hydrogen titanate sorbent (H2T1O3) ;
  • Figure 40 shows XRD patterns of TNT-120 sorbent after adsorption in 300 ppm Li + solution
  • Figure 41 shows XRD patterns of TNT-150 sorbent after adsorption in 300 ppm Li + solution
  • Figure 42 shows XRD patterns of TNT-180 sorbent after adsorption in 300 ppm Li + solution
  • Figure 43 shows XRD patterns of H 2 TiO 3 sorbent after adsorption in 300 ppm Li + solution
  • Figure 44 shows TEM images of TNT-120 sorbents after desorption with 0.05M HCI at 25 °C;
  • Figure 45 shows TEM images of TNT-150 sorbents after desorption with 0.05M HCI at 25 °C;
  • Figure 46 shows TEM images of TNT-180 sorbents after desorption with 0.05M HCI at 25 °C;
  • Figure 47 shows TEM images of H2T1O3 sorbents after desorption with 0.05M HCI at 25 °C;
  • Figure 48 shows Na + and CI " ion permeation through a GO membrane
  • Figure 49 shows the filtration performance of modified GO membranes with different thickness (Figure 49a) and different reduction time (Figure 49b);
  • Figure 50 shows the concentration of salts in a brine solution before and after filtration through a modified GO membrane, where the Y-axis - log scale and S1 and S2 represent data from two different membranes, the membrane used being 200 nm thick and 30 minute rGO;
  • Figure 51 shows the current efficiency data based on caustic collection and gas analysis for the electrolysis step
  • Figure 52 shows the cell voltage results, and the LiOH concentration exiting the cell during each run, for the electrolysis step of Figure 51 ;
  • Figure 53 shows the DC energy consumption data for the electrolysis step of Figure 51 .
  • the present invention provides a combined processing method for the purification of lithium containing solutions, the method comprising the method steps of : a) passing a lithium containing solution to one or more purification steps to produce a substantially purified lithium chloride solution; and b) passing the substantially purified lithium chloride solution of step a) to an electrolysis step in which lithium hydroxide monohydrate is produced, wherein the one or more purification steps comprises either or both of a first purification step in which the lithium containing solution is contacted with a titanate adsorbent whereby lithium ions are adsorbed thereon whilst rejecting substantially all other cations, the recovery of lithium from the adsorbent providing a part-purified lithium containing solution, and a second purification step in which a graphene based filter medium is utilised to provide a further purified lithium containing solution.
  • the part-purified lithium containing solution produced in the first purification step is passed in whole or part to the second
  • the lithium containing solution is a lithium containing brine.
  • the brine to be treated initially contains impurities from the group of sodium, potassium, magnesium, calcium and borate.
  • the brine contains lithium in the range of about 500 to 1500 ppm, and impurities including magnesium in the range of about 0.15% to 0.30%, calcium in the range of about 0.05% to 0.1 %, sodium in the range of about 8 to 10%, potassium in the range of about 0.7% to 1 .0%, and borate in the range of about 0.15% to 0.20%.
  • the brine contains about 700 ppm lithium, about 0.19% magnesium, about 0.09% calcium, about 8.8% sodium, about 0.8% potassium and about 0.18% borate.
  • the adsorbent is provided in the form of either a hydrated titanium dioxide or a sodium titanate.
  • the hydrated titanium dioxide is produced from titanium dioxide.
  • the process in turn produces a substantially pure lithium chloride solution.
  • the impurity concentration of the substantially pure lithium chloride solution does not exceed about 20 ppm.
  • the brine solution is preferably adjusted to a pH of 7 through the addition of a base.
  • the base is preferably provided in the form of sodium hydroxide.
  • the contact between the brine solution and the adsorbent preferably takes place at or about room or ambient temperature.
  • Room temperature is understood to be between about 20°C to 28°C.
  • the brine is collected into a vessel and cooled to room temperature prior to its exposure to the adsorbent.
  • the contact or residence time between the brine solution and the adsorbent is between about 4 to 24 hours.
  • the contact or residence time between the brine solution and the adsorbent is: a) between about 8 to 24 hours; b) between about 20 to 24 hours; or c) between about 8 to 16 hours.
  • the recovery of lithium from the adsorbent is achieved through the regeneration of the adsorbent by the addition of an acid solution and the adsorbed lithium is extracted to provide the part purified lithium containing solution.
