MX2013011323A

MX2013011323A - System and process for the continuous recovery of metals.

Info

Publication number: MX2013011323A
Application number: MX2013011323A
Authority: MX
Inventors: Cameron Barton
Original assignee: Smidth As F L
Priority date: 2011-04-01
Filing date: 2012-04-02
Publication date: 2013-10-17
Also published as: AU2012236120A1; CL2013002814A1; CN103582710A; WO2012135826A1; CA2831936A1; US20140144788A1

Abstract

A system [100'] and process [100] for the continuous recovery of metals is disclosed. The system [100'] comprises a continuous acid wash system [10'], a holding tank [60], a continuous elution system [20'], a continuous electrowinning system [40'], a carbon regeneration system [30'], and a continuous carbon loading/adsorption system [70']. The systems and methods disclosed overcome the disadvantages associated with current systems and processes which utilize batch process steps and equipment designed for batch processes. The systems [10', 20', 30'] are each configured to receive a continuous inflow of a solution or slurry and deliver a continuous outflow of a solution or slurry, without interruptions which are common with conventional metal recovery systems [9000'].

Description

SYSTEM AND PROCESS FOR CONTINUOUS METAL RECOVERY FIELD OF THE INVENTION The invention relates to mining and metallurgical refining, and more particularly to systems and processes for solvent extraction; and to the electroextraction of metals.

BACKGROUND OF THE INVENTION For this purpose, there are generally two main processes available for the concentration and recovery of precious metals: precipitation with zinc, and electroextraction. Precipitation with zinc involves crushing and grinding the ore containing the precious metal (eg, gold), and then combining the ground ore with a solution of water and caustic cyanide. The resulting slime-like pulp is moved into a sedimentation tank where the thicker charged solids, with gold move to the bottom via gravity, and a first, lighter, gold, water-based mother solution and the cyanide moves towards the top, and it is removed for further processing. The gold-laden solids are agitated and aerated in a separate, agitated leaching process where the oxygen reacts to leach the gold into the caustic water and the cyanide, forming a second stock solution. The second mother solution passes through a filter Ref 1 '243895 drum which subsequently separates the remaining solids. The first and second mother solutions are combined with zinc to precipitate the dissolved gold. The resultant precipitated gold concentrate can then be melted to produce a refined gold bar.

Electroextraction typically involves extracting a precious metal such as gold from an electrolyte. First, the activated carbon is combined with a stock solution in a batch process step. The activated carbon adsorbs the precious metal contained within the mother solution, and becomes "charged" with the precious metal. The charged carbon is then pickled by washing sequentially in three batching steps to remove the mineral residue. First, the charged carbon is moved to a wash tank and then the tank is filled with a dilute acid solution. The wash tank is then drained and the diluted acid solution, used, is pumped away and discarded. The same wash tank is then filled with water to rinse the remaining acid from the charged carbon. The water becomes slightly acidic during this process. In a manner similar to diluted acid, the slightly acidic rinse water, used, is i also drained from the washing tank, removed by pumping, and discarded. At the end, the tank is filled with a caustic solution, and the activated carbon is washed in the caustic solution. The caustic solution used is then drained from the tank, removed by pumping and discarded. One step of rinsing with final water, optional can be done again, filling the washing tank with rinsing water or neutral pH solution, rinsing the caustic residue of the charged carbon, and then draining the tank of the water / rinsing solution used, so that it can be removed by pumping for waste.

After washing, the charged carbon is removed from the washing tank and then added to a washing solution comprising water, a caustic substance, and cyanide to form a charged carbon washing / suspension solution. The charged carbon wash / suspension solution goes through an elution process where high temperatures and pressures are used to "leach" the gold from the charged carbon into the caustic wash solution to form an electrolyte solution. The electrolytic solution is then moved to an electrolytic cell in batches where wire cathodes (eg crosslink & o) or plate catches the gold concentrate deposited during electrolysis. After the batch electroextraction process, the cathodes are manually removed from the cell for cleaning, so that the gold concentrate deposited thereon can be removed from the cathodes and prepared for smelting. After cleaning, the cathodes are then manually replaced within the electrolytic cell, and the complete sequence of batch washing, elution and electroextraction processes; it is repeated. Some cathodes (for example, wire cathodes, due to their small interstices) are not reusable and must be recycled after processing, thereby increasing overall / operational costs.

Figure 27 illustrates schematically a conventional metal recovery process 9000, as described above. Activated or reactivated carbon 9560 is suspended within a stock solution in a batch carbon loading step, conventional 9700. The stock solution is generally formed by percolation of a dilute cyanide solution through a leach pad in mineral-laden, crushed ore pile (for example, as a spray immersion or irrigation having a concentration of approximately 226 grams to 453 grams (0.5 to 1 pound) of sodium cyanide, potassium cyanide, or cyanide of calcium per ton of solution). Once activated carbon adsorbs the desired material (eg, gold, silver, platinum, lead, copper, aluminum, platinum, uranium, cobalt, manganese) from the stock solution, it becomes "charged" 9570 carbon and enters a batch acid washing process 9100 configured to strip charged 9570 carbon as previously discussed.

Figure 28 shows an example of a conventional batch acid washing system 9100 '. The charged 9570 carbon enters an acid wash vessel 9120 which receives the diluted acid from a 9140 diluted acid tank via a 9132 pump. The overflow of dilute acid is captured by a sump pump 9150 that moves the overflow to a tank of neutralization 9160. The contents of neutralization tank 9160 can be moved to a secondary holding tank via; a pump 9136. The conventional batch acid washing process 9100 continues by draining the acid wash container 9120 from the diluted acid solution, and then filling the container 9120 with an aqueous rinse solution. The overflow of the aqueous rinse solution is captured by sump pump 9150 which moves the overflow to a neutralization tank 9160 and / or a holding tank. The process 9100 can be continued by draining the container 9120 from the aqueous rinse solution, and then filling the container 9120 with a caustic rinse agent. The overflow of the caustic rinse can likewise be captured by sump pump 9150 and moved to a neutralization tank 9160 and / or a holding tank (not shown).

After the loaded 9570 carbon is pickled, it leaves the batch acid washing process in batch 9100 (via the carbon transfer pump 9134) and enters a conventional batch elution process (eg, Zadra wash) 9200. As shown in Figure 29, a conventional batch elutriation process 9200 typically involves the feed of loaded carbon 9500 pickling and / or a charged carbon directly from an adsorption system 9700 and a wash container 9240. The wash container 9240 is in general, a large cylindrical tank of material suitable for maintaining reactants at a high pressure and temperature (for example 138 ° C to 148 ° C). The etched loaded carbon 9500 is maintained inside the washing vessel 9240 at high temperatures and pressure in the presence of an aqueous, caustic washing solution comprising cyanide. After a period of time, the spent 9550 carbon is removed from the wash container 9240 (for example, via the 9232 carbon transfer pump), and is moved to a carbon handling system or a 9300 carbon regeneration system. 'or carbon generation process' 9300. The hot electrolytic solution 9421 is formed inside the washing container 9240 since the material previously adsorbed on the charged carbon is leached into the washing solution. The hot electrolytic solution 9421 is also removed from the washing container 9240 and passes through a heating slide 9250 or equivalent heat exchanger for cooling before entering a conventional batch electroextraction system 9400 'or process 9400. Cooling of the hot electrolytic solution 9421 to form uria 9530 electrolytic solution of lower temperature, it is generally necessary to reduce the risk of ignition inside a batch electrolytic metal recovery cell, conventional 9420. The heating slide 9250 also serves to recycle the energy by heating the colder, sterile 9540 solution which leaves the the electrolytic metal recovery cell 9420 (for example, at approximately 66 ° C), and / or the sterile solution 9237 that sele of the sterile solution storage tank 9220 before re-entering the washing vessel 9240 to serve once more as a re-leaching agent for the washing solution. Heating of the colder sterile solution 9237, 9540 to form a sterile hot solution 9239 may also be performed using a heater in addition to, or in place of the heating slide 9250. One or more pumps 9234, 9236 are generally used to transfer the sterile solution back to the 9240 wash tank. Additional reagent from a reagent handling system and / or more stock solution can be added to the sterile solution tank 9220, as necessary.

As shown in Figure 30, the electrolytic solution 9530 enters a conventional batch electrolytic metal recovery cell 9420, which operates in batch cycles. A series of parallel plate cathodes are placed in close proximity and the 9530 electrolyte solution is pumped in and agitated around the cathodes. The body portions of the cell 9420 carry an opposite charge with respect to the cathodes, and by virtue of electrolysis, the ions contained in an electrolytic solution 9530 are subsequently deposited on the cathodes as a sludge concentrate or metal cathode sludge. of recovery or as a solid cathode plating. In operation, the cathodes are typically removed simultaneously from cell 9420 in a batch process step, in order to collect the recovered metal. In cases where plate cathodes are used, the cathode can be flexed to delaminate or to remove hard cathode plating from the cathode. In other cases, where higher deposition (ie "cross-linked") wire mesh cathodes are employed, the concentrate is separated from the cathode in a subsequent process and the cathodes are then recycled. The mud concentrate can be collected at the bottom of the i cell 9420 and can be removed periodically. An electroextraction pump box 9420 and pump 9430 can be employed to temporarily store the spent electrolyte (ie, the sterile solution) that is removed from cell 9420 between batches.

The problems associated with the conventional acid washing systems 9100 'mentioned above, and the 9100 processes are numerous. For example, systems use non-continuous, independent "batches" of process steps, which require constant labor, downtime, and energy (eg, draining and continuously filling the same acid wash container 9120 with different agents rinse). In addition, such conventional, batch, acidic washing processes 9100 typically discard expensive acid, caustic and / or other reagents after each use. This increases overhead costs (for example, purchase costs, disposal costs) and creates unnecessary danger to the environment. In addition, each time a conventional 9120 acid wash container is drained and filled with a different rinse solution, the carbon (and minerals / precious metals attached to it) may not be recovered due to system inefficiencies caused by heat , friction, increased residence time in the pump, and increased exposure, an increased number of pipe elbows and valves, and frequent disposal of the spent rinse solution, which may still contain small amounts of carbon ', loaded and precious metal. In other cases (not shown) \ if separate containers are used for each rinse step of the acid wash process, as many as four tanks and ten pumps may be required. This increases the overall costs of the initial plant, and the general layout of the plant.

The problems associated with the conventional batch elution process 9200, described, are also numerous. For example, the 9200 process uses batch process steps that require constant labor and energy (eg, draining and continuously refilling the 9240 wash container with the new wash solution, the 9239 hot sterile solution, and the charged 9500 carbon is increasingly necessary electrolytic solution 9530 for electroextraction 9400). This increases the overall costs (for example, labor, maintenance), complicates the production schedule, and can cause damage to the environment. In addition, the 9000 'conventional metal recovery systems are bulky and require large plant placement areas as demonstrated by Figure 23, when compared to a 100' system for the continuous recovery of metals according to the invention (FIG. 22) which will be described later in the present. further, conventional elution systems have limited operating flow rates, limited temperatures and pressures, which promotes radiation losses and energy consumption. In addition, electroextraction of the metals using the conventional batch electroextraction processes 9400 described above requires stop-time intervals without production of the electrowinning cell 9420 and significant physical labor, which may contribute to premature wear of the cathode and wasted electrolytic solution 9530.

