ELECTROCHEMICAL REACTOR FOR PROCESSES FOR NON-FERROUS METAL ELECTRODEPOSITION, WHICH COMPRISES A SET OF APPARATUSES FOR GENTLY AGITATING AN ELECTROLYTE, A SET OF APPARATUSES FOR CONTAINING AND COALESCING AN ACID MIST, AND A SET OF APPARATUSES FOR CAPTURING AND DILUTING ACID MIST AEROSOLS REMAINING IN THE GAS EFFLUENT OF THE REACTOR

Abstract

The invention relates to an electrochemical reactor for continuous copper electrodeposition at high current densities with copper sulfate electrolytes, which comprises devices and systems of functional means that are linked and operated in line, thereby forming a triad, for standardising operational conditions in a series of operative parallel reactors. The triad, installed in each existing or new electrolytic container, comprises: a gentle electrolyte agitation system (AGSEL) with means for pulsing control of the aeration volume diffused by bubbling directed into each inter-cathodic space; a duo of systems linked in line, which comprises a system of removable anode covers (CAR) for containing, confining and coalescing the acid mist; and an acid mist recycling system (SIRENA) that captures non-coalesced electrolyte aerosols and condenses the steam, returning same to the process, while the pollutants of the gaseous fluid from the reactor are substantially diluted.

Claims

1. Electrochemical reactor (1) for the conduction of electrodeposition processes of non-ferrous metals that operates with a container (2) of tried-and-tested monolithic polymer concrete, where a flow of a suitable electrolyte solution of given characteristics fed by a tuning fork to the surfaces of the cathode plates (11) energized in the interelectrode spaces of the electrochemical reactor (1) provide sufficient ion mass transfer for the proper integrity and uniform compaction of the metal deposits when operating stablyat the corresponding intensities currentthe process of electrowinning metals to their so-called limit current density; at higher current densities, the balances between the process variables become unstable and lose the balances with which acceptable deposit results are achieved, and objectionable physical quality defects and impairments begin to be generalized in the metallic sheets, as well as degradation in their chemical composition due to the presence of impurities in the electrolyte that are electrodeposited together with the metal; on the other hand, in the process operationat any current intensitythe solution decomposes, generating micro O.sub.2 bubbles (7) on the anode surfaces; the bubbles grow ascending through the electrolyte incorporating its gases, and when emerging into the atmosphere (3) they explode, configuring the problematic acid mist, gaseous fluid composed of gases in the electrolyte, water vapor, sulfuric acid and sulfurous electrolyte aerosols, highly harmful to health, CHARACTERIZED because it comprises a triad of concatenated sets of devices for continuous online operation in the electrochemical reactor (1), which allows the process to be operated at high current densities with simultaneous control and mitigation of the acid mist effluent; this triad is made up of: a) AGSEL (100) set of bubble flow controlled flow rate air diffusers, with or without pulses, to improve ion mass transfer as appropriate for current density operated in the electrochemical reactor (1), which is capable of accommodating current intensities up to 600 A/m.sup.2; The AGSEL (100) is made up of a self-supporting monolithic structural frame (101) that contains rectangular modules that carry air diffusers (102) to diffuse air in the form of bubbles (117), which are fixed with bolts (113) designed for quick replacement of the rectangular air diffuser carrying modules (102); b) Set of CAR (200) devices for containment, confinement, coalescence and recycling of electrolyte aerosols entrained in the acid mist generated by the process; the CAR assembly is made up of a series of individual removable anodic covers (201) on each anode of the electrochemical reactor (1); each cover consists of a structural body (206), monolithic molded of polymeric compound, with dielectric properties, high structural and corrosion resistance to be installed superimposed on each anodic plate hanging bar (10) under pressure; and two fixed covers (202) and (203) at the ends of the container (2); the individual removable anode covers (201) are held in each anode plate (10) by flexible holding tabs (212) inside the structural body of monolithic polymeric compound (206); on its upper part, it also has two vertical guide horns (204) joined by a horizontal settlement plate (205), which also serves to eventually install wireless differential pressure sensors under the individual removable anode covers (201) with regarding the atmosphere; the structural body on its lateral sides also accommodates at least two multiple parallel flexible longitudinal seals (207) superimposed on both sides and; c) SIRENA Apparatus Set (300) which is attached to an outer front wall (4) of each container (2) of the electrochemical reactor (1) to suck the flow of the effluent gaseous fluid and extract it from the container (2) to discharge it in the DEVA device (302)acid vapor depuratorwhose functions are to separate and recover as acid condensate: water vapor, sulfuric acid and electrolyte aerosols entered as acid mist from the electrochemical reactor (1); the depuration is of controlled intensity and allows increasing the safety of the effluent gaseous fluid, and directing the effluent gas flow from DEVA (302) to the global discharge to the external atmosphere (311), or to secondary depuration in at least one device DECOMUVA multi-stage acid vapor condenser depurator (312), if the requirement of safety in atmospheric discharge requires it.

2. Electrochemical reactor (1) according to claim 1, CHARACTERIZED in that the thermo-perforated flexible diffuser tubes (107) air diffusers in their rectangular bearing modules (102), are arranged parallel to the electrodes under the interelectrode spaces, and the number of Rectangular bearing modules for air diffusers (102) depend on the length of the electrochemical reactor (1), size, number of flexible thermo-perforated diffuser tubes (107) to diffuse the agitation air and the overall flow rate of aeration required in the interelectrode spaces to the inside the container (2) according to the range of current intensity operated in the electrochemical reactor (1).

3. Electrochemical reactor (1) according to claim 1, CHARACTERIZED because it also comprises a flow of atmospheric diffusion air that feeds the self-supporting monolithic structural frame (101), first passing through a rotameter and pressure switch (110), and then, optionally, by an anti-siphon device (111) in line with an anti-return device (112), prior to entering through the air entry point (103) into the self-supporting monolithic structural frame (101); by means of a PVC tube of at least 10 inches in diameter, externally reinforced by a continuous filament blanket (fiberglass and resin) encapsulated in the monolithic structural polymer mortar of the self-supporting monolithic structural frame (101), the diffusion air flow It moves through the self-supporting monolithic structural frame (101), which internally has T joints at the T connection points (104), to supply air to each rectangular module that supports air diffusers (102), through the connection point of power (105).

4. Electrochemical reactor (1) according to claim 3, CHARACTERIZED in that the rectangular modules that support the air diffusers (102), comprise a manifold (108), which is attached to the self-supporting monolithic structural frame (101) through the point The power connection (105) and the blind counter manifold (109) are bolted to the self-supporting monolithic structural frame (101) and accommodates the blind connectors (114) to insert the thermo-perforated flexible diffuser tubes (107).

5. Electrochemical reactor (1) according to claim 4, CHARACTERIZED in that the manifold (108) has feeder connectors (106) to insert the thermo-perforated flexible diffuser tubes (107).