  • the acid solution is a solution of hydrochloric acid.
  • the amount of lithium extracted from the adsorbent through exposure to the acid solution is greater than about 90%.
  • the amount of lithium extracted from the adsorbent through exposure to the acid solution is about 100% of the adsorbed lithium.
  • the graphene based filter medium of the second purification step comprises a graphene membrane formed of one or more graphene, graphene oxide and/or reduced graphene oxide and to which the part-purified lithium containing solution is presented.
  • the second purification step is conducted under pressure.
  • the pressure may be at or about 10 bar.
  • the further purified lithium containing solution is suitable is suitable for use in the production of battery grade lithium chemicals.
  • the graphene is provided as a graphene oxide membrane formed in turn from graphite oxide powder.
  • the graphene oxide membrane may be supported on a first support that is in turn located in an aperture of a second support.
  • the first support is, for example, an anodic alumina disc.
  • the second support is, for example, a copper plate.
  • the graphene is provided as a reduced graphene oxide membrane.
  • the graphene oxide membrane may be reduced by way of exposure to ascorbic acid.
  • the area used for pressure filtration is about 1 - 2 cm 2 .
  • the membranes may be further supported by a porous substrate.
  • the porous substrate may be provided in the form of polyether sulfone (PES).
  • PES polyether sulfone
  • An adhesive material may applied to the porous substrate to increase the bond between the substrate and the graphene material.
  • the adhesive material is, for example, provided in the form of a polymer.
  • the polymer is, in one form, a positively charged polymer, for example polydiallyldimethulammonium chloride.
  • the graphene membrane may have a thickness of between 30 to 200 nm.
  • the thickness of the graphene membrane is 150 to 200 nm.
  • the level of salt rejection achieved by the second purification step is 20% or greater as measured by the conductivity of the permeate relative to that of the part- purified lithium containing solution. Lithium is the least rejected ion or salt of the second purification step.
  • the first and second purification steps may comprise one or more stages, passes or repeats of contact or exposure between the lithium containing solution passed to them and to the adsorbent or filter medium, respectively.
  • the electrolysis step is conducted by passing the substantially purified lithium solution, for example a lithium chloride solution, to one or more electrolytic cells or electrolysers to convert the lithium present, for example present as lithium chloride, to lithium hydroxide.
  • the substantially purified lithium solution for example a lithium chloride solution
  • electrolytic cells or electrolysers to convert the lithium present, for example present as lithium chloride, to lithium hydroxide.
  • 6 to 20 electrolysers may be provided, in which substantially only lithium chloride and water are consumed, thereby producing substantially only lithium hydroxide, chlorine and hydrogen as products.
  • the chlorine and hydrogen so produced may be combined to produce HCI acid for use elsewhere bringing potential efficiencies and potential cost savings.
  • the electrolysis step is conducted using chlor-alkali technology at about or less than 50°C. This has been found by the Applicants to provide a current efficiency of greater than about 70%, for example 75%. The relatively low temperature and high current efficiency is understood to be due to the quality or purity of the substantially purified lithium solution being fed to the electrolysers of the electrolysis step. Both identified advantages bring beneficial cost implications. It is noted elsewhere that the purification steps of the present invention are capable of reduced impurity levels in lithium containing solutions to levels of less than 20 ppm. [0081 ] The lithium hydroxide product produced in the electrolysis step is passed to a crystallisation step in which lithium hydroxide monohydrate is crystallised.
  • the present invention further provides a process for the synthesis of a titanate adsorbent.
  • the titanate adsorbent is provided in the form of sodium titanate (Na 2 Ti 3 O 7 ) and hydrogen titanate (H2T1O3).
  • the titanate adsorbent formed in accordance with this process is suitable for the extraction of lithium from a lithium containing solution.
  • the lithium containing solution may be a brine.
  • the brine may contain impurities from the group of sodium, potassium, magnesium, calcium and borate.
  • T1O2 (Anatase type) powder was mixed with 3L NaOH solution (10 mol/L), and kept stirring for 2 hours, then transferred to 5L autoclave and react at each of 1 20°C, 1 50°C, and 1 80°C for 48 h. Resulting Na 2 Ti 3 O 7 nano-tubes were washed using vacuum filtration until pH of filtrate was 7. The product weight after drying at 100°C was 175 g. This produced high purity Na2Ti 3 O 7 nanotubes (over 95% product are tubes); the nanotubes have the largest specific surface area of 232 m 2 /g.