The process of using zinc to precipitate precious metals from stock solutions is also costly, can be less efficient for large-scale operations, works only on certain metals, and can! Result in less recovery of precious metals.

OBJECTIVES OF THE INVENTION Therefore, an object of the invention is to provide an improved metal recovery system, which is configured for continuous carbon loading / adsorption, continuous washing and debugging of charged carbon, continuous electrolyte formation, electroextraction! continuous and continuous regeneration / reactivation, thereby avoiding the aforementioned problems, associated with conventional, batch metal recovery processes.

Yet another object of the invention is to improve the efficiency of a metal recovery process, ie by minimizing radiation losses, reducing energy consumption, minimizing reagent consumption, and preventing the disintegration of metal. carbon and electrolyte loss).

Yet another objective of the invention is to prevent or minimize carbon loss and reagent waste.

Another objective of the invention is to maximize the total recovery of metals.

Yet another object of the invention is to provide a metal recovery system that is configured for lower cost and have a smaller work area than conventional metal recovery systems.

Yet another object of the invention is to provide a system and process for the recovery of metals, which is configured to operate at higher flow rates, temperatures and / or pressures than conventional processes. ' 1 A further object of the invention is to reduce the weight percentage of the unrecovered metal present in the spent electrolyte / sterile solution.

These and other objects of the invention will be apparent from the Figures and the description herein. Although it is believed that each objective of the invention is achieved by at least one embodiment of the invention, there is not necessarily some form of the invention that achieves all the objectives of the invention.

BRIEF DESCRIPTION OF THE INVENTION A system for the continuous recovery of metals is provided. The system comprises, according to some embodiments of the invention, at least one of a continuous acid washing system, configured to receive an uninterrupted, continuous influx of charged carbon particles, and the distribution of an uninterrupted output stream. , continuous carbonaceous particles charged, pickled; a continuous elution system configured to receive an uninterrupted, continuous inflow of a wash solution containing a carbonaceous, charged, pickled particulate material, and the distribution of an uninterrupted, continuous flow of the electrolyte solution; and a continuous electrowinning system, configured to receive an uninterrupted, continuous inflow of the electrolyte solution, the distribution of an uninterrupted, continuous flow of a sterile solution, and continuously and uninterruptedly forming a cathode mud concentrate. Each of the washing system has been continuous, the continuous elution system, and the continuous electroextraction system are generally configured to operate simultaneously without periodic interruptions that are common with conventional batch metal recovery processes.

In some embodiments, the system may comprise an integrated carbon regeneration system, operatively connected to the continuous elution system. A continuous carbon charge / adsorption system may be operatively connected to and upstream of the continuous acid wash system. The continuous acid washing system can be operatively connected to the continuous elution system; for example, via a holding tank between the 1 continuous acid wash system and the continuous elution system. One or more pumps can be provided to facilitate transportation of the suspension and solids within the system. In preferred embodiments, the continuous elution system is operatively connected to the continuous electrowinning system and comprises one or more meshes or filters configured to prevent the carbonaceous particles from passing into the continuous electrowinning system.

The continuous acid washing system may comprise a chamber adapted to retain a fluidization means; an inlet adapted to receive a feed containing charged carbonaceous particles; a fluidized bed distribution panel or other means adapted to fluidize charged carbonaceous particles in the presence of the fluidization medium; an aperture adapted to pass the charged carbonaceous particles and fluidization medium from the chamber; and a mesh adapted to filter charged carbonaceous particles from a fluidization medium. The continuous elution system may comprise a splash container, a continuous elution vessel, and a vaporization vessel, wherein the splash vessel is operatively connected to the continuous elution vessel in series, the continuous elution vessel is operatively connected to the vessel. vaporization vessel in series, and the splash container is operatively connected to the vaporization vessel in parallel. The continuous electrowinning system comprises an electrolytic cell having a cell body configured to maintain the electrolytic solution at a high pressure and / or temperature; at least one anode; at least one cathode; an input configured to receive an uninterrupted, continuous inflow current from the electrolytic solution; a first output configured to discharge an uninterrupted, continuous output current from the spent electrolyte solution; a second outlet configured to remove the mud concentrate from the cathode; and a residence chamber configured to continuously transfer the electrolyte solution from the inlet to the first outlet, and increase the residence time of the electrolyte solution between at least one anode and at least one cathode. The residence chamber may comprise one or more channels that are configured to provide a forced flow of the electrolyte solution therein that is strong enough to continuously discharge and / or transport the cathode sludge concentrate along one or more channels , and eventually outside the residence chamber.

The continuous elution vessel may comprise an inflow pipe and an outlet flow pipe which communicate with the first outlet and inlet of the electrolytic cell, respectively, and may further comprise a fluidized bed and / or one or more internal dampers which The flow trajectories are configured to be tortuous and increase a residence time of the charged carbonaceous particles in it. A valve configured to vaporize the solution leaving the continuous elution vessel and entering the vaporization vessel may also be provided.

The acid wash system continued may comprise at least one of an acidic solution, an aqueous solution and a caustic solution. The continuous elution system may comprise a solution containing at least one carbonaceous particulate material charged with a precious material, an electrolyte solution, spent carbonaceous particles, a caustic material, an aqueous component, and cyanide. The continuous electrowinning system 1 may comprise an electrolytic solution or a cathode mud concentrate. Each one of the layado system has been continuous, the continuous elution system and the continuous electrowinning system can be configured to increase a residence time, pressure or temperature of the solutions or suspensions contained therein and can comprise a mesh or filter element.

In some embodiments, the continuous acid lay system may comprise multiple wash containers, each wash container comprising a chamber adapted to retain a fluidization means; an inlet adapted to receive a feed containing a carbonaceous, charged particulate; a fluidized bed distribution panel or other means adapted to fluidize and clean the carbonaceous particles charged with the fluidization medium; an aperture adapted to pass the charged carbonaceous particles and fluidization medium from the chamber; and a mesh adapted to filter the particles 1 carbonaceous charged from the fluidization medium. For example, in some embodiments, the continuous acid wash system may comprise an acid wash tank containing an acid fluidization medium, an aqueous rinse tank containing an aqueous solution of substantially neutral pH, and a caustic rinse tank. which contains an alkaline fluidization medium; In some embodiments, the continuous acid wash system may comprise one or more recirculation tanks for collecting the spent fluidization medium, one or more landfills, channels, valves or drains to capture the spent fluidization medium. The continuous electrowinning system can be configured for continuous and uninterrupted collection, and removal of the cathode mud concentrate, and can comprise one or more channels defined between a cathode, an anode and an isolator. One or more channels may comprise portions of a helix, spiral, winding, compound curve, three-dimensional tilt curve, figure 8, or coil shape, and the cathode and anode may be formed as sleeves or tubes that are separated by the insulator. In some embodiments, the carbon regeneration system is operatively connected to the continuous elution system and the continuous carbon charge / adsorption system, and the continuous charge / adsorption system is operatively connected to the continuous acid wash system.

A process for the continuous recovery of a metal is also described. The process comprises, according to some modalities, continuously feeding a continuous washing system with the particles charged with a metal; washing continuously the charged particles inside a continuous washing system, to pick up the charged particles; continuously removing the charged pickled particles from the continuous washing system; continually loading a continuous elution system with the charged pickled particles; continuously remove the electrolyte solution from the continuous elution system; continuously feed a continuous electrowinning system with the electrolyte solution; continuously withdraw the spent electrolyte solution from the continuous electrowinning system; and, continuously distributing the spent electrolytic solution to the continuous elution system; wherein each of the continuous washing system, the continuous elution system and the continuous electrowinning system are configured to allow the above steps to be carried out simultaneously, without the periodic interruptions required for conventional batch processes.

The process may further comprise continuously removing the spent particulate material from the continuous elution system; continuously feed the spent particles to a carbon regeneration system; continuously withdraw the cathode mud concentrate from the continuous electrowinning system; and / or forming the charged particles by continuously adsorbing metal onto the particles in a continuous carbon adsorption / charging system, which is similar or identical to the continuous wash system. The particles may be of a carbonaceous particulate material, a polymeric adsorbent, and an ion exchange resin.

BRIEF DESCRIPTION OF THE FIGURES Figures 1 and 2 schematically illustrate a method and system for the continuous recovery of metals according to some modalities; Figure 3 is a flow chart of a continuous, acid washing operation of three sequences, according to some modalities; Figures 4 and 5 describe the steps of a continuous acid washing process, according to some modalities; Figures 6 and 7 describe a wash tank that can be used in the acid wash process shown in Figures 1-5; Figure 8 shows an acid washing system comprising a plurality of washing tanks described in Figures 6 and 7; Figures 9 and 12 schematically illustrate a system and method of continuous elution according to some modi? Cations; Figure 10 is an isometric view of a continuous elution system according to some modalities; , Figure 11 shows a sectional side view of the continuous elution system of Figure 10; Figures 13 and 19 schematically illustrate a continuous electroextraction system and method according to some embodiments; Figure 14 shows a top plan view of a continuous electrowinning system according to some modalities; Figures 15 and 16 are views in vertical and isometric section, respectively, of a continuous electrowinning system, taken on line XV-XV in Figure 14; Figure 17 is a detailed view of the Figure 15, which shows the particulates of an entry according to some modalities; Figure 18 is a cross-sectional view of an electroextraction cell along the line XVIII-XVIII in Figure 14; Figure 20 shows a process for the regeneration / deactivation of spent carbon according to some modalities; Figures 21 and 22 show a system for the continuous recovery of metals; Figure 23 shows a conventional batch system for the recovery of metals; Figure 24 shows an alternative to the wash tank shown in Figures 6-8 or an apparatus to be used for continuous carbon loading / adsorption; Figure 25 shows a detailed isometric view of the camera shown in Figure 24; Figure 26 is a sectional view of the camera shown in Figure 25; Figure 27 shows a conventional system for the recovery of metals; Figure 28 shows a conventional acid washing process; Figure 29 shows a conventional batch elution process; Y Figure 30 shows a conventional batch electroextraction process.