6. Electrochemical reactor (1) according to claim 5, CHARACTERIZED in that the thermo-perforated flexible diffuser tubes (107) with perforations arranged in their length from which emerges the controlled diffuser air flow to each thermo-perforated flexible diffuser tube (107) so that vertically ascending rows of individual air bubbles (117) are formed in the electrolyte (5), and in diffusion patterns determined by design.

7. Electrochemical reactor (1) according to claim 1, CHARACTERIZED because the characteristic of the air bubble (117), depends on the air flow and pressure, drilling diameter and number of holes per linear meter of flexible diffuser tubes thermo-drilled (107) to deliver the flow rate required for each flexible thermo-drilled diffuser tube (107) in determined bubble diffusion patterns to enhance the desired bubbling uniformity in each interelectrode gap.

8. Electrochemical reactor (1) according to claim 1, CHARACTERIZED because in the self-supporting monolithic structural framework (101) it is provided with height adjustable support supports (116) from the bottom of the container (2), to maintain the horizontality of the self-supporting monolithic structural frame (101) with respect to the anode plates (10) and cathodic plates (11) suspended vertically from the upper edges of the side walls of the container (2) of the electrochemical reactor (1).

9. Electrochemical reactor (1) according to claim 1, CHARACTERIZED in that the front ends of the structural body of monolithic polymeric compound (206), in which the multiple parallel flexible longitudinal seals (207) are housed, superimposed and at least double front seals (208) that cover the electrolyte (5) in the lateral channels (211) resting on the adjacent side walls of the container (2) of the electrochemical reactor (1).

10. Electrochemical reactor (1) according to claim 9, CHARACTERIZED in that the multiple superimposed parallel flexible longitudinal seals (207) form at least two superimposed ventilated perimeter mini-chambers (209), to initiate, enhance and promote the coalescence of the electrolyte aerosols in the acid mist confined inside the superimposed perimeter mini ventilated chambers (209) with the continuous entry of controlled atmospheric air flow rates (210) at a lower temperature than the ambient temperature inside the superimposed perimeter mini ventilated chambers (209).

11. Electrochemical reactor (1) according to claim 10, CHARACTERIZED in that it comprises multiple superimposed parallel flexible longitudinal seals (207) that rest against the vertical flat surface of the cathode plate (11), in the mist confinement volume acid that ends in the lines of support of the multiple superimposed parallel flexible longitudinal seal (207) with the cathodic plate (11).

12. Electrochemical reactor (1) according to claim 1, CHARACTERIZED because CAR (200) and SIRENA (300) are designed to operate concatenated in order to recover the water vapor, sulfuric acid and the electrolyte aerosols remaining in the flow rate of the effluent gaseous fluid extracted cell by cell (303) out of the electrochemical reactor (1).

13. Electrochemical reactor (1) according to claim 12, CHARACTERIZED in that the acidic vapors and aerosols extracted from the electrochemical reactor (1) in the effluent gaseous fluid, in the first instance, are captured in the DEVA acidic vapor depurator apparatus (302) by a bubbler (305) under a height adjustable liquid column (306) installed on an outer front wall (4) of each container (2).

14. Electrochemical reactor (1) according to claim 13, CHARACTERIZED in that, optionally, it can also comprise an apparatus for checking the contents of contaminating acidic vapors AVDEVA (315) remaining in the gaseous fluid effluent from the DEVA acidic vapor depuration apparatus (302) prior to its global discharge into the atmosphere (311) environment.

15. Electrochemical reactor (1) according to claim 14, CHARACTERIZED in that the suction to generate the extraction flow of the extracted fluid gas flow cell by cell (303), is provided in a preferred embodiment with amplifying apparatus of air (500) without moving parts powered by a compressed atmospheric air network (801) externally supplied by a continuous flow compressor (800) (screw or other), or alternatively, in each electrochemical reactor (1) by means of a mini turbine (309) with a very low flow rate, powered by an electric motor, preferably with a frequency variator (310).

16. Electrochemical reactor (1) according to claim 12, CHARACTERIZED because it also has an input that communicates to a differential flow pressure sensor apparatus on a calibrated orifice plate (601), an orifice plate sensor output (602), a calibrated orifice plate (603), a rotameter (700), whose compressed atmospheric air (801) is provided by a screw compressor (800).

17. AGSEL Soft Electrolyte Agitation System (100), which when working generates individual rows of controlled air bubbles (117), where the flow of a suitable solution of electrolyte of given characteristics fed by a tuning fork to the surfaces of the cathode plates (11) energized in the interelectrode spaces of the electrochemical reactor (1) provide sufficient ion mass transfer for the proper integrity and uniform compaction of the metal deposits by operating stablyat the corresponding current intensitiesthe process of electrodeposition of metals only up to their so-called limit current density; at higher current densities, the balances between the process variables become unstable and begin to lose the balances with which acceptable deposit results are achieved, and objectionable physical quality defects and impairments begin to occur in the metal sheets, as well as degradation in its chemical composition due to the presence of impurities in the electrolyte that are electrodeposited together with the metal; CHARACTERIZED because a horizontal self-supporting monolithic structural frame (101) is located in each electrochemical reactor (1) near the bottom of the container (2), designed to homogeneously diffuse outside air, in a controlled way that suitably directs the rows of emerging bubbles in the interelectrode spaces, in the form of small individual air bubbles (117), with which it is possible to considerably increase the transfer of ionic mass from the boundary layer of the cathode plates (11), which allows to effectively accompany current intensities up to 600 A/m.sup.2.

18. AGSEL soft electrolyte agitation system (100) according to claim 17, CHARACTERIZED in that the thermo-perforated flexible diffuser tubes (107) air diffusers in their rectangular bearing modules (102), are arranged parallel to the electrodes under the interelectrode spaces, and the number of modules (102) depends on the length of the electrochemical reactor (1), size, number of flexible thermo-perforated diffuser tubes (107) to diffuse the agitation air and the overall flow rate of aeration required in the spaces interelectrodes inside the container (2) according to the range of current intensity operated in the electrochemical reactor (1).

19. AGSEL soft electrolyte agitation system (100) according to claim 18, CHARACTERIZED in that the thermo-perforated flexible diffuser tubes (107) have perforations arranged in rows along which air bubbles emerge (117) individual forming rows with discharge directed towards the electrolyte (5) in the interelectrode spaces.

20. AGSEL soft electrolyte agitation system (100) according to claim 19, CHARACTERIZED because the characteristics, sizes, intervals of individual air bubbles (117) desired between each other when emerging into the electrolyte (5), depend on the flow rate of continuous air and of the pulses of the flow, of the diameter of the perforations, of their perforation pattern and the quantity of flexible thermo-perforated diffuser tubes (107) necessary to diffuse air in each interelectrode space per rectangular module carrying air diffusers (102).