  • the sodium titanate was characterized by powder X-ray diffraction (XRD) and transmission electron microscopy (TEM) to confirm the morphological phase and structure.
  • XRD powder X-ray diffraction
  • TEM transmission electron microscopy
  • FIG. 1 there is shown the XRD pattern of the pristine TiO2 powder. This suggests that TiO2 material contained mainly rutile (R) TiO2 m ixed with some anatase (A) phase.
  • Figure 2 there is shown a TEM image of pristine TiO 2 is shown. It can be seen that the diameter of the TiO 2 particles is around 100-200 nm.
  • the XRD patterns of the Na-titanate exhibit apparent difference from the pristine TiO 2 powder.
  • the XRD patterns of these samples are in good agreement with that of monoclinic Na 2 Ti 3 O 7 phase.
  • Na 2 Ti 3 O 7 samples prepared at different temperatures 120°C, 150°C and 180°C are provided below.
  • Anatase type TiO 2 (15.0 g, Ti 0.187 mole) and Li 2 CO 3 (13.9 g, Li 0.376 mole) were mixed, ground and heated in an alumina crucible at a rate of ca. 6°C/min in air up to 700°C and maintained for the next 4 h. After cooling to room temperature, the solid powder (Li 2 TiO 3 ) was treated with 0.2 M HCI solution with occasional shaking for 24 h at room temperature (5 g of solid in 1 L acid). The solid was separated by filtration, washed with deionized water until the filtrate was neutral and allowed to dry at room temperature to obtain the H 2 TiO 3 . [0099] The precursor (Li 2 TiO3) and (H2T1O3) sorbent was prepared through solid calcination method. XRD patterns of precursor and H2T1O3 sorbent matches the known literature.
  • TEM analysis indicates that H 2 TiO 3 sorbent is mostly round shape nanoparticles and nano-rods with average size 200-400 nm. Li 2 TiO3 precursor exhibits similar structure as H2T1O3 sorbent suggesting that acid treatment has negligible impact on the morphology of the sorbent.
  • a brine solution the composition of which is described in the table below ( ⁇ 300 ppm Li), was chosen for the adsorption tests.
  • the kinetics of lithium adsorption by sodium titanate was determined by sampling the brine during adsorption at time intervals of 5min, 15min, 30min, 1 hr, 2hr, 3hr, 4hr, 5hr, 6hr, 7hr, 8hr, 9hr, 10hr, 1 1 hr, 12hr, 24hr (16 sampling times).
  • the adsorption kinetics for all 9 sodium titanate sorbents was determined using brine solution of similar composition and no buffer. Analytical characterisation was done by ICP, XRD and BET methods on selected samples.
  • Na 2 Ti 3 O 7 (1 50 U C) shows the best results on Li uptake at 1 .42mg/ g of sorbent in 1 00 imL brine solution adsorbed for 2 hours.
  • Na 2 Ti 3 O 7 120 and Na 2 Ti 3 O 7 180 show much lower Li + uptake equilibrium below 1 .5 mg/g at those concentrations of Li in brine.
  • Li adsorption kinetics for H 2 TiO 3 sorbents was determined by sampling the brine during adsorption at time intervals of 5min, 15min, 30min, 1 hr, 2hr, 3hr, 4hr, 5hr, 6hr, 7hr, 8hr, 9hr, 10hr, 1 1 hr, 12hr, 24hr (16 sampling times).
  • the adsorption kinetics for H 2 TiO 3 sorbents was determined using just 300 ppm Li brine solution.
  • FIGS. 28 to 30 show the results of the kinetic adsorption tests of hydrogen titanate sorbent (H 2 TiO3) in different sorbent to solution ratio: 3g - 100ml_, 10g - l OOimL, and 100g - l OOOmL brine solution (-300 ppm Li), respectively.
  • H 2 TiO3 hydrogen titanate sorbent
  • Figure 31 shows XRD data of the sorbent hydrogen titanate sorbent (H 2 TiO 3 ) before and after adsorption at different times.
  • Figure 32 shows BET surface area data of the sorbent hydrogen titanate sorbent (H 2 TiO 3 ) before and after adsorption.