DETAILED DESCRIPTION OF THE INVENTION As shown in Figures 1 and 2, a plant system 100 'or process 100 for the continuous recovery of a metal from a mining ore may comprise, according to some embodiments of the invention, a 10' system or process 10 continuous acid wash, a 20 'system or continuous elution process 20, a 40' system or continuous electroextraction process 40, a system 30 'or continuous carbon regeneration process 30, and a system 70' or process 70 of charge / continuous carbon adsorption. Activated / reactivated carbon 56 (which can be derived by way of coconut husks or mineral carbon), or alternatively, an equivalent particulate substance such as charged polymeric adsorbent or charged ion exchange resin, is subjected to a process 70 of continuous adsorption of carbon, where it spends a residence time suspended in a mother solution containing a target recovery metal, dissolved such as gold, silver, copper, aluminum, platinum, uranium, chromium, zinc, cobalt, manganese or lead. The charging system 70 'or continuous carbon adsorption process 70 may comprise, for example, an apparatus as shown in Figures 6 and 7 or in Figures 24-26 which serves to fluidize the activated / reactivated carbon 56 within the mother solution. Once the carbon 56 is loaded with the target recovery metal, the latter undergoes a continuous acid washing process 10. The continuous acid washing process 10. The charged charged carbon 50 leaving the continuous acid washing process enters a holding tank 60 filled with a washing solution containing one or more reagents (e.g., water, caustic and cyanide) to form a suspension 51 of wash solution and loaded carbon 50 pickle. The suspension 51 enters a continuous elution process 20 where the temperature and / or the pressure of the suspension 51 is increased and the target recovery metal previously adsorbed by the carbon is re-leached into the wash solution, whereby an electrolyte solution 53 is formed which can be used for a continuous electroextraction process 40. The sterile solution 54 (is say, the spent electrolyte) that leaves the continuous electroextraction process 40 is returned to the continuous elution process 20 and / or 60 for reuse. A solid fraction 55 of spent carbon, depleted of its target recovery metal via the continuous elution process, is moved toward a carbon 30 regeneration process for reactivation before being reused in the continuous carbon loading / adsorption process. 70 As shown in Figures 2-5, a continuous acid wash process 10 can generally comprise the steps of feeding 1004 the charged carbon 57 into a continuous acidic wash system 10 ', the fluidization 1006 of the incoming loaded carbon 57 in an acid solution diluted within a first acid wash tank 12, extraction 1008 of the charged carbon from the acid wash tank 12, carbon screening 1010, charged, extracted, to remove the diluted acid solution, capture 1012 of the dilute acid solution 57c separated from the charged carbon, optionally the 1014 processing of the captured diluted acidic solution 57c (eg filtration, additives, pH adjustment), and the recycling of the captured diluted acidic solution 57c by feeding 1016 of the captured diluted acid solution 57c back to acid wash tank 12. Charged carbon rinsed with acid 57a that has undergone an acid bath in the The washing tank 12 is fed 1018 into the second aqueous rinse tank 14 containing water or another aqueous rinse solution of neutral pH 57d, and then fluidized 1020 into the second aqueous rinse tank 14. The process 10 further comprises the extraction 1022 of the rinsed charged carbon 57b from the second aqueous rinse tank 14, the sieve 1024 of the rinsed charged carbon 57b, to remove the aqueous rinse solution 57d, the capture 1026 of the separate aqueous rinse solution 57d, which is separated from the rinsed loaded carbon 57b, optionally processing 1028 of the aqueous rinse solution 57d captured (eg, filtration, additives, H setting), and recycling the aqueous rinse solution 57d by feeding 1030 of the aqueous rinse solution 57d again inside the second aqueous rinse tank 14. The rinsed charged carbon 57b which has been washed in the second aqueous rinse tank 14 1032 is fed into the third caustic rinse tank 16 which contains a caustic rinse solution 57e and is then fluidized 1034 in the caustic rinse tank 16. The continuous acid washing process 10 further comprises the 1036 extraction of wash solution and carbon loaded etching 50 from the caustic rinse tank 16, sieving 1038 from the washing solution and carbon loaded pickling 50 to remove the caustic rinse solution 57e, capture 1040 from the caustic rinse solution 57e separated from the washing solution and charged carbon 50 pickling, optional processing 1042 of the caustic rinse solution 57e captured (eg, by filtration, the provision of additives, or the pH adjustment), and recycling the caustic rinse solution 57e by feeding 1044 of the solution 57e back into the caustic rinse tank 16. The continuous acid washing process 10 can comprise the step of providing one or more pumps 13a, 13b for the recirculation of rinsing solutions in each of the aforementioned tanks 12, 14, 16. Optionally, a fourth rinse cycle (not shown) may be provided, and a person of ordinary skill in the art could recognize that one or more of the aforementioned washing steps can be repeated or alternated.

Returning now to Figures 6 and 7, an acid wash tank 200 for cleaning and stripping or charged particulate material, can be employed for any portion of continuous acid washing process 10. The charged particulate material, washing inside the acid wash tank 200 can be of any particle size, shape and density, which can be fluidized by or suspended within the fluidization means of cleaning. The acid wash tank 200 is advantageously configured to strip the active carbon particles that have been charged with a target metal, in preparation for the creation of an electrolyte for electroextraction. In such cases, the acid wash tank 200 can be filled with a fluidization medium comprising acid. Similar tanks 200 ', 200"can be used with the fluidization means comprising water and caustic soda.In addition, similar tanks can be used in other processes such as a continuous carbon loading / adsorption process 70, where the material in The particulate comprises activated / reactivated carbon 56 and the fluidization medium comprises a stock solution formed by the percolation of the cyanide and / or other reagents through a bed of heap leaching of crushed ore containing a target metal or mineral.

According to some embodiments, the acid wash tank 200 may comprise an acid wash tank having a first chamber 220, a first fluidized bed distribution panel 221, a first inlet 222, a first recirculation inlet 223a, first recirculation outlet 223b, first weir 224, first sieve 226, first overflow outlet 227, first discharge outlet 268, first recirculation tank 229, lower wall 260, internal tubular wall 266, an outer tubular wall 268, and a first channel 282 defined between the internal tubular wall 266 and the outer tubular wall 268 adjacent to the first weir 224. The first screen 226 serves to filter an inlet feed by the separation of its liquid fraction (per example, spent mother liquor, fluidization medium, or transport fluid) from its fraction of solid particles (charged or charged carbon, which carries metal). The liquid fraction drained from the particulate material is maintained in the first recirculation tank 229, and can be removed through the first recirculation outlet 223b. The first recirculation outlet 223b may be sealed during operation, coupled to a holding tank, coupled to a sump pump, or otherwise configured to feed an upstream or downstream process.

In some embodiments, as shown in Figure 8, the continuous acid washing process 10 'may comprise one or more separate washing tanks 200, 200', 200"connected in series in order to provide flexibility in the arrangement of the plant according to the personalized needs and / or reduce the total area In some cases, the tanks 200, 200 'and 200"may comprise similar or identical design features, c & one containing different fluidization means. For example, in some embodiments, a first tank 200 may comprise an acid wash tank containing a strong or diluted acid solution 57c, while the second 200 'and the third 200"tanks may comprise aqueous and caustic rinse tanks that they contain aqueous rinsing agents 57d and caustic 57e, respectively.While not required, tanks 200, 200 'and 200"can be constructed as" universal "or" interchangeable "tanks. In addition, tanks 200, 200 'and 200"can be configured with tubular shapes (eg, cylindrical tube or prismatic extrusion) as shown in order to reduce manufacturing costs One or more of the tanks 200, 200' and 200"can be replaced with a tank of similar scale or a tank 2000 as shown in Figures 24-26, which will be described later.

A first fluidization means which comprises a solution of dilute acid or anti-fouling agent can occupy the first acid wash tank 200. In some embodiments, the first fluidization means can comprise a solution of 1 to 10% vol / vol. of mineral acid / such as nitric acid or hydrochloric acid, configured to dissolve the carbonate scale. In use, the! charged / charged carbon 57 incoming moves on the first sieve 226 and flows into the first chamber 220 of the first! acid wash tank 200 via the first inlet 222. The fluid that may be present within the loaded / recharged carbon 57 drained and enters the first recirculation tank 229. The charged, screened carbon subsequently drops in a downward direction along the first sieve 226 and towards the first fluidized bed distribution panel 221, and is fluidized by the first fluidization means. - The first fluidizing medium enters the first recirculation inlet 223a and passes through the distribution panel 221. The first clarified fluidization medium is raised above the highest suspended level of the charged carbon within the first acid wash tank 200. and is emptied onto the first weir 224 and into the first channel 282. After this, the first clarified fluidization medium leaves the first acid wash tank 200 via the outlet 227 and optionally feeds the first recirculation inlet 223a and the first panel fluidized bed distribution 221. One or more pumps 13a may be provided between outlet 227 and inlet 223a.

A suspension of the charged carbon rinsed with acid 57a and the first residual fluidization means leaves the first acid washing tank 200 through the first discharge opening 228 and enters a second aqueous rinsing tank 200 'through a second inlet; 232. The charged carbon rinsed with acid 57a can be transported to the tank 200 'using only gravitational forces, or the rinsed loaded carbon with acid 57a can be transported to the tank 200' using one or more suspension pumps (not shown). A second fluidization means such as an aqueous neutralization solution of substantially neutral pH, or hot water may occupy the second aqueous rinse tank 200 '. In use, the charged carbon rinsed with acid 57a and the first fluidization means moves on a second screen 236 or equivalent filter, and then flows into the second chamber 230 for pre-rinsing. The second screen 236 serves to separate the liquid from the first residual fluidization medium from the acid-laden charged carbon 57a, wherein the first drained fluidization means is maintained in the second recirculation tank 239 and can be withdrawn through the second recirculation tank 239. recirculation outlet. The second recirculation outlet 233b may be coupled to a holding tank, a filtration apparatus, or an upstream or downstream process. For example, as indicated schematically by the dashed line path of the diluted acid solution 57c ', the second recirculation outlet 233b may be operatively connected to the first recirculation inlet 223a to fluidize the loaded / recharged carbon 57 within the first wash tank 200. Although not shown, one or more pumps may be placed between outlet 233b and outlet 223a.

After passing over the second screen 236, the charged carbon rinsed with acid 57a subsequently drops to a second fluidized bed distribution panel 231 and is fluidized within the second chamber 230 by a flow of the second fluidization medium entering the second. recirculating inlet 233a and passing in an upward direction through panel 231. The second clarified fluidization medium, free of charged carbon particles, rises above a suspended level of the acid-laden carbon loaded, and is emptied over a second weir 234 and to a second channel 284, where it exits the second aqueous rinse tank 200 'via the outlet 237 and optionally feeds the second recirculation inlet 233a and a second fluidized bed distribution panel 231 as schematically illustrated by the dashed line trajectory taken by the aqueous rinse solution 57d.

A rinsed charged carbon suspension 57d and the second fluidizing medium exits the second flushing tangent 200 'through the second flushing opening 238 and enters a third flushing tank 200"through a third inlet 242. The rinsed loaded carbon 57b can be transported to the third caustic rinse tank 200" i using only the gravitational forces ,! or the rinsed loaded carbon 57b can be transported to the tank 200"using one or more pumps (not shown) A third fluidization means such as a caustic rinse solution can occupy the third wash tank 200". For example, the third fluidization medium may comprise an amount of sodium hydroxide (NaOH) or potassium hydroxide (KOH) between 0.5% and 5% by weight, for example 1% by weight. The third fluidization medium may comprise other reagents, for example 1 to 10% by weight of sodium cyanide (NaCN). The third fluidization medium can be heated (for example, from 20 to 100 degrees C). In use, a rinsed charged carbon suspension 57b and the second fluidization medium flows onto a third screen 246 or equivalent filter and into the third chamber 240. The third screen 246 serves to filter the suspension by separating its second liquid fraction from the medium of fluidization of its solid fraction of the rinsed charged carbon 57b. The second separate fluidization means is maintained in a third recirculation tank 249. The second fluidization means can be removed from tank 249 via a third recirculation outlet 243b which can be coupled to a holding tank., filtration apparatus, or one or more processes upstream or downstream. For example, if it is indicated schematically by the path taken by the aqueous rinse solution 57d ', the third recirculation outlet 243b can be operatively connected to the second recirculation inlet 233a in order to help fluidize the particles within the second 200 'washing tank. Although not shown, one or more pumps may be placed between the outlet 243b and the entrance 233a. In some cases, the outlet 243b and the entrance 233a can be operatively connected to a plant water system.

