The present application relates to methods for the simultaneous leaching and extraction of precious metals. For example, the present application relates to methods of leaching and extracting gold and/or palladium from a substance comprising gold and/or palladium such as a gold- and/or palladium-containing ore in one step using a compound of Formula I:(I). ##STR00001##

The present application relates to methods for the simultaneous leaching and extraction of precious metals. For example, the present application relates to methods of leaching and extracting gold and/or palladium from a substance comprising gold and/or palladium such as a gold- and/or palladium-containing ore in one step using a compound of Formula I:(I). ##STR00001##

A metal composition includes from 90.10% wt up to 97% wt of copper, at least 0.1% wt of nickel, at least 0.0001% wt and less than 1.00% wt of iron, and 250-3000 ppm wt of oxygen. The composition is suitable for being processed by a process including the electrorefining of copper in an electrolytic cell, wherein the voltage difference over the cell is maintained at less than 1.6 volt, the anode comprises at most 98.0% wt of copper and less than 1.00% wt of iron, the current density through the cell is at least 180 A/m.sup.2 of cathode surface, electrolyte is removed from the cell during the operation at an average refreshing rate of 30-1900% per hour, by overflow of a stream of electrolyte over a cell wall, and a gas is bubbled through the electrolyte in between anode and cathode. The composition is even more suitable after a reduction of its oxygen content.

A metal composition includes from 90.10% wt up to 97% wt of copper, at least 0.1% wt of nickel, at least 0.0001% wt and less than 1.00% wt of iron, and 250-3000 ppm wt of oxygen. The composition is suitable for being processed by a process including the electrorefining of copper in an electrolytic cell, wherein the voltage difference over the cell is maintained at less than 1.6 volt, the anode comprises at most 98.0% wt of copper and less than 1.00% wt of iron, the current density through the cell is at least 180 A/m.sup.2 of cathode surface, electrolyte is removed from the cell during the operation at an average refreshing rate of 30-1900% per hour, by overflow of a stream of electrolyte over a cell wall, and a gas is bubbled through the electrolyte in between anode and cathode. The composition is even more suitable after a reduction of its oxygen content.

Described are methods for the recovery of uranium from uranium hexafluoride dissolved directly into ionic liquids.

Described are methods for the recovery of uranium from uranium hexafluoride dissolved directly into ionic liquids.

An apparatus, also named transfer box or TB, for conveying an anode assembly outside of an electrolyte cell is described. An apparatus, also named cell preheater lifting beam or CPLB, for conveying an anode assembly or a cell pre-heater outside of an electrolyte cell is also disclosed. TB and CPLB are conjointly used for starting up the electrolytic cell or for replacing a spent anode assembly while maintaining the production of non-ferrous metal, such as aluminum or aluminium. The thermal insulation of the TB allows maintaining the anode temperature homogeneity and preventing thermal shocks when introducing the inert anodes into the hot electrolytic bath. TN and CPLB allow accurate positioning of anode assemblies or cell-preheaters over the electrolysis cell before achieving mechanical and electrical connections of the anode assembly or the cell pre-heater to the electrolysis cell. Several related methods for the operation of an electrolytic cell are also disclosed.

An apparatus, also named transfer box or TB, for conveying an anode assembly outside of an electrolyte cell is described. An apparatus, also named cell preheater lifting beam or CPLB, for conveying an anode assembly or a cell pre-heater outside of an electrolyte cell is also disclosed. TB and CPLB are conjointly used for starting up the electrolytic cell or for replacing a spent anode assembly while maintaining the production of non-ferrous metal, such as aluminum or aluminium. The thermal insulation of the TB allows maintaining the anode temperature homogeneity and preventing thermal shocks when introducing the inert anodes into the hot electrolytic bath. TN and CPLB allow accurate positioning of anode assemblies or cell-preheaters over the electrolysis cell before achieving mechanical and electrical connections of the anode assembly or the cell pre-heater to the electrolysis cell. Several related methods for the operation of an electrolytic cell are also disclosed.

An apparatus, also named transfer box or TB, for conveying an anode assembly outside of an electrolyte cell is described. An apparatus, also named cell preheater lifting beam or CPLB, for conveying an anode assembly or a cell pre-heater outside of an electrolyte cell is also disclosed. TB and CPLB are conjointly used for starting up the electrolytic cell or for replacing a spent anode assembly while maintaining the production of non-ferrous metal, such as aluminum or aluminium. The thermal insulation of the TB allows maintaining the anode temperature homogeneity and preventing thermal shocks when introducing the inert anodes into the hot electrolytic bath. TN and CPLB allow accurate positioning of anode assemblies or cell-preheaters over the electrolysis cell before achieving mechanical and electrical connections of the anode assembly or the cell pre-heater to the electrolysis cell. Several related methods for the operation of an electrolytic cell are also disclosed.

A filter press device for electrolytic production of metal for electrodeposition of metal from solutions, constructed from a plurality of cells connected electrically and hydraulically in series. Each has alternating frames and ion-exchange membranes to form alternating anode and cathode compartments, allowing the free path of liquid. Anolyte or catholyte passes through each compartment. The electrolyzed product is discharged from the compartment in the form of metal or a metallic compound. The electrodes are designed with a vertical base plate acting as an anode with the respective anolyte in a cell unit and in the other, acting as a cathode with the respective catholyte in the adjacent cell unit. Completed the production cycle, the device is stopped, the cell is opened, allowing the metal deposition electrodes, cathodes, can be removed and replaced to start a new productive cycle or remain in place with automatic detachment of metal product.