A process for alumina and carbonate production from aluminium rich materials with integrated CO.sub.2 utilization, comprising: comminuting and leaching Al-rich materials in concentrated HCI; separating unreacted material from metal chloride solution; separating Al.sup.3+ from solution by crystallization of AlCl.sub.3.6H.sub.2O; calcination of AlCl.sub.3.6H.sub.2O with HCl recovery; precipitation of metal carbonates from CO.sub.2; regeneration of HCl and extractive amines; the Al.sup.3+ separation the facilitated by increasing HCl concentration; the calcination being performed in two steps, one in the range 400 and 600 C. to generate a HCl-rich gas and one above 600 C. to produce Al.sub.2O.sub.3; for precipitating metal carbonates, mixing the metal chloride solution with an organic solution containing a selected amine and contacting the mixture with a CO.sub.2-containing gas, thereby also extracting HCl by formation of an ammonium chloride salt complex; processing thermally or chemically the organic solution to regenerate the amine for recirculation.

A process for alumina and carbonate production from aluminium rich materials with integrated CO.sub.2 utilization, comprising: comminuting and leaching Al-rich materials in concentrated HCI; separating unreacted material from metal chloride solution; separating Al.sup.3+ from solution by crystallization of AlCl.sub.3.6H.sub.2O; calcination of AlCl.sub.3.6H.sub.2O with HCl recovery; precipitation of metal carbonates from CO.sub.2; regeneration of HCl and extractive amines; the Al.sup.3+ separation the facilitated by increasing HCl concentration; the calcination being performed in two steps, one in the range 400 and 600 C. to generate a HCl-rich gas and one above 600 C. to produce Al.sub.2O.sub.3; for precipitating metal carbonates, mixing the metal chloride solution with an organic solution containing a selected amine and contacting the mixture with a CO.sub.2-containing gas, thereby also extracting HCl by formation of an ammonium chloride salt complex; processing thermally or chemically the organic solution to regenerate the amine for recirculation.

A movable device, e.g., a laboratory, for obtaining lithium salt from brine has a movable box, and a device for removing impurities from brine and a lithium precipitation device that are disposed in the movable box. The device for removing impurities from brine is connected to the lithium precipitation device. The device for removing impurities from brine comprises one or more of an adsorption-separation device, a membrane device, an electrodialysis device, a device for deeply removing impurities with resin, and an evaporation device. The laboratory is in a form of box modular assembly and may be placed on a truck and flexibly transported to a brine lake. In a case of a large-scale pilot test, an adsorption-membrane coupling technology to evaporation and lithium precipitation may be completely implemented, so that a simulation test of a whole lithium carbonate process may be carried out on site.

A movable device, e.g., a laboratory, for obtaining lithium salt from brine has a movable box, and a device for removing impurities from brine and a lithium precipitation device that are disposed in the movable box. The device for removing impurities from brine is connected to the lithium precipitation device. The device for removing impurities from brine comprises one or more of an adsorption-separation device, a membrane device, an electrodialysis device, a device for deeply removing impurities with resin, and an evaporation device. The laboratory is in a form of box modular assembly and may be placed on a truck and flexibly transported to a brine lake. In a case of a large-scale pilot test, an adsorption-membrane coupling technology to evaporation and lithium precipitation may be completely implemented, so that a simulation test of a whole lithium carbonate process may be carried out on site.

A method to make LiF crystals by simultaneously adding aqueous LiHCO.sub.3 and HF to a stirred reactor containing water or a solution of LiF. The method yields LiF crystals having a Dv50 particle size of from about 60 m to about 90 m.

A method to make LiF crystals by simultaneously adding aqueous LiHCO.sub.3 and HF to a stirred reactor containing water or a solution of LiF. The method yields LiF crystals having a Dv50 particle size of from about 60 m to about 90 m.