After passing over the third screen 246, the rinsed charged carbon particulate material twice subsequently drops to a third fluidized bed distribution panel 241 and is fluidized within the third chamber 240 by a medium flow of the third fluidization medium. which enters the third recirculation inlet 243a and which passes through the panel 241. The third clarified fluidization medium rises above the highest level of suspension of the charged, fluidized carbon within the tank 200"and is emptied over a third weir 244 and to a third channel 286, where it leaves the caustic rinse tank 200"via the outlet 247 and optionally feeds the third recirculation inlet 243a as indicated by the dashed line path taken by the caustic rinse solution 57e.

A charged carbon 50 pickle, rinsed with caustic, and the third fluidizing medium leaves the third caustic rinse tank 200"through the third discharge opening 248 and may subsequently be screened or filtered for further processing. leaving the tank 200", the charged carbon, pickling 50 within the suspension can be separated from the third liquid fraction of the fluidization medium by a screen or filter (not shown) and then added to a solution of water washing, caustic and cyanide in a holding tank 60 for use in the continuous elution 20 downstream and in the electroextraction process 40.

The acid wash system 10 'shown and described, when used, reduces or eliminates the need to continuously buy and replace the lost amounts of the carbon particulate material, water, caustic material, acid and / or other anti-aging agents. -incrustation. The 10 'system also significantly reduces the amount of spent solution and carbon that requires waste, and reduces the potential for environmental damage.

It should be known that the particular characteristics and suggested uses of the continuous acid washing system 10 'described herein are exemplary in nature and should not limit the scope of the invention. For example, the fluidized bed portions 221, 231, 241 may be replaced with, or used in combination with one or more mechanical or forced air agitators (not shown) for suspending the charged carbon particles, in the fluidization medium. In addition, the number of cameras 220, 230, 240 by the 10 'system may be greater or less than that which is shown. In some embodiments, the relative sizes, dimensions and / or volumes of the cameras 220, 230, 240 may vary. In other embodiments, the cameras 220, 230, 240 may be of suitable dimensions and similarly provided. In addition, one or more tanks 200, 200 '200"can be placed in parallel with each other, in order to increase the performance, For example, a third caustic rinsing tank 200" of a system 10' can be directly or indirectly coupled to a plurality of upstream aqueous rinse tanks 200 '. Multiple tanks 200 can replace any of the single tanks 200, 200 ', 200"in the system 10', by dividing the inputs 222, 223a, 232, 233a, 242, 243a and / or the outputs 223b, 227, 233b , 237, 243b, 247. In addition, any of the cameras 220, 230, 240 can be compartmentalized into multiple chambers, as previously stated, the system 10 'or portions thereof can be used to continuously charge the activated carbon in a process Charge / continuous adsorption of carbon 70. For example, the feed particulate material may comprise activated or reactivated carbon and the first, second and third fluidization means may comprise a stock solution (eg, sodium cyanide solution (NaCN) containing a dissolved precious metal).

Figure 9 illustrates a continuous elution process 20 according to some modalities. A feed suspension 51 of the wash solution and the pickled charged carbon 50 is moved to a splash container 22 by means of gravity or one or more pumps 23. The splash container 22 increases the temperature and / or pressure of the inbound suspension 51, and distributes the hot pressurized suspension 51a to a continuous elution vessel 24. In the continuous elution vessel 24 the target metal previously adsorbed on the charged carbon is leached into the wash solution to form an electrolytic solution 53. The electrolytic solution 53 is filtered by one or more sieves to remove the spent carbon and the unwashed charged carbon, from Ta electrolytic solution 53, before being moved to a continuous electroextraction process 40. The electrolytic solution 53 can be transported to the electronic process.continuous traction via an effluent pipe 28b provided on the continuous elution vessel 24. The spent suspension 51c of the washing solution and the spent carbon is vaporized by a valve 29 and enters a vaporization vessel 25, where the steam is captured and returned to the splash container 22 via a steam return pipe 21 to help heat and pressurize the splash container 22 in an efficient manner. The resulting concentrated spent suspension 51d is separated into the solid 55 and liquid 52 using a. dehydration screen 26. The liquid fraction 52 of the spent spent suspension 51d can be returned to the holding tank 60, and the solid fraction 55 of the spent spent suspension 51d (ie, dehydrated, spent carbon) can be sent to a 30 carbon regeneration process for reactivation. The sterile solution 54 returning from a continuous electroextraction process 40 is generally heated with an immersion heater 27 and then sent back to the continuous elution vessel 24 via one or more pumps 23 and an incoming fluid line 28a.

Figure 10 shows a continuous elution system 20 'according to some modalities. The continuous elution system 20 'comprises in general a first splash container 22, a second continuous elution vessel 24 and a third splash vessel 25 connected in series via pipe sections, and a vapor return 21 extending between the splash containers 22 and vaporization 25 in parallel. One or more pumps 23 may be provided in various portions of system 20 ', in order to facilitate flows to, from and between containers 22, 24, other parts of system 20' and / or other portions 10 ', 30'. , 40 'inside a 100' system for the continuous recovery of metals.

As shown in Figure 11, the continuous elution vessel 24 comprises a fluidized bed distribution panel 320 which separates a residence chamber 340 from a fluidisation chamber 350. One or more baffles 318 may be provided within the chamber residence 340 in various configurations (eg, number, angle, spacing, geometry), in order to increase the residence time of the incoming hot pressurized suspension 51a within the continuous elution vessel 24. One or more deflectors 318 may be parallel and staggered to create a serpentine flow path 51b of the hot pressurized suspension 51a. Baffles 318 can be parallel, non-parallel, staggered at a predetermined simple angle, or placed in an alternating manner with each deflector oriented at a different predetermined angle. It should be understood that other deflector patterns and arrangements thereof may be used without limitation, and that the shapes, porosities and / or textures of the deflectors 318 may differ from what is shown. For example, one or more of the baffles 318 may comprise folds, bends, curves, corrugations, openings, network structures or the like.

The suspension flowing within the continuous elution vessel 24 may contain the incoming hot pressurized suspension 51a and the sterile solution 54 leaving a continuous electrowinning system 40 'or process 40. The fluidization chamber 350 may be fed by a flow line inlet 28a connected to the continuous elution vessel 24 via one or more inflow gates 326 having inflow gate assemblies 322. Alternatively, the inflow pipe 28a may rather be directly connected to one or more walls; laterals 310 of the continuous elution vessel 24. A sterile solution co-current 54 flows into the continuous elution vessel 24 via the inflow line 28a. The stream enters and fills the fluidization chamber 350 and flows through the fluidized bed 320 to help fluidize and suspend the carbon particles within the residence chamber 340 as it travels along the path; flow in serpentine 51b.

An effluent pipe 28b is also provided to the continuous elution vessel 24 for extracting an electrolytic solution 53 from the residence chamber 340 and distributing the electrolytic solution 53 to a system 40 'or continuous electroextraction process 40. The effluent pipe 28b comprises one or more effluent pipe gates, which can be provided with effluent pipe gate assemblies for ease of connection to the vessel, of continuous elution 24. Similarly to the inflow pipe 28a, the pipeline of effluent 28b may be directly connected to one or more side walls 310 of continuous elution vessel 24, or may be connected to vessel 24 via one or more effluent gates 316 having effluent gate assemblies 312.

While in the residence chamber 340 of the continuous elution vessel 24, the charged carbon is exposed to the reagents of the layered solution under high temperature and high pressure conditions. The reagents in the washing solution act to wash the charged carbon from its previously adsorbed metal contents (eg, gold), and "re-leach" it to the solution to form an electrolyte solution. One or more sieves or filters 324 may be provided between the residence chamber 340 and the effluent line 28b, in order to extract a clarified stream of the electrolyte solution 53 from the continuous elution vessel 24 and / or prevent the particles from carbon pass downstream of the effluent pipe 28b. In some embodiments, as shown, the placement of the screens or filters 324 may be at the interface between the effluent gates and one or more side walls 310 of the continuous elution vessel 24. However, the screens or filters 324 may be provided in other sites without limitation, for example: within the effluent pipe 28b within the continuous elution vessel 24, at the interface between the effluent pipe 28b and the assemblies 312, or downstream of the effluent pipe 28b. It should be known that one or more seals or gaskets (not shown) can be placed between the inflow lines 28a or effluent 28b and the elution vessel continues 24.

The fluidized carbon and the solution within the residence chamber 340 continue to move along the coil flow path 51b, until it is either withdrawn through the effluent pipe 28b to be used as an electrolyte, or passes to through outlet 328. Exit 328 may comprise an outlet assembly 330 and / or an exit seal 329 to be connected to a valve 29. Valve 29 may be of any kind known in the art, such as a ball valve or cone without limitation, and one would appreciate that the valve can be separately to, or integrally formed with either or both of the continuous elution vessel 24 and the vaporization vessel 25. In addition, additional pipe sections can be added between the second outlet 328 and the valve 29 if the distance between the continuous elution vessel 24 and the vaporization vessel 25 is large.

The hot pressurized spent suspension stream 51c leaving the continuous elution vessel 24"vaporizes" as it passes through the valve 29. The resulting mixture of the gaseous vapors, fluids and solids enters the vaporization vessel 25 further low pressure, where the heated vapor is diverted back to the splash container 22 via the steam return pipe 21. The spent non-vaporized solution and the spent carbon leave the vaporization vessel 25 in a concentrated spent suspension stream 51d . The concentrated casted suspension 51d may comprise a liquid fraction of sterile solution 52, and a solid fraction 55 of spent carbon, substantially free of the previously adsorbed precious metal (eg, gold). As previously mentioned, the spent suspension stream, concentrated 51d. it can be subsequently screened or filtered by a dehydration screen 26.

In the embodiment shown, a liquid fraction 52 of the spent spent suspension 51d is separated from the solid fraction 55 by the dehydration screen 26 and returned to the holding tank 60 for re-dilution as the wash solution. One or more pumps (not shown) can be provided to remove the liquid fraction 52 to the holding tank 60. The solid fraction 55 of spent dehydrated carbon is sent to a carbon regeneration process 30 comprising a regeneration furnace 35 or other means to reactivate carbon. Dehydration screen 26 can be provided as a two-stage screen, wherein a first stage removes a greater part of liquid fraction 52 from the fraction of spent carbon solids 55, and a second stage removes caustic and / or liquid. residual cyanide from the solids fraction 55 of the spent carbon, before it enters a regeneration furnace 35 or washing vessel. Accordingly, the equipment in the carbon regeneration system 30 'is not damaged.