  • H 2 TiO 3 sorbent reaches the Li + uptake equilibrium of 4.4 mg/g at Li + concentration of 500 ppm when dispersed 3 g sorbent into 100 ml brine solution. Neither increasing nor decreasing Li + concentration leads to reduced Li + uptake capacity. Increase the sorbent amount to 10 g, the uptake equilibrium is decreased to 2.8 mg/g.
  • the sorption capacity is rather low up to 1 .3 mg/g only.
  • Figure 33 shows the reaction kinetics of 3 g hydrogen titanate sorbent (H 2 TiO 3 ), 100 imL brine solution with different concentrations of with different
  • Figure 34 shows the reaction kinetics of 10 g hydrogen titanate sorbent (H 2 TiO 3 ), 100 imL brine solution with different concentrations of with different
  • Figure 35 shows the reaction kinetics of 100 g hydrogen titanate sorbent (H2T1O3), 1000 imL brine solution with different concentrations of with different concentrations of Li + ions.
  • the higher concentration of HCI recovery solution exhibited the higher recovery amount of Li + from the used sodium titanate synthesized at 120°C (TNT 120).
  • the elevated desorption temperature 60°C is able to increase the Li + recovery, but not significantly.
  • the triangles are desorption data over time using 0.05 M HCI solution at 25°C.
  • the squares are desorption data over time using 0.05 M HCI solution at 60°C.
  • the diamonds are desorption data over time using 0.1 M HCI solution at 25°C.
  • the inverted triangles are desorption data over time using 0.1 M HCI solution at 60°C.
  • the Li + recovery amount from TNT-150 sorbent is the highest (1 .4 mg/g) during all samples used for this recovery test.
  • the higher concentration of HCI recovery solution exhibited the higher recovery amount of Li + from the used TNT-150 sorbents, as shown in Figure 37.
  • the elevated desorption temperature 60°C is able to increase the Li + recovery significantly, this is quite different from the other recovered samples.
  • the triangles are desorption data over time using 0.05 M HCI solution at 25°C.
  • the squares are desorption data over time using 0.05 M HCI solution at 60°C.
  • the diamonds are desorption data over time using 0.1 M HCI solution at 25°C.
  • the inverted triangles are desorption data over time using 0.1 M HCI solution at 60°C.
  • the elevated desorption temperature (60°C) did not show a clear increase of Li + recovery.
  • the triangles are desorption data over time using 0.05 M HCI solution at 25°C.
  • the squares are desorption data over time using 0.05 M HCI solution at 60°C.
  • the diamonds are desorption data over time using 0.1 M HCI solution at 25°C.
  • the inverted triangles are desorption data over time using 0.1 M HCI solution at 60°C.
  • Figure 39 shows kinetic desorption test of H 2 TiO 4 sorbent after adsorption in brine solution.
  • the triangles are desorption data over time using 0.05 M HCI solution at 25°C; the squares are desorption data over time using 0.05 M HCI solution at 60°C; the diamonds are desorption data over time using 0.1 M HCI solution at 25°C; the inverted triangles are desorption data over time using 0.1 M HCI solution at 60°C.
  • Figure 40 shows XRD patterns of TNT-120 sorbent after adsorption in 300 ppm Li + solution. From the bottom, the first line is original TNT-120. The second line is TNT-120 after desorption using 0.05 M HCI solution at 25°C. The third line is TNT-120 after desorption using 0.1 M HCI solution at 25°C. The fourth line is TNT-120 after desorption using 0.05 M HCI solution at 60°C. The top line TNT-120 after desorption using 0.1 M HCI solution at 60°C.
  • Figure 41 shows the XRD patterns of TNT-150 sorbent after adsorption in 300 ppm Li + solution. Reading from the bottom, the first line is original TNT-150. The second line is TNT-150 after desorption using 0.05 M HCI solution at 25°C. The third line is TNT-150 after desorption using 0.1 M HCI solution at 25°C. The fourth line is TNT-150 after desorption using 0.05 M HCI solution at 60°C. The top line TNT-150 after desorption using 0.1 M HCI solution at 60°C.
  • Figure 42 shows the XRD patterns of TNT-180 sorbent after adsorption in 300 ppm Li + solution. Reading from the bottom, the first line is the original TNT-180. The second line is TNT-180 after desorption using 0.05 M HCI solution at 25°C. The third line is TNT-180 after desorption using 0.1 M HCI solution at 25°C. The fourth line is TNT-180 after desorption using 0.05 M HCI solution at 60°C. The top line is TNT-180 after desorption using 0.1 M HCI solution at 60°C.
