TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Process: The process comprises heating the supernatant at the temperature of at least 97 degrees C or at 95 degrees C so as to at least partially convert the lithium bicarbonate into lithium carbonate and precipitate any dissolved lithium carbonate contained in it. During the sparging, the pH is at least substantially maintained at 11. During the process, the aqueous composition comprising lithium hydroxide is at least substantially maintained at a concentration of lithium hydroxide of 30-70 g/l, preferably 48-55 g/l. The sparging is carried out at 15-30 degrees C. During the process, the supernatant, when being heated, is at least substantially maintained at a lithium concentration of 1-10 g/l, preferably 3-5 g/l. The process (P1) is carried out: in a three-compartment membrane electrolysis cell; and by introducing the aqueous composition comprising the lithium compound into a central compartment, an aqueous composition comprising lithium hydroxide into a cathodic compartment, and an aqueous composition comprising an acid into an anodic compartment. During the process (P1), the aqueous composition comprising: lithium hydroxide is at least substantially maintained at a concentration of lithium hydroxide of 35-70 g/l, preferably 45-65 g/l; and sulfuric acid is at least substantially maintained at a concentration of sulfuric acid of 20-100 g/l, preferably 25-35 g/l or 60-90 g/l. During the process (P1): temperature of the aqueous composition comprising lithium sulfate is at least substantially maintained at 20-100 degrees C, preferably 30-40 degrees C or 46-54 degrees C; electrical current is at least substantially maintained at a density of 200-6000 A/m2, preferably 450-550 A/m2, or 50-250 mA/cm2, preferably 100-175 mA/cm2 or at a constant value; and voltage is at least substantially maintained at a constant value i.e. 3-10 V, preferably 4-7 V. During the process: the aqueous composition comprising lithium hydroxide is at least substantially maintained at a concentration of lithium hydroxide of 2-4 M, preferably 2.7-3.3 M; the aqueous composition comprising sulfuric acid is at least substantially maintained at a concentration of sulfuric acid of 0.3-1.5 M, preferably 0.5-1 M; the process aqueous composition comprising lithium sulfate is at least substantially maintained at a concentration of lithium sulfate of 10-20 g/l, preferably 13-17 g/l; and the aqueous composition comprising lithium sulfate is at least substantially maintained at a concentration of lithium sulfate of 0.4-2.5 M, preferably 0.6-1.8 M. During the electrolysis, the aqueous composition comprising lithium sulfate: has a pH of 7-14.5, preferably 7-9; and is maintained at a pH of 7-13.5, preferably 7-12. An anolyte used during the electrolysis or electrodialysis comprises ammonia, ammonium sulfate, ammonium bisulfate and/or ammonium hydroxide, thus generating an ammonium salt. The process further comprises adding ammonia and/or ammonium hydroxide at an anode or its adjacent, thus generating an ammonium salt, in an anolyte where the anode is used for the process, pH of the anolyte is maintained at -0.5 to 3.5, preferably -0.25 to 1. Ammonia and/or ammonium hydroxide is added in a sub-stoichiometric quantity as compared to sulfuric acid produced. Ammonia is added in a molar ratio ammonia:sulfuric acid comprised of 0.5:1-2:1, preferably 1:1-1.9:1. The supernatant is heated at a temperature of at least 87 degrees C, preferably 95 degrees C. The aqueous composition comprising lithium and at least one metal ion is reacted with the base so as to obtain a pH of 5.4-5.8. The process (P2) further comprises maintaining the aqueous composition comprising lithium and the metal ion that is reacted with a base so as to obtain a pH of about 4.5 to about 6.5 at an oxidative potential of at least 350 mV. The aqueous composition is at least substantially maintained at an oxidative potential of at least 350 mV by sparging a gas comprising oxygen in it. The process (P2) comprises reacting the aqueous composition comprising lithium and having the reduced content of the metal ion with another base so as to obtain a pH of 9.5-11.5, preferably 10-10.5 or 9.8-10.2. The aqueous composition comprising lithium and having the reduced content of the metal ion is reacted with the another base over a period of time sufficient for reducing the