Figure 12 illustrates schematically a continuous elution process 20 according to some modalities. First, a suspension 51 of the etched carbon 50 and a caustic wash solution comprising water and cyanide is produced 1048. The suspension 51 can be formed and stored in a holding tank 60. The suspension 51 is then pumped 1050 into the vessel. splash 22 which is configured to raise the temperature and / or the pressure of the loaded carbon suspension pickle / wash solution 51. After increasing the temperature and / or pressure 1052 of the suspension 51 in the splash container 22 , a hot pressurized suspension 51a of the charged carbon solution / wash solution is formed and moved 1054 from the splash container 22 to the continuous elution vessel 24. The hot pressurized suspension 51a is held within the container 24 by a increased residence time 1056, for example, by the provision of a fluidized bed 320 alone or in combination with a plurality of deflectors 318, in order to lengthen the physical travel path of the hot pressurized suspension 51a between the inlet 304 of the container 24 and the outlet 328. The physical travel path may be, for example, a coil flow path 51b as it shows.

During its residence time inside the continuous elution vessel 24, the carbon charged in the hot pressurized suspension 51a is stripped of its adsorbed precious metal, by the reagents in the caustic wash solution. Accordingly, the caustic wash solution dissolves the precious metal itself whereby an electrolytic solution 53 is formed. The electrolyte solution 53 is screened to remove the carbon particles therefrom and is removed 1064 from the continuous elution vessel 24. Subsequently, the electrolytic solution 53 I 1066 is fed to a continuous electroextraction system 40 '(for example, inside a metal, electrolytic, continuous extraction cell 42) for the recovery of precious metal. During the electrowinning process 10/68 (see Figure 19), the sterile solution 54 is continuously withdrawn 1070 from the continuous electrowinning system 40 ', and pumped 1072 back to the continuous elution vessel 24 either directly, or indirectly (e.g. , via a holding tank of the sterile solution (not shown) or the immersion heater 27).

The solution and the carbon are continuously removed from the continuous elution vessel 24, and the liquid fraction from the solution "vaporized" or at least partially vaporized with a valve 29, before entering the vaporization vessel 25. The process 20 further comprises the recovery 1060 of the hot steam from the rapid evaporation of the spent outlet suspension 51c, and the pipe 1062 the steam back to the spill container 22 in order to efficiently increase 1052 the temperature and / or pressure of the first container 22. The spent spent suspension 51d is removed 1074 from the steaming vessel 25, and then dewatered 0076 to separate the spent liquid fraction 52 from the spent solids fraction 55. The solids fraction comprises dehydrated carbon which is sent to a system 1078 of regeneration of carbon 30 ', and the spent liquid fraction 52 of the spent spent suspension 51d is sent i 1080 to the holding tank 60 for reuse.

It should be known that the particular characteristics and suggested uses of the continuous elution systems 20 'and the processes 20 shown and described herein; they are exemplary in nature and should not limit the scope of the invention. For example, the fluidized bed 320 may be replaced with, or used in combination with, one or more mechanical agitators (not shown) to suspend the charged carbon particles. In addition, the number of baffles 318 in the continuous elution vessel 24 may be greater or less than that shown, in order to provide the residence times and the flow rates required for a particular process. In addition, one or more additional containers 22, 24, 25 can be added to a continuous elution system 20 ', and placed in series or parallel with other containers 22, 24, 25 to increase the yield. For example, two or three continuous elution vessels 24 can be directly or indirectly coupled to one another in parallel, and placed in series between a simple splash container 22 and a simple vaporization vessel 25.

Figure 13 shows a continuous electroextraction process 40 according to? some modalities The process 40 comprises the continuous provision of an electrolytic solution 53, the continuous feeding of the electrolytic solution 53 to a continuous electrolytic metal extraction cell 42, the extraction of the cathode mud concentrate 53f from the cell 42 in a current of sludge removal 53g, continuously withdrawing the sterile solution 54 from cell 42 and using the sterile solution 54 to feed a continuous elution vessel 24 into a continuous elution process 20.

As shown in Figures 14-18, the continuous electrowinning system 40 'comprises mainly a continuous electrolytic metal extran cell 42 comprising a cell body 406 having a first end 440, a second end 480, one or more side walls 482 extending between them, a base 404 having one or more assemblies 402, at least one inlet 410 for receiving a continuous inflow current of an electrolytic solution containing precious metal 53, at least a first outlet 420 to provide the continuous output of a spent electrolytic current 53d , and the sterile solution 54 contained therein, and at least a second outlet 430 to provide the outlet of the cathode mud concentrate 53f collected within the cell 42. The second outlet 430 may be configured for the continuous output of the mud concentrate. cathode 53f, harvested, or the second outlet 430 can be configured for the intermittent output of the caustic slurry concentrate all collected 53f. Within the cell body 406 there is provided a first chamber 405, a second chamber 407, a third chamber 408, and a residence chamber 460 comprising one or more elongated channels 462. The channels 462 are configured to increase the residence time of the electrolytic solution 53, and to provide a forced flow electrolytic current 53b of the electrolytic solution 53 therein, which is strong enough to detach and / or displace the cathodic sludge concentrate that is formed and which accumulates within channels 462. One or more channels 462 may comprise, for example, a portion of a helix, double helix, winding, spiral, coil, groove, compound curve, and can extend in curvilinear trajectories. In some embodiments, as shown, the residence chamber 460 may be concentrically located between the first chamber 405 and the third chamber 408. The first chamber 405 may be configured to be devoid of the electrolyte and / or the cathodic mud concentrate during the operation, and may serve in general as a space filler, joined between the first end 440, the internal anode 477 and the baffle 450. The space filling first of the chamber 405 generally provides the channels 462 within the residence chamber 460 with a larger radius1, thereby increasing the total effective length and the total surface area of the channel 462 exposed to the forced-flow electrolyte streams 53b, contained therein. The third chamber 408 serves to temporarily maintain and / or transport the spent electrolytic currents 53d from within the cell 42 to one or more first outlets 420. In some embodiments, to reduce material costs, the first end 440 can be configured as an annular panel having a central opening that exposes the first chamber 405, instead of as a solid continuous circular panel as shown. One or more first outlets 420 may be provided in an upper portion of the cell 42, where the overflow is more likely to be more clarified and free of the cathodic slurry concentrate.

Each channel 462 may be defined between at least one anode 474, at least one cathode 472 and one or more insulators 476 extending therebetween. In the particular embodiment shown, one or more anodes 474 and one or more cathodes 472 are provided as sleeve portions that alternate concentrically between an external anode 479 and an internal anode 477 with each sleeve portion that has! a different radio. The anodes 474 and the cathodes 472 are radially spaced apart and maintain uniform spacing by one or more spacing protrusions 473 protruding from one or more cathodes 472. It should be understood, that while not shown, one or more protuberances 473 may extend. alternatively from anodes 474 alone, or; they may extend from anodes 474 and cathodes; 472 without limitation. However, by providing the protrusions 473 on one or more cathodes 472, a small amount of extra cathodic surface area is provided for the precipitation of the cathodic mud concentrate out of the forced flow electrolytic stream 53b: during electrolysis . One or more insulators 476 prevent the short circuit between the negatively charged anodes 474 and the positively charged cathodes 472, they can serve as flexible tolerance compensation packages that delineate the cross-sectional limit of each channel 462 and accumulate / concentrate the electrolytic current of forced flow 53b within each channel 462.

As shown in Figure 18, each anode 474 may communicate with one or more anode terminals 442. The anode terminals 442 may comprise, for example and without limitation, a fastener 442a such as a dowel or screw, a clamping member 442b such as a nut, flange or head, a terminal guide 442c connected to a ground or power source, a conductive washer 442d or another clamping member, an insulating bushing 442e for preventing electrical currents from passing to the surrounding portions of cell 42, an equivalent assurance thread or feature 442f provided on fastener 442a, a conductive support 442h comprising a complementary thread or equivalent assurance feature 442g to communicate with the thread or equivalent assurance feature 442f, and a receiving portion 442i provided within the conductive holder 442h for coupling and support of one or more anodes 474. In the particular embodiment shown, the anodes 474 are in general tubular cylindrical sleeves and therefore, the receiving portions 442i can be provided as small straight or generally arched slits. However, other equivalent interconnections are considered, particularly for anodes 474 and non-cylindrical or non-tubular cathodes 472. For example, instead of the slits, the receiving portion 442i may comprise a plurality of conductive clamps, spring clips or legs extending from the bracket 442h that straddle and secure an anode 472 thereto.

In some embodiments, the continuous electrowinning system 40 'may be provided with a cylindrical cell body 406, a first flat upper end 440, and a second generally frustoconical lower end 480. The frusto-conical shape of the second lower end 480 in general helps in the channeling of the cathodic mud concentrate 53f, weighed, collected to the second outlet 430 for the removal. The first end 440 can be secured to the cell body 406 via an annular flange 445 which can be electrically neutral or positively charged with the remainder of the cathodic cell body 406. The first end 440 can comprise a series of sandwich panels, such as one or more; neutral or electrically neutral panels 447, one or more anodic panels 444, and one or more insulating panels 446.; In some embodiments, one or more insulating panels 446 may comprise a package, such as an insulating package of polytetrafluoroethylene (PTFE). One or more fasteners 441 or adhesives may be provided to secure: the first end 440 to the body 406 and / or to secure the sandwich panels 444, 446, 446 together. For example, a series of fasteners 441 may be provided around a perimeter of the first end 440, to secure the first end 440 to the flange 445. The fasteners 441 may be insulated, for example, with a sheath, cover, liner or washer of non-conductive material such as high molecular weight polyethylene (HMWPE), polyvinylidene fluoride (PVDF), polypropylene or polyvinyl chloride (PVC). In addition, fasteners 441 can serve the double purpose of securing the first end 440 to the body 406, and i also securing the sandwich panels 444, 446, 447 entered yes.

In use, an inflow current of the electrolytic solution 53 at a pressure and temperature i greater than the environmental ones continuously enters the cell 42 via the inlet 410. The electrolytic solution 53 may contain copper, gold, silver, platinum metal ions , lead, zinc, cobalt, manganese, aluminum or uranium, without limitation. The continuous electroextraction system 40 'is preferably maintained at a higher temperature and / or pressure than the ambient ones (for example, around 88 degrees C). The tributary stream of the electrolytic solution 53 comes from an upstream electrolyte holding tank (not shown), a continuous elution system 20 ', or a combination thereof. In some embodiments, the inlet 410 may be formed from a portion of a tube or pipe having one or more side walls 412 and may further comprise an inlet assembly 414 having a flange, seal, valve, pipe fitting or equivalent connector for integration with the continuous elution system 20 '. The inlet 410 comprises one or more openings 413 (for example, through one or more side walls 412), which are configured to feed one or more channels 462 of the residence chamber 460 with the incoming electrolytic solution 53. Although not it is shown, a plurality of openings 413 can be provided by each channel 462. In the case of multiple channels 462 and a single input 410 which are employed as shown, the inflow current of the electrolytic solution 53 can be divided into a plurality of dispense influx currents 53a, each entering different channels 462. Alternatively, while not shown, a separate input 410 may be provided for each channel 462. The openings 413 may be configured to provide uniform or non-uniform flow rates through each channel 462, or provide similar electrolyte residence times for each channel 462. As clearly shown in Figure 17, one or more insulators 417 (eg, an insulation pad) can be placed between one or more side walls 412 of the inlet 410 and the first end 440 of the cell body 460. One or more insulators 417 can surround circularly one or more openings 413 to ensure that the incoming electrolytic solution 52 from the disperse tributary streams 53a does not form, form sheet or mud within the openings 413, particularly the adjacent cathodes 472.