21. System of removable anode covers CAR (200), to contain, confine, coalesce and recycle acid mist, highly harmful to health, in each unit cell of the electrochemical reactor (1), because the volumes of oxygen (02) generated in the current industrial electrowinning processes of copper and other non-ferrous metals are directly proportional to the current intensities applied to the anodes, and therefore, to the environmental contamination associated with the operation of the electrowinning cells of the current art, CHARACTERIZED because the removable anode covers (201) are individual, of remove and put for each anode plate (10), they are easily removable from their seat on their anode hanger bar, and can be firmly installed by the simple pressure resulting from inserting on the horizontal part of the structural body of monolithic polymeric compound (206) of the individual removable anodic cover (201) on the hangers It is horizontal of the anode plates (10), since they have ad hoc clamping means with flexible clamping tabs (212) to be firmly locked in the working position by mere insertion pressure, and therefore, at the same time they are easily removable by a trained operator; The CAR System (200) also includes fixed covers (202) and (203) at the ends of the container (2) of the electrochemical reactor (1) and are installed over the free spaces of anodic plates (10) and cathode plates (11) at each end of the container (2).

22. System of removable anode covers CAR (200) according to claim 21, CHARACTERIZED because it also includes the means for the entrance of controlled flows of atmospheric air (210) in each interelectrode space through the support line against the cathode plate (11) adjacent to the multiple overlapping parallel longitudinal flexible seals (207) installed in each individual removable anode cover (201) to admit a controlled entry in a range of minimum external air flow rates necessary to produce a slight vacuum under the covers individual removable anodes (201) and thus ensure the impossibility of escape of acid mist in the opposite direction to the flow of air entering from the atmosphere (3), over the electrochemical reactor (1), maintaining the minimum necessary depression continuously over time the CAR System (200).

23. System of removable anode covers CAR (200) according to claim 21, CHARACTERIZED because it also comprises at least two superimposed ventilated perimeter mini-chambers (209), to contain, confine and coalesce the liquid aerosols of the acid mist with the suction of an external air flow, whose temperature lower than that of the superimposed perimeter mini-ventilated chamber (209) initiates and promotes coalescence, increasing the size of the micro drops in suspension to larger and heavier drops that they adhere, first to the available surfaces, and then with the subsequent increase in volume and weight, they detach from the same surfaces when their individual weight exceeds their adhesion with the surfaces to which they were adhered, precipitating by gravity to the electrolyte (5) of the reactor electrochemical (1), which generates them in real time.

24. CAR removable anodic roof system (200) according to claim 22, CHARACTERIZED in that the multiple superimposed parallel flexible longitudinal seals (207) and the path of egress of the coldest external atmospheric air of the superimposed perimeter mini ventilated chambers (209) provide protection from corrosive anions to the stainless steel material of the cathode plates (11), since the lower seal of the lower superimposed perimeter mini-chamber (209) closest to the electrolyte level is just above the electrolyte level (5), whereby the emission of external atmospheric air by the seal of the superimposed perimeter mini-ventilated chamber (209) constantly sweeps the cathodic surfaces, protecting them from the onset of corrosion.

25. Removable anodic cover system CAR (200) according to claim 23, CHARACTERIZED because the confinement of the liquid aerosols of the acid mist (6) is inside the superimposed perimeter mini-ventilated chambers (209) formed by the minus two multiple perimeter overlapping parallel flexible longitudinal seals (207) abutting against the vertical flat surfaces of the adjacent cathode plates (11); the multiple overlapping parallel flexible longitudinal seals (207) are preferably housed in longitudinal grooves in the monolithic polymer composite structural body (206) of the individual removable anode covers (201) in each anode plate (10), and further have two horns vertical guides (204) to facilitate smooth re-entry of the empty cathode plates (11) after harvests to their working position in the inter-anode spaces; on the upper horizontal face of the monolithic polymer composite structural body (206); On its upper part, it also has two vertical guide horns (204) joined by a horizontal settlement plate (205), which also serves to eventually install wireless differential pressure sensors under the individual removable anode covers (201), to ensure the control of depression under the CAR System (200) with respect to the atmosphere; which ultimately ensures the impossibility of the acid mist escaping into the atmosphere (3) over the electrochemical reactor (1).

26. System of removable anode covers CAR (200) according to claim 21, CHARACTERIZED because it also comprises a container (2), based on a dielectric polymeric compound, with high structural resistance, and chemical resistance to corrosion, and strategically designed to locate the housings of the multiple overlapping parallel flexible longitudinal seals (207) on both sides, and at least double front seals (208) covering the electrolyte (5) in the side channels (211) adjacent to the side walls of the container (2) of the electrochemical reactor (1).

27. CAR removable anodic cover system (200) according to claim 21, CHARACTERIZED in that the multiple superimposed parallel flexible longitudinal seals (207) that form at least two superimposed perimeter mini ventilated chambers (209), to promote the coalescence of the acid mist confined within it;

28. Effluent gaseous fluid depurator system extracted cell by cell (303) from the electrochemical reactor (1) SIRENA (300), to reduce the remaining water vapor, sulfuric acid and electrolyte aerosols remaining, highly harmful to the health, that may have been entrained in the effluent gas flow from the container (2) of the electrochemical reactor (1), because the volumes of oxygen (02) generated in the current processes of industrial electrowinning of copper and other non-ferrous metals are directly proportional to the current intensities applied to the anodes, and consequently, to the environmental contamination associated with the operation of the electroobtaining cells of the current art, CHARACTERIZED because it comprises a collection manifold (301) of at least one discharge of the fluid effluent gas extracted cell by cell (303) from the container (2) of the electrochemical reactor (1) and discharging it through the lower part of the access to the bubbler (305) installed on the interior floor of the DEVA acid vapor depurator (302) attached to an exterior front wall (4) of the container (2) in the electrochemical reactor (1); Two effluent gaseous fluids are discharged from the DEVA acid vapor depurator apparatus (302): (a) liquid fluid condensed with water vapor and acid that is led to a central accumulator of acidic condensates ACECOA (313); and (b) substantially harmless effluent gaseous fluid (304) treated by the DEVA acid vapor depurator apparatus (302) that is discharged directly into the atmosphere (311), or to secondary depurators in at least one multi-stage condenser depurator apparatus. DECOMUVA (312) acidic vapors, if the requirement of safety in atmospheric discharge requires it.

29. SIRENA (300) water vapor, acid and electrolyte aerosol recycling system, according to claim 28, CHARACTERIZED because in its first instance the gaseous fluid enters through a bubbler (305) under a liquid column (306) height adjustable in the DEVA acid vapor depurator (302) installed on the outer front wall (4) of each container (2) of the electrochemical reactor (1).

30. Recycling system for water vapor, acid and electrolyte aerosols SIRENA (300), according to claim 28, CHARACTERIZED in that the suction to generate flow rates of the gaseous fluid effluent extracted cell by cell (303), At sustained levels of the Null Escape condition, it is preferably provided by means of an air amplifier (500) without moving parts, or else a mini turbine (309) with its frequency variator (310) in each electrochemical reactor (1).