  • Figure 43 shows the XRD patterns of H2T1O3 sorbent after adsorption in 300 ppm Li + solution. Reading from the bottom up, the first line is the original H2T1O3. The second line is H 2 TiO 3 after desorption using 0.05 M HCI solution at 25°C. The third line is H 2 TiO 3 after desorption using 0.1 M HCI solution at 25°C. The fourth line is H 2 TiO 3 after desorption using 0.05 M HCI solution at 60°C. The fifth line is H 2 TiO 3 after desorption using 0.1 M HCI solution at 60°C.
  • TEM images of TNT-120 sorbents after desorption with 0.05M HCI at 25 °C are shown in Figure 44.
  • the comparison of sorbent morphology before and after desorption indicates that the Li+ recovery process does not show significant impact on the nanofiber.
  • TEM images of TNT-120 sorbent after desorption with 0.05M HCI at 25 °C under different resolution (a) 50 nm, (b) 100 nm, (c) 200 nm, (d) 500 nm are shown.
  • EM images of TNT-150 sorbents after desorption with 0.05M HCI at 25 °C are shown in Figure 45.
  • the comparison of sorbent morphology before and after desorption indicates that the Li + recovery process does not show significant impact on the nanofiber.
  • TEM images of TNT-150 sorbent after desorption with 0.05M HCI at 25 °C under different resolution (a) 50 nm, (b) 100 nm, (c) 200 nm, (d) 500 nm are shown.
  • Both sodium titanate (Na 2 Ti 3 O 7 ) and hydrogen titanate (H 2 TiO 3 ) are, as noted above, preferred forms of the adsorbents used in the process of the present invention.
  • Suitable sodium titanate (Na 2 Ti 3 O 7 ) and/or hydrogen titanate (H 2 TiO 3 ) were synthesised as per methods described above.
  • the function of the adsorbent material in the process of the present invention without being limited by theory, is to absorb lithium ions from the LiCI brine and thereby rejecting the impurities, including competing cations.
  • the adsorbent (Na2Ti 3 O7 and/or H2T1O3) used in this embodiment of the present invention may advantageously be placed in a series of column. Further, the adsorbent may be placed in a series of columns and the brine solution may be directed through this series of columns. In other preferred embodiments the adsorbent columns may be placed before the brine solution.
  • the lithium containing brine with the composition stated above was placed in a beaker.
  • the adsorbent Na 2 Ti 3 O 7 or H 2 TiO 3
  • the amount of adsorbent top pack in the series of columns to treat a particular brine was selected to adsorb maximum Li from the brine in provided series of columns as per data obtained from our R&D and stated above.
  • An appropriate apparatus to be used in carrying out the first purification step of the present invention may be any manifold system whereby a lithium containing brine can be delivered to a series of columns containing an adsorbent and then ultimately collected in a receiving vessel.
  • the apparatus may also have a means for drawing aliquots of LiCI for analysis.
  • Such means may be a sample port comprising a resilient septum affixed in line to the apparatus.
  • the apparatus may be composed of several vessels such as glass flasks, ceramic containers, metal containers or other typical non-reactive chemical reaction vessels. The vessels may be connected using non-reactive polymeric tubing, metal pipe or tube, or glass pipe or tube.
  • the apparatus may be sectioned off using any type of valve stopcock or clamp depending on the composition of the tubing or piping.
  • the combined processing method for the purification of lithium containing solutions of the present invention further provides a method for the purification of semi- pure or part-purified LiCI solution obtained as may be produced as described above from a brine by using an adsorbent.
  • the combined processing method further comprises passing the semi-pure LiCI solution obtained after desorption of adsorbent to a graphene based filter medium, for example a graphene based membrane.
  • the graphene based membrane is, in one form, prepared from graphene oxide (GO) or reduced graphene oxide (rGO), which allows appropriate permeation through the membrane.
  • Graphene oxide dispersion is prepared by the ultra-sonication of graphite oxide powder in water and subsequent centrifugation.
  • a first support for example an anodic alumina disc
  • a membrane is then glued onto a second support, for example a copper plate having a 2 cm aperture provided in the centre thereof, for the conduct of permeation
  • the permeation experiment was carried out such that the GO membranes, supported by the copper plate, were clamped between two O-rings and then fixed between feed and permeate compartments to provide a leak tight environment.