In some embodiments, the channels 462 can be configured to allow the dispersed tributary streams 53a of the electrolytic solution 53 to flow forcefully through the channels 462 in a forced flow electrolytic stream 53b following a uniform helical or spiral path, as shown in FIG. sample. However, while they are not shown, channels 462 can also be configured to direct currents; scattered tributaries 53a along straight paths, coil paths, composite curve paths, or complex three-dimensional groove curve trajectories, as long as they can withstand a forced flow electrolytic current 53b therein and provide sufficient residence time of the electrolyte between an anode 474 and the cathode 472.

The channels 462 may shrink or grow in circumference, or change completely or in cross section and / or in size as they extend within the residence chamber 460; however, it is preferred that the channels 462 remain uniform in cross section, in direction and / or anode-cathode spacing throughout their entire length. While not shown, since channels 462 located at greater radial distances from the center of cell 42 are longer and will generally have residence times higher than internal channels 462, the number of turns of internal channels 462 (for example, channels adjacent to the internal anode 477 and the first chamber 405) can be adjusted to be greater than the number of turns for the external channels 462 (for example, the channels closest to the external anode 479 and the third chamber 408). In other words, while not shown, the internal portions of the residence chamber 460 may be greater in height '; that the external portions of the residence chamber 460, in order to lengthen the effective length of the intermediate channels 462 (adjacent to the first chamber 405). The portions of the baffle 450 adjacent to the residence chamber 460 and the third chamber 408 are generally open to allow the channels 462 to continuously distribute the spent electrolytic streams 53d to the third chamber 408, and the collected cathodic mud concentrate 53f formed in the channels 462 to the second chamber 407.

As shown in Figure 16, baffle 450 may comprise an anode layer 452, an electrically neutral intermediate insulator 454 for supporting one or more anodes 474 and cathodes 472, and a support structure 456 for supporting insulator 454 and layer Anodic 452. Isolator 454 can be made from a chemically strong material such as ultra high molecular weight polyethylene (UHMWPE) and can be cruciform as shown. A plurality of receiving portions 458 such as notches may be provided to the insulator 454 to retain, space, isolate and support one or more anodes 474 and cathodes 472; however, other retaining means such as legs, spring clips or clamps may be provided. The insulator 454 can be connected to the support structure 456 with one or more fasteners, adhesives or other connection means, and the support structure 456 can be connected to the body 406 by conventional means such as bolting, forming, bonding, welding or Support on a flange or shelf. The anodic layer 452 can serve to close the first chamber 405 and prevent the electrolyte 53 in the forced flow electrolytic current 53b between the first chamber 405. In some embodiments, the support structure 456 can be a network structure such as a mesh screen or support member such as a cross bar spanning a width of the cell body 406. The support structure 456 is generally configured so as not to inhibit the electrolyte from flowing from the channels 462 to the third chamber 408.1 or inhibit the passage of the cathodic mud concentrate 53f to the second chamber 407.

As . the electrolytic solution 53 forcibly flows through one or more channels 462 in the residence chamber 460, a large electrical potential is placed between one or more anodes 474 and one or more cathodes 472 in order to effectively "veneer" the concentrate sludge on one or more cathodes 472. However, by varying operating parameters such as residence time, electric current, electrolyte flow rate, temperature, pressure, concentration / composition of the electrolyte and smoothness / material / coating of each of the cathodes 472, the channels 462 can be configured such that the cathodic mud concentrate initially forms on or adjacent to one or more cathodes 472, but will not effectively bind or "plate" the cathodes 472 and instead it will flow down the channels 462 and / or suspend in the forced flow electrolytic streams 53b. Any sludge concentrate that can settle to the bottom of a channel 462 can also be washed and eventually swept out of the channels 462 and into the second chamber 407 by the forced flow electrolytic streams 53b. The mud concentrate can be flushed out of one or more channels 462 by virtue of: the gravitational forces acting on the inclined surfaces, the high flow velocities of the forced flow electrolytic streams 53b passing through one or more channels 462, increased turbulence within each channel 462, and / or by virtue of the small cross-sectional areas provided to each channel 462.

After the forced flow electrolytic streams 53b pass through one or more channels 462, the external flow 53c of the residence chamber 460 will generally comprise a liquid carrier component of the: sterile solution 54 which is substantially free of precious metal dissolved, and a solid precipitate component comprising cathodic mud concentrate that has been discharged from the i channels 462 by the forced flow electrolytic current 53b. The heavier solids may follow a stream of the sludge precipitate 53e before settling into a cathodic harvested concentrate mass 53f within the second chamber 407 adjacent the second end 480. The sterile solution 54 travels via the spent electrolytic current 53d within the third chamber 408 and continuously leaves the cell 42 through the outlet 420. In embodiments where the cell body 406 is cathodic, some residual plating or cathodic mud concentrate formation may occur within the third chamber 408 (for example, on or around the internal portions of the cathodic wall or walls 482). However, any cathodic mud concentrate 53f formed within the third chamber 408 will typically settle and eventually end up in the second chamber 407 with the remainder of the collected cathodic mud concentrate 53f.

The first outlet 420 may be formed from a portion of a pipe or pipe having one or more side walls 422 and may further comprise a first outlet assembly 424 having a flange, seal, valve, pipe fitting, or connector equivalent for integration with a 20 'continuous elution system. When in use, an effluent stream of the sterile solution 54 continuously leaves the cell body 406 through the first outlet 420, at which point it can enter a sterile solution holding tank (not shown), be discarded, return to a 20 'continuous elution system or undergo further processing.

The captured cathodic sludge concentrate 53f can be removed from the cell 42 intermittently in a continuous manner via the second outlet 430. The lower stream, or sludge removal stream 53g, of the cathodic sludge concentrate 53f can proceed to a holding tank, be pumped away for later refining, or it can be placed inside a container and transported to a smelter. In some embodiments, the second outlet 430 may be formed from a portion of a tube or pipe having one or more side walls 432 and may also comprise a second outlet assembly 434 having a flange, seal, valve, tube, accessory, nozzle., key or equivalent connector for integration with a holding tank or casting apparatus.

The cross section of the residence chamber 460 may vary, as long as one or more channels 462 therein are formed between at least one anode 474 and at least one cathode 472 that are separated from each other by one or more insulators 476. The channels may extend linearly (resembling a elongated tube), helically, in a cascade of "Figures in 8, connected, horizontally accommodated and vertically displaced, or in any continuous path in the three-dimensional space that is configured to provide a" forced flow "of the electrolytic solution. In order to help with the degassing of the air that could become trapped in the channels 462 and also prevent the accumulation of the precipitated mud concentrate inside the channels, it is preferred that the continuous path that follows in the channels in: the three-dimensional space, is free from sharp bends, abrupt turns, protruding parts, high points and / or tightly rolled corners that may be prone s to air capture and plugging. In some embodiments, a residence chamber 460 may comprise one or more channels 462 therein that simply extend as long straight tube sections inclined at an angle with respect to the horizontal.

Figure 19 illustrates schematically a continuous electroextraction process 40 according to some modalities. The process 40 comprises the provision 1082 of an electrolytic solution 53 having a temperature f pressure elevated with respect to the ambient conditions. The electrolytic solution 53 can be produced from a continuous elution process 20 and can comprise water, cyanide, caustic and a loose metal (e.g., gold, copper, silver, platinum, aluminum, lead, zinc, cobalt manganese or uranium) in this one. The electrolytic solution 53 is continuously fed 1084 (for example at a predetermined flow rate) into a continuous electrolytic metal recovery cell 42 which is preferably held 1086 at a higher temperature and / or pressure than ambient. In some embodiments, cells 42 may comprise a series of nested anode sleeves 474 and cathode sleeves 472, where the adjacent sleeves have different electrical potential or charge. In a preferred embodiment, the sleeves are spaced concentrically and radially uniformly with respect to each other, so that any two neighboring sleeves maintain an opposite load 1088. Nail or more insulators 476 can be placed between the anodes 474 and the cathodes 472 to define a plurality of channels 462 (e.g., helical channels) and simultaneously prevent arcing between anodes and cathodes. The process 40 further comprises subjecting 1090 the electrolyte solution 53 to a further residence time; prolonged within the electrolytic metal recovery cell, 42 continues. This can be achieved by providing one or more elongated channels 462 between the sleeves? of anode 474 and cathode 472, which extend in smooth, continuous and uninterrupted helical trajectories. It should be known that the residence time can also be increased by alternatively employing long tubular straight channels. Electrolytic solution 53 maintained within channels 462 is forced through channels 462 and walls thereof by small pressure differentials between inlet 110 and first outlet 120 and / or small pressure differentials between inlet 110 and the second outlet 130. As the electrolyte solution 53 moves through the channels 462, the cathodic mud concentrate is precipitated out of the electrolytic solution 53 until the solution becomes weaker in concentration and eventually substantially free of precious material 1092 The precipitating concentrate from the stream of sludge precipitate 53e is continuously collected 1094 into the second chamber 407, and the collected cathodic sludge concentrate 53f can be continuously or intermittently withdrawn 1098 or a combination thereof. A sterile solution stream 54 (which is substantially devoid of precious material) is continuously withdrawn 1096 from cell 42 via outlet 420, and can be fed to a continuous elution vessel 24 within a continuous elution process; twenty.

Figure 20 shows a regeneration process of carbon 30 according to some modalities. A fraction of solids 55 of the spent spent suspension, 51d comprising the spent dehydrated carbon, is siphoned with a screen 32 to remove the spent fine carbon materials 55b. Gauged carbon fine materials 55b I they are placed in a carbon fines retention tank 34. The remaining coarse spent carbon 55a is sent to a regeneration furnace 35 (or other means for regeneration such as a chemical, vapor or biological process). The hot reactivated carbon 55c is removed from the regeneration furnace 35 and turned off in a carbon 36 quench tank. A suspension of regenerated, cooled carbon and the fluid is moved to a dehydration sieve 37 via the pump 33. After passing to Through the dewatering sieve 37, the activated / reactivated dehydrated carbon 56 is moved to a continuous carbon adsorption / charging process 70. The lower fluid flow, which comprises the cold reactivated carbon suspension 55d, is moved to the tank of retaining carbon fines 34.

Figure 21 shows a continuous metal recovery system 100 'according to some embodiments of the invention, comprising a continuous acid washing system 10', a continuous elution system 20 ', a continuous electroextraction system 40' a system of regeneration of carbon 30 '. Figures 22 and 23 are used to compare the provisions of the scale plant and the general areas. Figure 22 shows the system 100 'for the continuous recovery of metals according to Figure 21, and Figure 23 comprises a conventional system 9000' for batch recovery of the metals using the process steps by "batches". As can be seen from Figures 22 and 23, the system 100 'according to the invention is smaller in size than the conventional system 9000' described in Figure 23. In addition to the smaller size, the system 100 'is also more efficient and environmentally friendly.