31. Recycling system for water vapor, acid and electrolyte aerosols SIRENA (300), according to claim 28, CHARACTERIZED because also the process control of the effluent gas depurator system cell by cell extracted (303) from the electrochemical reactor (1) to the SIRENA System (300) is not limited only to manual control.

32. Electrochemical method for the conduction of electrodeposition of non-ferrous metals that operates with a container (2) of tried-and-tested monolithic polymer concrete, where a flow of a suitable electrolyte solution of given characteristics is fed by a tuning fork to the surfaces of the cathode plates (11) energized in the interelectrode spaces of the electrochemical reactor (1) provide sufficient ion mass transfer for the proper integrity and uniform compaction of the metal deposits by operating stablyat the corresponding current intensitiesthe process electrowinning of metals up to its so-called limit current density; at higher current densities, the balances between the process variables become unstable and lose the balances with which acceptable deposit results are achieved, and objectionable physical quality defects and impairments begin to be generalized in the metallic sheets, as well as degradation in their chemical composition due to the presence of impurities in the electrolyte that are electrodeposited together with the metal; on the other hand, in the process operationat any current intensitythe solution decomposes, generating micro O.sub.2 bubbles (7) on the anode surfaces; the bubbles grow ascending through the electrolyte incorporating its gases, and when emerging into the atmosphere (3) they explode, configuring the problematic acid mist, gaseous fluid composed of gases in the electrolyte, water vapor, sulfuric acid and sulfurous electrolyte aerosols, highly harmful to health, CHARACTERIZED because it comprises: a) Locating a horizontal self-supporting monolithic structural frame (101), of the AGSEL Set (100) in each electrochemical reactor (1) near the bottom of the container (2), which has been designed to homogeneously diffuse outside air, in the form of small individual air bubbles (117), in a controlled manner, directing the rows of emerging bubbles in the interelectrode spaces, enhancing the transfer of ionic mass from the electrolyte (5) to the cathode plates (11) to operate at high current intensities above 400 A/m.sup.2, and predictably, up to 600 A/m.sup.2; once the air bubbles emerge from the electrolyte surface, they explode and join the acid mist that occupies the volume under the removable anode covers (201) of the CAR Apparatus Set (200) and the acid mist rises entering the mini chambers of the removable anodic roofs (201), where it is knocked down by coalescence, which is promoted by the entry of controlled atmospheric air flow rates (210) substantially at a lower temperature than that of the environment inside the superimposed perimeter mini-chambers (209) in each of the unit cells and, b) Air enters the acid mist confinement volume in each unit cell of the container (2); and then, this same air, already in the confining volume on the electrolyte in each unit cell, drags the confined acid mist transversely towards the lateral channels (211) of the container (2); and then, when leaving the lateral channels (211), the gaseous flow of each unit cell moves through the lateral channels (211) towards the front suction wall of the container (2); c) The effluent gas flow from the electrochemical reactor (1) enters through the collection manifold (301) into the SIRENA assembly (300) in each container (2) of the electrochemical reactor (1), the entrance of atmospheric air at the height of the volume confinement of the acid mist in each unit cell is a short distance from the surface of the electrolyte (5), which prevents the permanence of corrosive emerging gaseous anions of the electrolyte in the strip of the protruding surface of the cathode plate (11) on the electrolyte (5) over the entire width of the cathode plate (11) in the unit cell, reducing the possibility of eventual corrosion of the cathode plates (11) precisely in the critical area on the electrolyte of the electrochemical reactor (1).

33. Electrochemical method according to claim 32, CHARACTERIZED in that the thermo-perforated flexible diffuser tubes (107) air diffusers in their rectangular bearing modules (102), are arranged parallel to the electrodes under the interelectrode spaces, and the number of Rectangular bearing modules for air diffusers (102) depend on the length of the electrochemical reactor (1), size, number of flexible thermo-perforated diffuser tubes (107) to diffuse the agitation air and the overall flow rate of aeration required in the interelectrode spaces to the inside the container (2) according to the range of current intensity operated in the electrochemical reactor (1).

34. Electrochemical method according to claim 32, CHARACTERIZED in that a flow of atmospheric diffusion air that feeds the self-supporting monolithic structural frame (101), first passes through a rotameter and pressure switch (110), and then optionally, through a device anti siphon (111) located in line with an anti return device (112), prior to entering through the air entry point (103) into the self-supporting monolithic structural frame (101), by means of a PVC tube of at least 10 inches diameter, externally reinforced by a continuous filament blanket (fiberglass and resin) encapsulated in the monolithic structural polymer mortar of the self-supporting monolithic structural frame (101), where the diffusion air flow is displaced by the self-supporting monolithic structural frame (101), which internally has T-junctions at the T-junction points (104), to supply air to each rectangular module carrying air diffusers (102), to through the power connection point (105).

35. Electrochemical method according to claim 32, CHARACTERIZED in that the coalescence is initiated in the superimposed perimeter mini-ventilated chambers (209) by the entry of controlled atmospheric air flow rates (210) that is at a lower temperature than the mini-ventilated chambers. superimposed perimeters (209), which initiates and enhances the growth of size and weight of the aerosols until they reach such a size that, by their own weight, they fall back into the electrolyte (5) that originated them, being continuously recycled at the same time as generated with the operation of the electrochemical reactor (1).

36. Electrochemical method according to claim 32, CHARACTERIZED because also the emerging flow on the liquid column (306) of the bubbler (305), always inside the DEVA acid vapor depurator (302), by means of a heat exchanger (307) and a refrigerant fluid cooled externally to the electrochemical reactor (1), from 1 to 5 C., either with a Vortex tube (501), or preferably with a Chiller cooler (308) for some liquid refrigerant (water, glycol or other), the aerosols and vapors of the gaseous fluid effluent from the bubbler (305) in the DEVA (302) are recovered substantially by condensation.

37. Electrochemical method according to claim 32, CHARACTERIZED because it also includes supplying external atmospheric air to the self-supporting monolithic structural framework (101), which enters through a rotameter and pressure switch (110) and optionally through a pipe that leads it through an anti-siphon device (111) in line with an anti-return device (112) of gaseous fluid, prior to its feeding at the air entry point (103) to the self-supporting monolithic structural frame (101); using a PVC tube of at least 10 inches in diameter externally reinforced by a bidirectional continuous filament blanket encapsulated in structural polymer mortar; the air flow travels through the self-supporting monolithic structural frame (101), which internally has T joints at the T connection points (104), to feed each rectangular module carrying air diffusers (102), through from the power connection point (105).

