A method for separating organic solvent(s) from an aqueous process stream including organic solvent(s), includes passing the aqueous stream including organic solvent(s) through a granular bed including glass granules, wherein at least 90% of said glass granules have a maximum particle diameter smaller than 1.0 mm.

A method for separating organic solvent(s) from an aqueous process stream including organic solvent(s), includes passing the aqueous stream including organic solvent(s) through a granular bed including glass granules, wherein at least 90% of said glass granules have a maximum particle diameter smaller than 1.0 mm.

A process for preparing lead by electroreduction with ammonium sulfate and ammonia is provided. In the process, an ammonium sulfate aqueous solution is used as an electrolyte, a lead compound is used as a raw material, titanium is used as an anode, stainless steel or lead is used as a cathode, and a direct-current electric field is applied in an electrolytic bath; the lead compound is reduced to metal lead after obtaining electrons at the cathode; and at the anode, ammonia is oxidized to nitrogen for escaping, and H.sup.+ ions are generated simultaneously; sulfate radical ions and chloride ions in the lead compound enter the solution and react with the ammonia water to form ammonium sulfate and ammonium chloride; and the lead monoxide and lead dioxide in the lead compound are reduced to a metal lead and OH.sup. ions are released to combine with the H.sup.+ ions to form water.

The invention relates to an EWS module device for electro-winning and/or electro-refining, based on a saturated leaching solution of PLS/electrolyte/raffmate/ILS without solvent extraction, characterised by comprising: a tank (10 and 12); a set of electrolytic cells contained within the tank, wherein the cells are electrically and volumetrically separated by the internal walls of the module (14), with the cells being connected in series by a joining board or capping board (3); an intercellular bar (1); an intercellular bar guide (2); inlet and outlet ducts for the PLS/electrolyte/raffinate/ILS (17) and (11) for each cell independently; and each EWS module is in turn connected to the other modules by an inter-module connector (18), and same in turn control the connection and disconnection of the EWS modules by an interrupter (25); operating process of the EWS module device; and connection and disconnection process between different EWS module devices.

A process for preparing lead by electroreduction with an ammonium chloride and an ammonia is disclosed. In the process, an ammonium chloride aqueous solution is used as an electrolyte, a lead compound is used as a raw material, titanium is used as an anode, stainless steel or lead is used as a cathode, and a direct-current electric field is applied in an electrolytic bath; the lead compound is reduced to metal lead after obtaining electrons at the cathode; and at the anode, ammonia is oxidized to nitrogen for escaping, and H.sup.+ ions are generated simultaneously; sulfate radical ions and chloride ions in the lead compound enter the solution to form ammonium sulfate and ammonium chloride; and the lead monoxide and lead dioxide in the lead compound are reduced to a metal lead and OH.sup. ions are simultaneously released to combine with the H.sup.+ ions to form water.

Materials and methods for precious metal recovery are disclosed. Usable leaching solutions are preferably aqueous based and include appropriate materials in sufficient quantities to solubilize and stabilize precious metal. Such materials typically include oxidant material. Some or all of the oxidant material can be, in some instances, generated in-situ. The leaching solution is typically contacted with a substrate having a target precious metal, thereby solubilizing precious metal to form a stable, pregnant solution. The precious metal can then be recovered from the pregnant solution. In some instances, components of the leaching solution can be regenerated and reused in subsequent leaching.

Materials and methods for precious metal recovery are disclosed. Usable leaching solutions are preferably aqueous based and include appropriate materials in sufficient quantities to solubilize and stabilize precious metal. Such materials typically include oxidant material. Some or all of the oxidant material can be, in some instances, generated in-situ. The leaching solution is typically contacted with a substrate having a target precious metal, thereby solubilizing precious metal to form a stable, pregnant solution. The precious metal can then be recovered from the pregnant solution. In some instances, components of the leaching solution can be regenerated and reused in subsequent leaching.

A process for recovering non-ferrous metals from a solid matrix may include: (a) leaching the solid matrix with an aqueous-based solution containing chloride ions, ammonium ions, and Cu.sup.2+ ions, having a pH of 6.5-8.5, in a presence of oxygen, at a temperature of 100 C.-160 C. and a pressure of 150 kPa-800 kPa, so as to obtain an extraction solution comprising leached metals and solid leaching residue; (b) separating the solid leaching residue from the extraction solution; and/or (c) subjecting the extraction solution to at least one cementation so as to recover the leached metals in elemental state. The pH may be greater than or equal to 6.5 and less than or equal to 8.5. Temperature may be greater than or equal to 100 C. and less than or equal to 160 C. Pressure may be greater than or equal to 150 kPa and less than or equal to 800 kPa.

A process for recovering non-ferrous metals from a solid matrix may include: (a) leaching the solid matrix with an aqueous-based solution containing chloride ions, ammonium ions, and Cu.sup.2+ ions, having a pH of 6.5-8.5, in a presence of oxygen, at a temperature of 100 C.-160 C. and a pressure of 150 kPa-800 kPa, so as to obtain an extraction solution comprising leached metals and solid leaching residue; (b) separating the solid leaching residue from the extraction solution; and/or (c) subjecting the extraction solution to at least one cementation so as to recover the leached metals in elemental state. The pH may be greater than or equal to 6.5 and less than or equal to 8.5. Temperature may be greater than or equal to 100 C. and less than or equal to 160 C. Pressure may be greater than or equal to 150 kPa and less than or equal to 800 kPa.

The present invention discloses a method and system for quickly detecting a cathode short circuit. The method includes: continuously measuring a cathode current; determining whether an increased value of the cathode current in a set time is within a set range of the increased value; if the increased value is within the set range of the increased value, establishing a linear model according to a change of the cathode current with time, and calculating a slope and a determining coefficient according to the linear model; if the increased value is not within the set range of the increased value, determining that the cathode does not have a short circuit; determining whether the slope is within a set slope threshold range; if the slope is within the set slope threshold range, determining whether the determining coefficient is greater than a set determining coefficient threshold; if the slope is not within the set slope threshold range, determining that the cathode does not have a short circuit; if the determining coefficient is greater than or equal to the set determining coefficient threshold, determining that the cathode has a short circuit; and if the determining coefficient is smaller than the set determining coefficient threshold, determining that the cathode does not have a short circuit. The present invention can avoid a sustained short-circuit current loss and improve the electrolysis current efficiency.