  • the part-purified LiCI solution obtained after desorption from the adsorbent was used as feed and deionized water in the permeate side.
  • ions tend to diffuse through the membrane and reach the permeate side.
  • Permeate solution is collected after 24 h and chemical analysis is conducted to quantify the ions in the permeate side.
  • GO membranes on PES substrates were found to be disintegrating after long time exposure to brine solution at high pressure and to resolve this issue we have partially reduced GO membrane with ascorbic acid. Partial reduction of GO decreased the amount of functional groups present in the membrane and subsequently reduced the hydrophilicity and wettability of the membrane.
  • the ascorbic acid reduced graphene oxide (rGO) is found to be more stable in brine solution after long exposure.
  • An aqueous suspension of graphene oxide was prepared by dispersing millimeter-sized graphite oxide flakes (purchased from BGT Materials Limited) in distilled water using bath sonication for 15 hours. The resulting dispersion was centrifuged 6 times at 8000 rpm to remove the multilayer GO flakes. The concentration of as prepared GO solution was 0.1 mg/ml. To improve the stability of GO membrane in brine solution we have partially reduced the GO with ascorbic acid. 1 ml of 0.17 mg/ml vitamin C was mixed with 1 ml GO solution and then the whole mixture was diluted to a volume of 20 ml. The pH of the mixed solution was adjusted to about 9-10 with 25% ammonia solution to promote the colloidal stability of the GO nanosheets. The solution was then heated at 90 degrees for 30 minutes in water bath to finish the reduction process.
  • Modified GO membranes were then prepared from the partially reduced GO (rGO) solution via vacuum filtration through a PES membrane with 0.22 urn pore size.
  • rGO partially reduced GO
  • PES substrate we coated a very thin polymer film on the surface of the PES substrate.
  • the polymer used was Poly(diallyldimethylammonium chloride), which is a positively charged polymer.
  • the positively charged Poly(diallyldimethylammonium chloride) tightly bonded the GO membrane and PES substrate via the electrostatic forces.
  • the coated PES membrane was stored in the vacuum oven for two hours at 50 °C before depositing the partially reduced GO via vacuum filtration.
  • Figure 50 shows the concentration of salts in brine solution before and after filtration through the modified GO membrane.
  • S1 and S2 represent data from two different membranes.
  • Membrane used is 200 nm thick and 30 minute reduced GO.
  • nano-channels and/or interlayer galleries formed between the nano-sheets of, for example, GO or rGO act as ion-sieves.
  • the present invention further provides an electrolysis step conducted on part-purified lithium chloride solution that is the product of either or both of the first and second purification steps as described hereinabove.
  • the combination of either or both of the first and second purification steps as described hereinabove and an electrolysis step allows the production of high purity lithium hydroxide.
  • the electrolysis is carried out at a current density of 5kA/m2 at ⁇ 50°C.
  • the electrolysis utilises N982TM ion exchange membranes from DuPont and is conducted in the range of 3.9-4.0V.
  • the feed lithium containing solution is obtained as a lithium chloride solution from either of the first or second purification steps described hereinabove, or potentially as the result of both the first and second purification steps if conducted in series. Whichever is the case, the solution is diluted to 300 g/L.
  • the anolyte flow rate is adjusted to about 35 imL/min to achieve a depleted brine concentration of 200 g/L.
  • the electrolysis step is performed using the ion exchange membrane N982TM at a current density of 5kA/m2 and at ⁇ 50°C.
  • the current efficiency data based on caustic collection and gas analysis are presented in Figure 51 , the cell voltage results are shown in Figure 52, and the DC energy consumption data shown in Figure 53.
  • the LiOH concentration exiting the cell during each run is noted in Figure 52 also.
  • the average cell voltage was in the range of 3.9-4.0V.
  • the chlorated hypo-brine is treated with peroxide to destroy chloratre levels and the brine reused for electrolysis.
  • Membrane cell electrolysis showed an energy consumption of 3,500 kWh/ton of LiOH.H 2 O, the cell voltage being in the range 3.9 to 4 V at 5kA/m 2 , and the caustic current efficiency being ⁇ 75% with N982TM membranes.
  • the chloride concentration in the catholyte product LiOH was ⁇ 360 ppm. These chloride levels were removed during crystallization of LiOH catholyte using double crystallization process as described below.