38. Electrochemical method according to claim 32, CHARACTERIZED because in addition the multiple superimposed parallel flexible longitudinal seals (207) closest on the electrolyte, with the sweep flow of the effluent ventilation air from the superimposed perimeter mini-ventilated chambers (209) prevents the sustained and necessary contact of the corrosive anions with the cathode plate (11) in the unit cells in the strip of cathode plates (11) that remains on the surface of the electrolyte (5) of the multiple superimposed parallel flexible longitudinal seal (207) bottom of the superimposed perimeter mini ventilated chamber (209) next to the electrolyte.

39. Electrochemical method according to claim 35, CHARACTERIZED in that the coalescence is promoted with the entry of controlled atmospheric air flow rates (210) sufficient to drag the confined acid mist under the multiple superimposed parallel flexible longitudinal seals (207) and then through the lateral channels (211) of the container (2) of the electrochemical reactor (1) to the point of extraction of the container (2) for depuration outside the container (2) of the vapors and aerosols in the DEVA acid vapor depurator (302).

40. Electrochemical method according to claim 39, CHARACTERIZED because the coalescence of mini droplets with continued growth in aerosol size that is initiated in the superimposed perimeter mini-ventilated chambers (209) by the entry of controlled atmospheric air flow rates (210) colder than the ambient temperature of the superimposed perimeter mini-ventilated chambers (209), the thermal differential enhances the growth in size of the aerosols until reaching such a size that, due to their own weight, they fall back to the electrolyte (5) where they originated, being continuously recycled at the same time that they are generated with the operation of the electrochemical reactor (1).

41. Electrochemical method according to claim 36, CHARACTERIZED in that the emergent flow on the liquid column (306) of the gaseous effluent bubbling fluid (305), always inside the DEVA acid vapor depurator (302), by means of an exchanger of heat (307), whereby the aerosols and vapors of the gaseous fluid effluent from the bubbler (305) are recovered substantially by condensation.

42. Electrochemical method according to claim 41, CHARACTERIZED in that the cooling of the effluent gaseous fluid extracted cell by cell (303) from the DEVA acid vapor depurator (302) to condense water vapor, recover sulfuric acid, and electrolyte sprays and incorporate them into the condensate of the DEVA acid vapor depurator (302) by feeding hyper cold air provided by a Vortex Tube device (501), or preferably with a Chiller cooler (308) for any liquid refrigerant (water, glycol or other), in two alternatives: (a) directly to the interior volume of the liquid column of the DEVA acid vapor depurator (302) that bubbles the gaseous fluid; (b) feeding the heat exchanger (307) and circulating the cooled hyper air to produce condensation of the flow of the gaseous effluent fluid extracted cell by cell (303); in both cases the flow of the hot effluent air (502) from the Vortex Tube (501) and the Air Amplifier (500) (if included), is used to dilute the level of contaminants remaining from the discharge of the harmless effluent gas fluid (304) of the DEVA acid vapor depurator (302) and air amplifier (500).

Description

BRIEF DESCRIPTION OF THE DRAWINGS OF THE INVENTION

[0078] The accompanying drawings are included to provide a better understanding of the principles of functional concatenation to achieve the seven simultaneous in-line operations on the container operated at high current densities in this invention, illustrated, in a preferred embodiment for continuous operation. of the electrochemical reactor, with manual controls by trained operators; which is not restrictive, since it constitutes the simplest way, of several possible alternatives, for the continuous operation of the electrochemical reactor with more sophisticated semi-automatic and automatic control controls in versions that have already been validated; and that, moreover, they are not limiting for the development of electrochemical reactor improvements for which industrial protection is requested.

[0079] FIG. 1 shows a perspective view of the electrochemical reactor (1) for electrodeposition of copper and other non-ferrous metals that houses the triad AGSEL (100), CAR (200), and SIRENA (300) of the present invention for continuous operation sustained in time above the current limits of the electrodeposition process.

[0080] FIG. 2 shows a perspective view with vertical and cross section of the container (2) of the electrochemical reactor (1) to show the relative arrangement of the triad of AGSEL (100), CAR (200) and SIRENA (300) systems, which are functionally concatenated as shown, to achieve the objectives of the invention.

[0081] FIG. 3 shows a longitudinal section in elevation of the container (2) with the electrolyte (5) of the electrochemical reactor (1) in operation with the triad of concatenated systems of the electrochemical reactor (1). Controlled atmospheric air flow inputs (210), sustained over time, are shown in each interelectrode space through the multiple parallel flexible longitudinal seals (207) installed in each removable anode cover CAR (201), and thus ensuring, the impossibility of escape of acid mist into the atmosphere (3) over the electrochemical reactor (1), which is kept continuous with a minimum stable depression under the CAR System (200), by means of adequate individual suction in each unit cell of the container (2).

[0082] FIG. 4 shows a general perspective view of the AGSEL System (100) installed in the container (2) with the side walls of the electrochemical reactor (1) removed.

[0083] FIG. 4.1 shows a plan view of the self-supporting monolithic structural frame (101) of the AGSEL System (100), including its structural reticulated reinforcements (115), and the air supply system, to each rectangular module that supports removable air diffusers (102); A preferred embodiment is shown based on end-blind thermo-perforated flexible diffuser tubes (107). Optionally, the feeding system can be duplicated so as to feed the thermo-perforated flexible diffuser tubes (107) at both ends, increasing the overall capacity of diffusion of air bubbles (117) for agitation the electrolyte (5).

[0084] FIG. 4.2 shows a plan view of a typical rectangular air diffuser carrying module (102) with the thermo-perforated flexible diffuser tubes (107) installed in its air distributor manifold (108) and blind counter manifold (109) with the connection air supply at the supply connection point (105) from the self-supporting monolithic structural frame (101).

[0085] FIG. 5 shows in perspective an individual Removable Anodic Cover (201) of the CAR System (200), with the structural body of monolithic polymeric compound (206) of the removable anodic cover (201) provided with multiple parallel flexible longitudinal seals (207) arranged in their vertical sides, which serve to form at least two mini perimeter ventilated chambers (209) when the linear extremes of the multiple parallel flexible longitudinal seals (207) rest on the vertical flat faces of the cathode plates (11) that are inserted at their working positions in the electrochemical reactor (1) intercalated between the anode plates (10).

[0086] FIG. 5.1 shows a cross-sectional view of the electrochemical reactor (1) in elevation and the AGSEL (100) and CAR (200) Systems. The electrical power connections to the electrodes, the anode (10) and cathodic (11) plates are shown by means of the electric bus bar (8), which are installed on the electrode spacer insulating pieces (capping boards) (9). The capping boards (9) determine the length or pitch center to center between the anode (10) and cathodic (11) plates.

[0087] FIG. 5.2 in longitudinal section shows a detail of FIG. 3, of the connection of the container (2) with the SIRENA System (300), and serves to also illustrate the penetration of atmospheric air through the multiple parallel flexible longitudinal seals (207) of the CAR System (200).