content of the metal ion in the aqueous composition below a predetermined value. The reaction is carried out over a period of time sufficient for reducing the content of calcium below 250 mg/l, preferably below 200 mg/l. Contacting with the ion exchange resin allows for reducing a content of calcium of the composition below 10 mg/l, preferably below 0.5 mg/l. The acid roasted lithium-containing material is leached with water so as to obtain the aqueous composition comprising lithium and at least three metal ions comprising iron, aluminum, manganese or magnesium, or at least four metal ions comprising aluminum, ferrous, ferric, magnesium, calcium or manganese. The base-baked lithium-containing material is beta -spodumene that has been previously reacted with sodium carbonate and with carbon dioxide, and eventually heated. Preferred Components: The aqueous composition comprising the lithium compound comprises lithium sulfate (preferred), lithium chloride, lithium fluoride, lithium carbonate, lithium bicarbonate, lithium acetate, lithium stearate or lithium citrate. The lithium sulfate is present at 10-20 g/l, preferably 13-17 g/l. The aqueous composition comprising lithium sulfate has a pH of greater than 7.2, preferably greater than 8.5 and is submitted to a membrane electrolysis process, preferably a three compartment membrane electrolysis process. The ammonium salt is ammonium sulfate. The metal ion is ferric ion, aluminum (both preferred) or ferrous ion. The hydroxide comprised in the precipitate is aluminum hydroxide and/or iron(III) hydroxide. The base as to obtain a pH of 4.5-6.5 is lime that is provided as an aqueous composition having a concentration of 15-25 wt.%. The gas is air. The base used so as to obtain a pH of 9.5-11.5 is sodium hydroxide. The metal carbonate is sodium carbonate, sodium bicarbonate or ammonium carbonate. The ion exchange resin is a cationic resin that is substantially selective for divalent and/or trivalent metal ions. ACTIVITY - Neuroleptic.    MECHANISM OF ACTION - None given.    EXAMPLE - Lithium hydroxide solution was used as a feed. Tenor in 14-15.5 g/l lithium was used. The lithium hydroxide carbonization (LC) process was conducted in an enclosed 4 l Pyrex (RTM: Reactor). The reactor was equipped with an overhead impeller, sparger, level controller, pH probe and thermocouple. A burp-type sparger was used for carbon dioxide addition. The sparger was located below the impeller. The below disposed sparger ensured full dispersion of the gas. The carbon dioxide flow was controlled by pH of reaction slurry using a solenoid valve. Peristaltic pumps were used for transferring solutions and slurries. The process slurry from LC was continuously pumped to the LC clarifier, where the solids were permitted to settle and the solution phase could continuously overflow back into the LC reactor. The clarifier solids were harvested from the clarifier underflow on a per shift basis and filtered through filter paper. The filter cakes were flood-washed in triplicate with hot reverse osmosis water and then dried in an oven set at 105-110 degrees C. The recovered filtrate was returned back to the LC circuit. The LC reactor level was maintained at a constant volume of 3 l by the level sensor controlling the bleed pump to direct current (DC) circuit. The LC circuit bleed was lined in advanced LC clarifier overflow to the DC reactor. The DC process was conducted in an enclosed 4 l Pyrex (RTM: Reactor). The reactor was placed in an electric heating mantle and equipped with an overhead impeller, pH probe and thermocouple. The solution in the DC Reactor was heated to 95 degrees C to decompose lithium bicarbonate and drive the remaining lithium carbonate from solution. The resulting slurry was pumped to a heated clarifier. A bleed was taken from the top of the clarifier and collected in a DC Filtrate drum. The slurry level in the DC reactor was maintained by positioning the DC bleed tubing inlet in the clarifier at a fixed level and setting the bleed pump to a greater flow rate than that of the feed to the DC reactor. The thickened pulp was harvested on a per shift basis. The filtered cake was treated in the same manner as the LC reactor solids. The resulting solids represented a secondary lithium carbonate product. This DC solid stream was kept separate from the primary carbonate stream and was independently characterized.