Figure 24 shows an alternative to the washing tanks 200, 200 ', 200"shown in Figures 6-8 In one embodiment shown, an acid washing tank 2000 is provided, which can replace the washing tank with acid 200. The acid wash tank 2000 comprises a washing chamber 2020 having a fluidized bed panel 2021 that spans the length of the wash chamber 2020 with pore sizes smaller than the average particle size of the charged / charged carbon , one or more adjustable assemblies 2007, 2009 which can be individually raised, lowered or pivoted on a frame or connection (not shown for clarity) to change the camera tilt angle 2020 with respect to the 2002 slider, an input of recirculation 2023a provided below the fluidized bed panel 2021 / and a recirculation outlet 2023b provided above the fluidized bed panel 2021. The recirculation outlet n 2023b outputs comprises one or more overflow 2027, each provided with at least one screen cleanable / replaceable 2008 wrap, which maintains up-loaded carbon / recharged 57 within chamber 2020 and filters the projection 57c dilute acid solution. The 2008 recycle screens may be provided proportionally between the bolt flange members of the overflow outlets 2027 and may comprise integral peripheral gaskets. Figures 25 and 26 show more detailed views of the camera 2020 shown in Figure 24.

The recirculation inlet 2023a may comprise one or more adjustable nozzles 2011 which serve to fluidize the loaded / recharged carbon 57. The nozzles 2011 may be individually or collectively angularly adjusted and "placed" at a fixed angle, in order to: compensate the various inclinations of the 2020 camera, prevent the accumulation of charged / recharged carbon 57, and counteract the backflow within the 2020 chamber, caused by the parasitic currents surrounding the internal deflectors 2018. The 2020 camera, can, as shown, be constructed in the shape of a clam shell, with a number of fasteners 2004 that connect the shell portions of almej ai superior and inferior to each other. One or more additional packages may be employed between the upper and lower clam shell portions to form a seal, or the fluidized bed panel 2021 itself may be provided with properties of the peripheral packing material to provide a seal between the shell portions. of upper and lower clam. A first filter 2001 is provided at an inlet 2022 of the acid wash tank 2000. The first filter 2001 comprises a housing 2003 that serves to collect the loaded / recharged carbon suspension tributary 57 ', a first screen 2026 which serves to separate the loaded / recharged carbon 57 of the carrier fluid 5 * 7f present in the suspension 57 ', a first filter outlet 2006 that serves to transfer the loaded charged / charged carbon 57 from inside the upper housing 2003 to the washing chamber 2020, a recirculation tank 2029 that collects the carrier fluid 57f separated from the liquid fraction of the tributary suspension 57 ', and one or more clamps 2005 that removably couple the housing 2003 to the recirculation tank 2029 with the first sieve 2026 that extends between them, whereby periodic cleaning and / or replacement of the first 2026 screen is allowed. The 2029 recirculation tank can be configured to redistribute r continuously the carrier fluid 57f to a holding tank (not shown) or may simply comprise a valve for batch removal of the collected carrier fluid 57f.

A second filter 2024, similar to the first filter 2001, is provided adjacent a first channel 12082 extending from the fluidized bed panel 2021 to a i external portion of the washing chamber 2020. The first channel 2082 is configured to provide the outlet of the rinsed charged carbon with acid 57a, resting on, around / above the fluidized bed panel 2021, after it has undergone a time of predetermined residence of acid wash within the chamber 2020. The charged carbon rinsed with acid 57a is filtered by a second screen 2036, and the fraction of filtered solids of the unfilled carb rinsed with acid 57a leaves a discharge outlet 2028. The charged carbon rinsed with acid exiting discharge outlet 2028 can be captured and contained by a holding tank 2060 and subsequently transported (via pump 2030) to a downstream process (eg, aqueous rinse cycle). Alternatively, the charged carbon rinsed with acid leaving the discharge outlet 2028 can directly enter a downstream process (eg, dump into another 200 'aqueous rinse tank without an intermediate holding tank 2060 and pump 2023). ). The holding tank 2060 advantageously serves as a baffle which maintains a level of process control and prevents too much carbon feeding to downstream processes.

In use, the replenished diluted acidic solution 57c '(obtained by filtering the charged carbon rinsed with acid 57a with the second screen 2036) enters the recirculation tank 2039 and is pumped into the chamber 2020 via a pump 2030. The acid solution refilled diluent 57c 'enters recirculation inlet 2023a and then passes upwardly through the fluidized bed panel 2021 via the 2011 nozzles. The replenished diluted acid solution 57c' suspends the incoming loaded / recharged carbon 57, and moves the carbon loaded / recharged 57 through the 2020 camera and around the deflectors 2011 for a predetermined residence time. The replenished diluted acid solution 57c 'passes through the 2008 recycle sieves and the filtered dilute acid solution 57c re-enters the recirculation tank 2039 via the recirculation outlet 2033b. The residence time of the loaded / recharged carbon 57 can be increased or decreased by the adjustment of the inclination angle of the chamber 2020 and / or the adjustment of the angular orientation of the nozzles 2011. For a metal extraction process, not variable , fixed, the angle of inclination of the 2020 camera and the angular positions of the nozzles can be pre-established by the manufacturer and permanently fixed in the optimal configuration to produce the most efficient residence time for said process.

EXAMPLE 1 A water-loaded 57-carbon suspension, comprising approximately 850 to 8505 grams / ton (30-300 ounces / ton) of pro and approximately 30% w / w, activated carbon from coconut shell is distributed to a system 10 'continuous acid wash. First, the inorganic components, specifically calcium carbonate and magnesium, are removed from the charged carbon by fluidization of a bed of charged active carbon with a dilute aqueous acid solution comprising about 1 to 5% by weight of hydrogen chloride ( HCl) and / or nitric acid (HNO3) in an acid wash tank 12, 200. The loaded active carbon is continuously transferred from the acid wash tank to an aqueous rinse tank 14, 200 'where the activated carbon is fluidized and cleaned with water. The charged carbon is subsequently continuously transferred from the aqueous rinse tank 14, 200 'to a caustic rinse tank 16, 200"The pH of the active carbon loaded or distributed to the caustic rinse tank is elevated above 10 by a solution caustic comprising about 1 to 3% by weight of sodium hydride.

The basic pickled loaded carbon 50 is fed continuously to a splash container 22 within a continuous elution system 20 'via a transfer medium of the caustic wash solution comprising approximately 1% by weight of caustic material (NaOH) and 0.1 % by weight of cyanide (NaCN). The splash container 22 is generally maintained at an operating temperature between about 38 and 93 ° C (100 and 200 degrees Fahrenheit (° F), and bears a pressure of about the atmospheric level.The charged carbon is transferred from the container of splash 22 to the continuous elution vessel 24, where the gold is removed from the carbon (ie, dissolution of the gold) The continuous elution vessel 24 operates at approximately 149 ° C (300 degrees Fahrenheit (° F), whose temperature It is reachable by raising the pressure of the wash solution to approximately 4.92 kg / cm2 (70 psi) (calibrator). The continuous elution vessel 24 continuously discharges into a vaporization vessel of lower pressure 25. A drop in the pressure between the continuous elution vessel 24 and the vaporization vessel 25 causes rapid flash vaporization of a portion of the effluent caustic wash solution. nerated is channeled to the splash container 22, whereby the splash container 22 is heated simultaneously and the vaporization vessel 25 is cooled. The spent carbon, (eg, comprising less than 3.3 grams / ton (1 oz / ton) (gold) is continuously moved out of the continuous elution system 20 'and into the regeneration process 30.

The caustic lavage solution pressurized to approximately 140 ° C (300 ° F) is filtered by one or more 324 sieves or filters to remove the sterile carbon particles and form the electrolytic solution 53, which is then passed through a cell metal extraction, electrolytic, continuous, (ie, electroextraction) 42. The electrolytic solution 53 is forced (via the increased pressure provided by the continuous elution vessel 24) through at least one channel 462 having a path helical fixed between a cylindrical sleeve anode 474 and a cylindrical sleeve cathode 472. A voltage between approximately 2 and 4 volts is passed between the anode 474 through the electrolytic solution 53 and the cathode 472, whereupon the concentrate is deposited cathodic mud 53f on the cathode surfaces 472. The speed of the electrolytic solution 53 creates a forced flow electrolytic current 53b within the channel 462 which continuously washes the collected cathodic sludge concentrate 53f which can be formed and collected on the cathode surfaces towards the conical bottom of the cell 42, where it can be removed at the operator's will or continuously by means of a valve control.

A contractor or other entity may provide a 100 'system or 100 process for the continuous recovery of metals in part or totally as shown and described. For example, the contractor may receive a bidding request for a project related to the design of a continuous metal recovery system 100 'or process 100, or the contractor may offer to design such a 100' system or a 100 process for a customer. The contractor can then provide, for example, one or more of the objectives, characteristics thereof shown and / or described in the modalities discussed above. The contractor can provide such devices by selling those devices or offering to sell those devices. The contractor may provide various modalities that are sized, shaped and / or otherwise configured to meet the design criteria of a particular customer or purchaser. The contractor may subcontract the manufacture, distribution, sale or installation of a component of the devices or other devices used to provide such devices. The contractor can also supervise a site or design or design one or more storage areas to stack the material used to manufacture the devices. The contractor may also maintain, modify or update the devices provided. The contractor may provide such maintenance or modifications by subcontracting such services, or by directly providing those services or components necessary for maintenance or modifications, and in some cases, the contractor may modify an existing metal recovery process 9000 or 9000 system. with a retrofit f'kit "to arrive at a modified process or system comprising one or more steps of the method, devices or features of the systems 100 'and the processes 100 discussed herein.

Although the invention has been described in terms of particular modalities and particular applications, a person of ordinary skill in the art, in light of this teaching, may generate additional modalities and modifications without departing from the spirit of or exceeding the scope of the invention. claimed invention. For example, particulate materials and carriers other than carbon (eg, polymers or ion exchange resins) can be used with the systems and processes described. In addition, reagents other than water, cyanide and caustic can be used to wash, strip or purify the particulates. In addition, the described systems and processes can be used to recover numerous types of materials that include; but they are not limited to copper, gold, silver, platinum, uraniq, lead, zinc, aluminum, copper, cobalt, manganese, rare and alkaline earth metals, etc. Accordingly, it should be understood that the Figures and descriptions herein are offered by way of example to facilitate understanding of the invention, and should not be considered as limiting the scope thereof.