[0088] The arrangement and material specifications of flexible seals are designed to allow controlled atmospheric air flow rates (210) to enter with the minimum suction necessary to prevent confined acid mist (3) from leaking into the atmosphere, and at the same time, said suction manages to aerate the mini perimeter ventilated chambers (209), sharing the volume with the acid mist inside. However, the atmospheric ventilation incoming air, due to its lower temperature compared to the acid mist temperature under the CAR System (200), initiates the coalescence of the electrolyte liquid droplets suspended as aerosols in the acid mist, at the same time, that the cold air flow rates of ventilation promote the increase of the already coalesced electrolyte droplets (5).

[0089] FIG. 5.3 shows the same cross-sectional view as explained in FIG. 5.2.

[0090] FIG. 6 shows a front perspective view of the container (2) with the CAR Systems (200) and the SIRENA System (300) in line, and its unified discharge of the global effluent gaseous fluid (503) from both systems to the AVDEVA (315) or global discharge into the atmosphere (311). Also shown is the portable removable device (600), verifier of the flow rate of the effluent gaseous fluid of each individual DEVA V4 (302); and serves to confirm the accuracy of the flow readings delivered by the rotameters (700) over time.

[0091] FIG. 6.1 shows a front view of the electrochemical reactor (1) with the SIRENA System (300) installed on the outer front wall (4) of the container (2) with all the suction and condensation equipment to depurated the extracted gaseous fluid cell by cell (303) of the electrochemical reactor (1), by means of pneumatic devices without moving parts, which is the preferred embodiment of the present invention. In FIG. 6.1, the recovery of the acid condensate is included to substantially recover the condensates from the EW process of the electrochemical reactor (1) in the ACECOA Central Acid Condensate Accumulator (313) for immediate recycling of the condensates back to the process (314) in the electrochemical reactor (1); and also shows the discharge path of the harmless effluent gas flow (304), whose safety is verified (on average every 24 hours) by the AVDEVA Acid Vapor Verification Apparatus (315) before its global discharge into the atmosphere (311). This function of the AVDEVA is required to verify that the triad is properly concatenated and with correct settings to complyvery comfortablythe operation of the EW process within the permissible limits of contamination regulated for the location of each Plant.

[0092] FIG. 7 shows a front view of the installation diagram of an industrial prototype of the cell by cell execution, showing a plurality of 4 electrochemical copper reactors (1), in a configuration for an automatic continuous operation, which is supplied with centralized extraction device for the individual effluent gaseous fluids from the electrochemical reactors (1), by means of a variable speed extraction turbine (316) of the instantaneous global flow of effluent gaseous fluid extracted cell by cell (303), regulated in real time by a Programmable Automation Controller (CAP.sup.(4)) (400) that includes instantaneous monitoring and recording of process variables in real time and firmware for autonomous operation, which includes (optionally) secondary depuration by means of a DECOMUVA (312) device, a multi-stage condenser/depurator of acidic vaporsif requiredto achieve extreme of innocuousness levels of the gaseous fluid effluent from the primary depuration in DEVA V4 (302).

[0093] FIG. 7.1 shows a front view of the installation diagram of an industrial prototype of the cell by cell execution showing a plurality of 4 copper electrowinning electrochemical reactors (1), in a configuration for continuous semi-automatic operation with individual acid mist flow extraction from each electrochemical reactor (1) implemented by individual mini turbines (309) of variable speed, including an external cooling system (not shown) to the heat exchanger (307) in the DEVA V4 (302) (which eliminates need for secondary depuration by ensuring innocuous contents, well below the DS 594 limit of personal exposure); and an instantaneous monitoring and recording system of process variables in real time, and firmware for autonomous operation installed in a prototype of the invention applied to 4 copper EW electrodeposition containers (2), including secondary depuration of the innocuous effluent gaseous fluid (304) from the primary depuration provided by DEVA V4 (302).

DESCRIPTION OF THE INVENTION

[0094] The objectives of the invention are implemented for a set of electrochemical deposition reactors (1) for copperand other non-ferrous metalsoperating with aqueous sulfuric solutions and anodic plates (10) of insoluble lead that generate O.sub.2 bubbles (7), specifically configured to install and allow continuous operation of the triad of systems and equipment to accommodate specific cell by cell copper (and other non-ferrous metal) electrowinning processes conducted in various industrial plants currently operating at densities current of 250-320 A/m.sup.2; the installation and concatenation of the triad in the containers (2) enables them to operate sustainably with current intensities above 400 A/m.sup.2; the innovations presented serve as well for the design and construction of new electrowinning Plants for operation at high current densities from 350 A/m.sup.2 and upwards, incorporating the same triad systems (FIGS. 1 and 2) of the invention, formed by:

(4) CAPabbreviation for Programmable Automation Controller in Spanish AGSEL System (100) Soft Agitation of Electrolyte serves to increase and improve homogeneity in the transfer of ionic mass from the electrolyte (5) to the cathodes (11) (FIGS. 2 and 4);

[0095] CAR System (200) serves to contain, confine, coalesce and recycle acid mist as it is generated in each electrochemical reactor (1) by means of Removable Anodic Covers (201) (FIGS. 1 and 2), and;

[0096] SIRENA Acid Mist Recycler System (300) serves to recycle aerosols and condense polluting vapors (FIGS. 3 and 6).

[0097] The continuous operation of the triad of systems, in the plurality of existing containers (2), in the tankhouse or electrowinning plant, can be operated and maintained concatenated, either manually or automatically, with the incorporation of a suitable Programmable Automation Controller (CAP) (400), which includes access to monitoring and instant registration of process variables.

[0098] The description below includes sufficient details to improve the understanding of the global concatenation of the triad of systems that make up the present invention and their sustained operation over time; therefore, they are incorporated and constitute part of the description with one of the preferred embodiments of the invention, which explain the application of the novel principles of the cell by cell solution and make viable its adoption on an industrial scale in existing industrial containers of the current art.

[0099] The Soft Electrolyte Agitation System (AGSEL) (100) installed in each container (2) of the electrochemical reactor (1), parallel and at a short distance from the bottom of the container (2), shown in FIGS. 2 and 4, is designed to homogeneously diffuse external atmospheric air in the electrolyte (5), feeding the air with control means for pulsating the aeration flow and pressure, so that the rows of small individual air bubbles (117) generated are of given diffused sizes, and above all, precisely directed so that they preferentially act in the intercathode spaces in each unit cell of the electrochemical reactor (1). The controlled directed O.sub.2 bubble agitation of the AGSEL system (100), is discharged directly into the intercathode spaces, is intended to mix uniformly with the natural O.sub.2 bubble agitation from the anodes, so as to generate together a soft upward turbulence parallel to the surfaces of the cathodic (11) and anodic (10) plates; the minimum air flow rates in individual bubble rows are designed from 0.65 liters per minute per linear meter of diffuser tube, which considerably increases the ion mass transfer with the emission of individual bubble rows that favor the homogeneity of the electrodeposit, even at densities above 400 A/m.sup.2, and especially in the lower third portion of the cathode plates (11). Indeed, the decrease in minimum flow rate with controlled directed O.sub.2 bubble agitation according to the present invention is of the order of less than the minimum flow rates of the order of 1.9 liters per minute per linear meter achievable with a non-aeration configuration directed from current art. This consideration is significant because the transversely directed air bubbling system in the intercathode spaces as it is provided with rectangular modules carrying air diffusers (102) allows to increase the overall aeration flow to the container (2) of the order of 2.5 times With respect to the maximums of current gear, that is, the AGSEL System (100) can operate over 200 liters per minute, instead of being limited to about 80 liters per minute of current art systems; likewise, the air supply pressure of the AGSEL System (100) exceeds 200 mbar. Without these increases in controlled aeration capacities the results of industrial operation of the AGSEL System (100) could not accommodate the levels of current intensity increases disclosed in the present invention. All of the above also makes it possible to reduce the diameters of thermo-drilled holes below 0.8 mm in the current art, and/or also to use flexible pipes with smaller diameters and wall thicknesses.