  • the crystallizer body was a 3 L cylindrical stainless steel (SS) vessel with a hemispherical bottom and was heated with a 100 watt external SS mantle.
  • the vessel was equipped with a variable speed overhead agitator.
  • the liquor temperature inside the crystallizer was maintained at 80°C by operating under vacuum, using a two stage rotary vane vacuum pump downstream of the condenser.
  • a needle valve was used to bleed atmospheric air into the vacuum line to control the internal pressure.
  • a digital pressure gauge displays the absolute pressure for the system for operator interface.
  • the temperature of the saturated vapour was calculated and was used to calculate the boiling point rise (BPR) of the solution.
  • BPR boiling point rise
  • the crystallizer was operated in a quasi-steady state manner, with continuous feed and evaporation and batch slurry removal. Slurry was removed batch- wise and separated through a laboratory 5 inch vertical basket centrifuge with a 10- 15 micron screen.
  • the LiOH.H 2 O product was dried in a glove box (VeoliaTM). Nitrogen was used in the crystallizer operation in order to minimize CO 2 contamination including the feed tank, the crystallizer body during standby, centrifuge during solid-liquid separation, and the glove box drying operation.
  • the catholyte LiOH from the electrolysis had the composition set out in the table below.
  • the first and/or second purification steps may comprise more than a single stage, pass or repeat of contact or exposure between the lithium containing solution passed to them and the adsorbent or graphene based filter medium, respectively, to realise the most significant benefits of the combination process of the present invention.
  • a particular advantage is realised in accordance with the present invention in that the nanotube/fibre adsorbents of the present invention can be readily separated from a liquid after the sorption by filtration, sedimentation, or centrifugation because of their fibril morphology. It is expected that this will significantly reduce the cost of separation of the adsorbent from the liquid.
  • the present invention provides a process to separate and purify LiCI and reduce or eliminate impurities in LiCI solutions to concentrations acceptable for use as a feed to an electrolysis step for the production of lithium hydroxide.
  • LiCI solutions may be used as a pre-cursor in high purity applications such as lithium ion batteries. This purification is achieved as described hereinabove.
  • the preferred process according to the present invention specifically provides a method of reducing the contaminant impurities in the LiCI solution to less than about 20 ppm.
  • the combination of the techniques of adsorption and filtration using a graphene filter medium is particularly advantageous in the production of substantially purified lithium solutions, particularly lithium chloride solutions.
  • substantially purified lithium solutions particularly lithium chloride solutions.
  • One basis for this apparent synergy in the combination of the adsorption and filtration appears to be the effectiveness of adsorption in removing sodium ions, in particular, which in turn ensures that the part-purified lithium containing solution that is then passed to the graphene based filter medium is able to be further purified effectively thereby.
  • the present invention provides an improved extraction method for the extraction of lithium from a LiCI containing brine.
  • Preferred processes according to the present invention are envisaged as being able to meet the needs and demands of today's lithium ion battery industry.
  • Preferred processes according to the present invention specifically provide a method of reducing the contaminant impurities in the brine to less than 20 ppm.

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Abstract

L'invention concerne un procédé de traitement combiné pour la purification de solutions contenant du lithium, le procédé comprenant les étapes de procédé qui consistent : a) à faire passer une solution contenant du lithium à travers une ou plusieurs étapes de purification pour produire une solution de chlorure de lithium sensiblement purifiée ; et b) à faire passer la solution de chlorure de lithium sensiblement purifiée de l'étape a) dans une étape d'électrolyse dans laquelle un monohydrate d'hydroxyde de lithium est produit, la ou les étapes de purification comprenant une première étape de purification dans laquelle la solution contenant du lithium est mise en contact avec un adsorbant de titanate, des ions de lithium étant adsorbés sur celui-ci tout en rejetant sensiblement tous les autres cations, la récupération de lithium à partir de l'adsorbant fournissant une solution contenant du lithium partiellement purifiée, et/ou une seconde étape de purification dans laquelle un milieu filtrant à base de graphène est utilisé pour fournir une solution contenant du lithium davantage purifiée.
PCT/AU2017/050100 2017-02-08 2017-02-08 Procédé de traitement combiné incorporant une électrolyse pour solutions contenant du lithium Ceased WO2018145142A1 (fr)

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