Identifiers of the reference numbers 10 Continuous acid washing process 10 'Continuous acid washing system 12 Washing tank with acid 13 Pump 14 Aqueous rinse tank 16 Caustic rinse tank 20 Continuous elution process 20 'Continuous elution system 21 Return of steam 22 Splash bowl 23 Pump 24 Continuous elution vessel 25 Vaporization vessel 26 Dehydration sieve 27 Immersion heater 28th Influx Pipe 28b Output flow piping 29 Valve 30 Carbon regeneration process 30 'Carbon regeneration system 32 Sieve 33 Pump 34 Carbon fines retention tank 35 Regeneration oven 36 Carbon off tank 37 Dehydration sieve 40 Continuous electroextraction process 40 'Continuous electroextraction system 42 Metal electrolytic continuous extraction cell 50 Carbon loaded pickling (or suspension) caustic / basic 51 Suspension of washing solution and carbon loaded pickling 51a Heated and / or pressurized suspension 51b Solution flow path in solution coil 5lc Worn suspension 5Id Concentrated spent suspension 52 Liquid fraction of concentrated spent suspension 53 Electrolytic solution 53a Dispersed influx current 53b Forced flow electrolytic current, 53c Residence chamber exit flow 53d Worn electrolytic current 53c Mud precipitate stream 53f Cathodic mud concentrate 53g Sludge removal stream 54 Sterile solution (ie spent electrolyte) 55 Fraction of solids from the spent suspension concentrated (eg, dehydrated) 55th Coarse spent carbon 55b Spent carbon fines 55c Carbon reactivated hot 55d cold reactivated carbon suspension 56 Carbon activated / reactivated 57 'Charged / recharged carbon suspension 57 Carbon loaded / recharged 57a Charged carbon rinsed with acid 57c, 57c 'Dilute acid solution 57d, 57d 'Aqueous rinse solution 57e Caustic rinsing solution 57f Carrier fluid 60 Holding tank 70 Charge process / continuous carbon adsorption 70 'Charge system / carbon continuous adsorption 100 Process for the continuous recovery of metals 100 'System for the continuous recovery of metals 200 Washing tank with acid 200 'Aqueous rinse tank 200"Caustic rinse tank 220 First camera 221 First fluidized bed panel 222 First entry 223rd First recirculation inlet 223b First recirculation outlet 224 First landfill 226 First sieve 227 First overflow exit 228 First download output 229 First recirculation tank 230 Second camera 231 Second fluidized bed panel 232 Second entry 233rd Second recirculation inlet 233b Second recirculation outlet 234 Second landfill 236 Second screen 237 Second overflow exit 238 Second discharge output 239 Second recirculation tank 240 Third camera 241 Third fluidized bed panel 242 Third entry 243rd Third recirculation inlet 243b Third recirculation outlet 244 Third landfill 246 Third screen 247 Third overflow output 248 Third discharge output 249 Third recirculation tank 251 Acid overflow 253 Return of drained acid 254 Overflow of rinse water 256 Return of drained rinse water 257 Overflow of caustic rinse 260 Lower wall 266 Internal tubular wall 268 External tubular wall 282 First channel 284 Second channel 286 Third channel 57b Charged carbon rinsed 301 Entry stamp 302 Input assembly 304 Entry 306 First extreme 308 Second extreme 310 One or more side walls 312 Effluent dam assembly 314 Assembly member 316 Effluent damper 318 One or more deflectors 320 Fluidized bed panel 322 Admirement gateway of the tributary 324 Filter (eg, disk screen) 326 Influence damper 328 Exit 329 Exit stamp 330 Output assembly 340 Residence chamber 350 Fluidization chamber 402 Montaj e 404 Base 405 First camera 406 Cell body 407 Second camera 408 Third camera 410 Entry 412 One or more side entrance walls 413 One or more openings 414 Input mounting 417 One or more insulators 420 First outing 422 One or more first side walls of exit 1 424 First output assembly 430 Second exit 432 One or more second side exit walls 434 Second output assembly 440 First extreme 441 Bra 442 Anode terminal 442nd Bra 442b Clamp 442c Terminal Guide 442d Conducting washer 442c Insulating lining 442f Thread or equivalent assurance feature 442g Complementary thread or characteristic of assurance 4 2h Driver support 442i Reception portion 444 Anodic panel 445 Cathodic tab 446 Insulating panel 447 Anodic panel 450 Baffle 452 Anodic panel 454 Anode / Cathode Isolator 456 Anode / Cathode Isolator Holder 458 One or more reception portions 460 Residence Chamber 462 One or more channels 472 Cathode 473 One or more protuberances 474 Anode 476 One or more insulators 477 Internal anode 479 External anode 480 Second extreme 482 One or more side walls 1000 Process for the continuous recovery of metals 1002-1046 Steps of continuous acid washing 1048-1080 Continuous elution steps 1082-1100 Continuous electroextraction steps 2000 Washing tank with acid 2001 First filter 2002 Sliding 2003 Accommodation 2004 Bra 2005 Clamp 2006 First filter output 2007 First adjustable assembly 2008 Recycling sieve 2009 Second adjustable assembly 2011 Mouthpiece 2018 Deflector 2020 Camera 2021 Fluidized bed panel 2022 Entry 2023 Pump 2023a Recirculation inlet 2023b Recirculation outlet 2024 Second filter 2026 First sieve 2027 Overflow output 2028 Discharge output 2029 Recirculation tank 2033b Recirculation outlet 2036 Second screen 2039 Recirculation tank 2060 Holding tank 2082 First channel 9000 Conventional batch metal recovery process 9000 'Conventional batch metal recovery system 9100 Conventional batch acid washing process 9100 'Conventional batch acid washing system 9120 Acid washing container 9132 Pump 9134 Carbon transfer pump] 9136 Bomb '|' 9140 Diluted acid tank 9150 Sump pump 9160 Neutralization tank 9200 Conventional batch elution process (washing Zadra) 9200 'Conventional batch elution system (washing Zadra) 9220 Sterile solution tank 9232 Carbon transfer pump 9234 Sterile solution backup pump 9236 Sterile solution pump 9237 Sterile solution 9239 Hot sterile solution 9240 Washing container 9250 Heat exchanger or equivalent heat exchanger 9300 Carbon regeneration process 9400 Conventional batch electroextraction process 9400 'Conventional batch electroextraction system 9420 Electrolytic metal recovery cell, batch (for example, plate cathodes rewireable) 9421 Hot electrolytic solution 9430 Pump 9440 Electroextraction pump housing 9500 Carbon loaded pickling 9530 Electrolytic solution 9540 Sterile solution 9550 Spent carbon 9560 Carbon activated / reactivated 9570 Charged or recharged carbon 9700 Batch carbon loading process, conventional It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Claims

CLAIMS Having described the invention as above, the content of the following claims is claimed as property:

1. A system for the continuous recovery of metals, characterized in that it comprises at least one of the following: a continuous acid washing system, configured to receive an uninterrupted, continuous inflow of charged carbonaceous particles, and the distribution of an uninterrupted, continuous stream of carbonaceous, charged, pickled particles; a continuous elution system configured to receive an uninterrupted, continuous inflow of a wash solution, containing charged, pickled carbonaceous particles, and the distribution of an uninterrupted, continuous stream of electrolyte solution; Y a continuous electrowinning system configured to receive an uninterrupted, continuous inflow of electrolyte solution, distributing a continuous uninterrupted flow of a sterile solution, and continuously and uninterruptedly forming a cathodic mud concentrate; wherein each of the continuous acid wash system, the continuous elution system, and the continuous electrowinning system are configured to operate simultaneously without common interruptions with the conventional batch metal recovery processes.

2. The system according to claim 1, characterized in that it also comprises a carbon regeneration system operatively connected to the continuous elution system.

3. The system according to claim 1, characterized in that it furthermore comprises a carbon charging / activation system, operatively connected to the continuous acid washing system.

4. The system according to claim 1, characterized in that it also comprises a holding tank operatively connected to the continuous acid washing system, and to the continuous elution system.

5. The compliance system! with claim 1, characterized in that it comprises all three of the continuous acid wash system, the continuous elution system and the continuous electroextraction system;

6. The compliance system i with claim 1, characterized in that it also further comprises one or more pumps.

7. The compliance system, with claim 1, characterized in that in addition the continuous elution system is operatively connected to the continuous electrowinning system.

8. The system according to claim 7, characterized in that the continuous elution system further comprises one or more screens or filters configured to prevent the carbonaceous particles from passing into the continuous electrowinning system.

9. The system according to claim 1, characterized in that the continuous acid wash system further comprises a chamber adapted to retain a fluidization means; an inlet adapted to receive a feed containing charged carbonaceous particles; a fluidized bed distribution panel or other means adapted to fluidize the particular carbonaceous in the presence of the fluidization medium; an outlet adapted to pass the charged carbonaceous particles and fluidization medium from the chamber; and a screen adapted to filter charged carbonaceous particles from a fluidization medium; \ wherein the continuous elution system comprises a splash container, a continuous elution vessel, and a vaporization vessel, wherein the splash vessel is operatively connected to the continuous elution vessel in series, the continuous elution vessel is operatively connected to the vaporization vessel in series, and the splash container is operatively connected to the vaporization vessel in parallel; Y wherein the continuous electrowinning system comprises a continuous electrolytic metal recovery cell having a cell body configured to maintain the electrolytic solution at a high pressure and / or temperature; at least one anode, at least one cathode, an inlet configured to receive an uninterrupted, continuous tributary stream of the electrolytic solution; a first outlet configured to discharge an uninterrupted effluent stream, continues the sterile solution; a second outlet configured to remove the cathodic mud concentrate; and a residence chamber configured to continuously transfer the electrolyte solution from the entrance to the first exit, and to increase! the residence time of the electrolytic solution between at least one anode and at least one cathode, the residence chamber comprises one or more channels that are configured to provide a forced flow of the electrolytic solution therein;; which is strong enough to continuously detach, and / or transport the cathodic mud concentrate to! along one or more channels and eventually out of the residence chamber.

10. The system according to claim 1, characterized in that the continuous acid wash system further comprises one of a diluted acid solution, an aqueous rinse solution and an acoustic rinse solution; wherein the continuous elution system further comprises a solution containing at least one of a carbonaceous particulate material charged with a precious metal, an electrolytic solution, the spent carbonaceous particles, a caustic, an aqueous component and cyanide; and wherein the continuous electrowinning system further comprises an electrolytic solution

11. The system according to claim 1, characterized in that the continuous acid washing system, the continuous elution system and the continuous electrowinning system are each configured to increase a pressure and / or temperature of a solution or suspension contained therein.

12. The system according to claim 1, further characterized in that a carbon regeneration system is operatively connected to the continuous elution system, a continuous carbon activation / charging system is operatively connected to the continuous acid wash system, and the Carbon regeneration system is operatively connected to the carbon loading / activation system.

The system according to claim 1, characterized in that the continuous acid washing system is operatively connected to the continuous elution system.

14. A process for the continuous recovery of a metal, characterized in that it comprises: continually feed a continuous washing system with particles loaded with a metal; continuously washing the charged particles inside the continuous washing system, to pick up the charged particles; continuously removing the charged, pickled particles from the continuous washing system; continuously loading a continuous elution system with the charged, pickled particles; continuously withdrawing the electrolytic solution from the continuous elution system, continuously feeding a continuous electrowinning system with the electrolytic solution; continuously withdrawing a sterile solution from the continuous electrowinning system; Y continuously distribute the spent electrolyte solution to the continuous elution system. wherein each of the continuous washing system, the continuous elution system, and the continuous electrowinning system are operably operated and configured to allow the above steps to be performed simultaneously.

15. The process according to claim 14, characterized in that it also comprises the formation of charged particles by continuously adsorbing metal on the particles in a continuous loading / adsorption system, identical to the continuous washing system.

16. The process according to claim 15, characterized in that the particulate material is one of a carbonaceous particulate, a polymeric adsorbent or an ion exchange resin.

17. The process according to claim 14, characterized in that it also comprises continuously withdrawing the cathocic mud concentrate from the continuous electrowinning system. ,