[0100] The sustainability over time of the aeration ranges at the appropriate flow rates and pressures is maintained with a programmable solenoid valve that controls the flow of air supplied by pulses with a determined pressure and frequency that ensures that the holes of the diffuser flexible tubes are maintained free of obstructions.

[0101] In the AGSEL System (100) the minimum separation between adjacent rows of bubbles in the thermo-perforated flexible diffuser tubes (107) directed to each intercathode space can be reduced to 15 mm, a dimension that is 4 times less than the current art minimum of 70 mm.

[0102] The greatest generation of acid mist expected with the operation of the electrochemical reactor (1) at high current intensities is managed in coordination with the online installation of the pair made up of the CAR (200) and SIRENA (300) Systems, to configure with the AGSEL System (100) the triad of the present invention.

[0103] The Soft Electrolyte Agitation System (AGSEL) (100) is installed at a short distance on the bottom of the container (2) of the electrochemical reactor (1), in FIG. 4, radically increases the performance of electrolyte air agitation thanks to the transverse arrangement of the thermo-perforated flexible diffuser tubes (107); as mentioned, this allows duplicating the length of thermo-perforated flexible diffuser tubes (107) for any length of container (2). With what has been said, the AGSEL System (100) is capable of comfortably accompanying up-current intensities in the electrochemical reactor (1) proportional to the increase in intensity above 400 A/m.sup.2, and predictably, up to 600 A/m.sup.2.

[0104] The sustained operation of the electrochemical reactor (1) at high current intensity levels will test, sooner rather than later, the level of manual skill requirement of trained operators to keep the concatenation of the equipment consistently stable over time. Therefore, in order to project the indicated levels of raised current density, both the development and the validation of semi-automatic and automatic process control systems have already been advanced, and even the firmware required for eventual autonomous optimized operation of the complete electrowinning process if desired.

[0105] The air supply to the AGSEL System (100) requires pneumatic feeding devices to deliver a continuous flow range of 0 to 400 liters per minute at a pressure of 0 to 3 atmospheres, with means to generate pulses of controlled duration and spacing, including a rotameter and pressure switch (110); a pipe connects it (optionally) to pneumatic anti-siphon (111) and anti-return (112) devices, after connecting to the air inlet point (103) in the self-supporting monolithic structural frame (101), which is a PVC tube, typically at least 10 inches in diameter, externally reinforced by a continuous filament fiberglass and resin blanket. The air flow moves through the tube through the self-supporting monolithic structural frame (101), which supplies the air at the supply connection points (105) to each rectangular module that supports the air diffuser tubes (102), through the power connection point (105), which in turn feeds the manifold (108) of the rectangular module that supports air diffusers (102) and finally, to the thermo-perforated flexible diffuser tubes (107).

[0106] Each flexible diffuser tube with thermo-drilled holes (107) is attached to the manifold (108) with a feeder connector (106), from which air is diffused in rows of bubbles to the electrolyte (5); the ends of each flexible diffuser tube are blocked with a blind connector (114), where it is attached to the blind counter manifold (109); This, in turn, is fixed to the self-supporting monolithic structural frame (101) by means of bolts (113).

[0107] The distributor manifold (108) is molded of a monolithic polymeric compound and the blind counter manifold (109) houses the blind connectors (114) to remove the thermo-perforated flexible diffuser tubes (107). The manifold (108) is bolted to the self-supporting monolithic structural frame (101) through bolts (113) and likewise, the blind counter manifold (109) is fixed to the homologous member of the self-supporting monolithic structural frame (101) with bolts (113).

[0108] The number of rectangular air diffuser carrying modules (102) in the self-supporting monolithic structural frame (101) depends on the length of the container (2) of the electrochemical reactor (1), on the diameter of the thermo-perforated flexible diffuser tubes (107), and the separation distance between axles; and also of the hole-hole patterns in the surface of the thermo-perforated flexible diffuser tubes (107) and of the diameter of the holes and perforation patterns; all of which determines the air flow capacity required by the AGSEL System (100), which is calculated once the current intensity range at which the electrochemical reactor (1) is to be operated with its complete supply of electrodes is determined.

[0109] The AGSEL System (100) has height adjustable support supports (116) on the floor of the container (2), to be adjustable, as required, to maintain the horizontality of the self-supporting monolithic structural frame (101) with respect to the lower edges of the anode plates (10) and cathode plates (11) of the electrochemical reactor (1); and they can compensate for inclinations of the bottom or floor that the container (2) may have to facilitate its overflow.

[0110] Notwithstanding the foregoing, the AGSEL System (100) can also be supplied prepared to add thermo-perforated flexible diffuser tubes (107) in the total or partial perimeter of the self-supporting monolithic structural frame (101) in order to diffuse additional aeration to obtain effects hydrodynamic that may be necessary to support stable operation at high current intensities, to enhance additional diffusion favorable to the primary objective of directed external air bubbling in intercathode spaces.

[0111] A longitudinal section elevation of an electrochemical reactor (1) shown in FIG. 3, describes a plurality of removable anodic covers (201) that make up part of the CAR System (200) installed on each anode plate (10), together with the covers fixed (202) and (203) at each end of the container (2) of the electrochemical reactor (1) outside the area of anodic plates (10) and cathode plates (11), with which the CAR System (200) is completed for sealing the total surface of the electrolyte (5) with respect to the atmosphere (3) on the electrochemical reactor (1).

[0112] The CAR System (200), container, confiner, coalescer and also recycler of acid mist, in each electrochemical reactor (1), confines the aerosols of the acid mist (6) in the perimeter mini-ventilated chambers (209) where the micro drops of electrolyte in suspension forming drops of greater size and weight; as the micro drops gain weight, they first adhere to the available surfaces pushed by the ventilation generated by the entrance of atmospheric air to the container (2) through the plurality of multiple parallel flexible longitudinal seals (207) of the CAR system (200); As the droplets weight continues to grow, eventually they detach themselves cells from the surfaces to which they adhered, precipitating by gravity to the electrolyte (5) of the electrochemical reactor (1), in fact self-recycling.

[0113] After installing a removable anode cover (201) on each anode plate (10), with two vertical guide horns (204) provided, connected together by a horizontal seating plate (205) (for optional installation of wireless differential pressure sensor (605) (not shown) as required under the CAR System (200)); the vertical guide horns (204) are monolithic with the structural body (206) of dielectric polymeric mortar compound, highly corrosion resistant. The structural body (206) on both outer lateral sides, lodges multiple parallel flexible longitudinal seals (207) that protrude horizontally to contact the adjacent cathodic plates (11); while towards the inside of the lateral sides of the structural body there are two rows of flexible clamping tongues (212) to affix each anodic removable cover (201) onto each anodic plate (10). On the front ends, there are affixed two separate front seals (208) that cover the electrolyte (5) over the lateral channels (211) of the container (2). The multiple parallel flexible longitudinal seals (207) form at least two superimposed mini perimeter ventilated chambers (209), to: a.-) Promote the coalescence of the acid mist confined inside; coalescence is enhanced by ventilation with the entry of controlled flow rates of atmospheric air (210) that keep the mist confined under the multiple parallel flexible longitudinal seals (207). Coalescence takes place in the perimeter mini-ventilated chambers (209), since the controlled atmospheric air flow rates (210) are at a lower temperature than typical 50 C. of the electrolyte (5) in the copper electrowinning process, favoring the initiation of coalescence of the acid mist (6) with growth in size of the aerosols until reaching such a size that, due to their own weight, they fall back into the hot electrolyte (5) in the container (2) of the electrochemical reactor (1) that originated them. Recycling occurs simultaneously with the generation of acid mist in the operation of the electrochemical reactor (1), b.-) The multiple parallel flexible longitudinal seals (207) designed for the entry of atmospheric ventilation with the suction by the SIRENA system (300) in each mini ventilated perimeter chamber (209) of each removable anode cover (201) also serve to sweep cathodic and anode surfaces and keep them clear of vapors and aerosols, thereby providing anti-corrosive protection for body/hanger bar welds cathodic (11) and anodic (10) plates due to the possible presence of anions, (which are generally present in the electrolyte (5) and come from the ore leaching stage, as entrained contaminants). Removable Anodic Covers (201) substantially prevent the formation of copper sulfate in the socket contacts of the electric bars/electrode hanger bars, thus avoiding process current leaks.

[0114] To implement anion protection with the multiple parallel flexible longitudinal seals (207) of the CAR System (200) it is necessary to establish the average level of the electrolyte (5) in the industrial container (2) of the current artor in the electrochemical reactor (1)of a given Plant or tankhouse, to fix the distance of the multiple parallel flexible longitudinal seal (207) with respect to the position of the structural body of monolithic polymeric compound (206) of the removable anode cover (201) already seated on the anodic plate (10) such that the line of contact of the multiple parallel flexible longitudinal seal (207) of the mini perimeter ventilated chamber (209) closest to the level of the electrolyte (5) with the cathodic plate (11) is just above said level, so that the volume of gaseous fluid confined by the CAR System (200) in the electrochemical reactor (1) is entrained and extracted from it together with the acid mist.

[0115] With reference to the drawings, FIG. 3 and FIG. 6 show sectional views of the SIRENA System (300) including the collection manifold (301) of the effluent gaseous fluid extracted cell by cell (303) from the reactor container (2) electrochemical (1) to deliver it to the DEVA V4 gaseous effluent vapors depurator (302) attached to one of the ends of the electrochemical reactor (1) with its ducts for feeding the extracted gaseous fluid flow cell by cell (303) of each electrochemical reactor (1).

[0116] The SIRENA System (300), linked in line with the CAR System (200), recovers and substantially reduces acidic vapors, recycling the acid mist aerosols (6) remaining in the flow of the gaseous effluent fluid extracted cell by cell (303) of the electrochemical reactor (1), to be immediately depurated, outside the container (2) of the electrochemical reactor (1), in the first instance, by means of a gaseous fluid bubbler (305) that operates under a liquid column (306) of adjustable height in the DEVA V4 acid effluent vapor depurator (302) installed on the outer front wall (4) of each container (2). Each bubbler (305) of the DEVA V4 (302) recovers substantially, of the order of 9598% of the uncoalesced micro aerosols in the container (2) and which are dragged to the DEVA V4 (302) and recovered in the form of liquid condensate; at the same time, on the liquid column (306) of the bubbler (305), always inside the DEVA V4 (302), with the bubble, bubble explosions take place when emerging from the level of liquid condensate. To minimize water vapor and new aerosols generated in DEVA V4 (302), forced condensation is introduced by means of a heat exchanger (307), to substantially recover the new aerosols and vapors in the effluent gaseous fluid extracted from the DEVA V4 (302). The suction of the extraction flow of the extracted effluent gaseous fluid cell by cell (303), is provided, in the preferred embodiment, by means of a pneumatic air amplifying device (500), which operates with dry and compressed atmospheric air (801), preferably provided by a screw compressor (800), or alternatively, with a mini turbine (309) provided with its frequency variator (310) to control the extraction flow, installed in each container (2) of the electrochemical reactor (1).

[0117] The continuous operation over time of a plurality of electrochemical reactors (1) requires setting the overall flow rate of extraction of individual effluent gaseous fluid from each electrochemical reactor (1), in such a way that said suction maintains a depression over time of at least 2 mbar under the removable anode covers (201) of the CAR System (200) of each container (2) of the electrochemical reactor (1). This condition is essential to guarantee zero emission of acid mist from the electrochemical reactor (1) to the working environment.

[0118] The triad of the present inventionas statedcan be operated and maintain the indicated essential condition manually, automatically or autonomously.

[0119] In case of using a Programmable Automation Controller (CAP) (400); with or without autonomic capacity, the mini extraction turbines (309) or preferably, the air amplifiers (500) and Vortex tubes (501), in each electrochemical reactor (1), are in charge of moving the extracted effluent gaseous fluids cell by cell (303) of each electrochemical reactor (1) discharging them directly to their DEVA V4 acid effluent steam depurator (302), which when cooled prior to their global discharge into the atmosphere (311), by heat exchanger (307) with atmospheric air cooled preferably by pneumatic device Vortex Tube (501), or alternatively by a Chiller (308) that cools conventional refrigerant fluid, such as Glycol, cooled in a range of 1 to 4 C.

[0120] The SIRENA System (300) is designed to safely discharge the global gaseous effluent from each electrochemical reactor (1) directly into the atmosphere. Alternatively, or as required, the SIRENA (300) is also designed to be able to incorporate online, prior to discharge to the atmosphere, a second DECOMUVA multi-stage depurator/condenser (312) and to couple a pneumatic air supply system atmospheric pressure of the triad to maximize the safety of the effluent gaseous fluid.