Abstract:
A vessel for contacting a plurality of objects with a fluid. An upwardly directed stream of fluid and a portion of the objects are confined in a conduit such that the fluid stream causes the objects to flow upward from a moving bed thereof to a disengaging position from where they fall onto a distribution shield and move downward to a feed position. The vessel may be used for treating electrically conductive objects wherein the fluid is an electrolyte, an electrode is positioned to contact the moving bed, and a counterelectrode is positioned in spaced relation to the moving bed. The vessel may be fixed or portable.

Description:
RELATED APPLICATIONS 
     This application claims the benefit of U.S. Provisional Application No. 60/068,498, filed Dec. 22, 1997, and is a Continuation of International Application No. PCT/US00/35413 filed Dec. 28, 2000 (filed and to be published in English), which was a Continuation-In-Part of U.S. Aplication Ser. No. 09/216,859 filed Dec. 21, 1998, now U.S. Pat. No. 6,193,858 issued Feb. 27, 2001, the entire contents of this patent and these prior applications being expressly incorporated herein by reference. 
    
    
     FIELD OF THE INVENTION 
     The invention relates to the use of spouted beds of particles, pieces, parts and other small objects for the treatment thereof in a liquid or gaseous fluid. The invention has particular application for the electroplating of small parts which are difficult to plate by conventional means. The invention also has application in the fields of wastewater treatment, electrowinning, electrochemical synthesis, anodic electrochemical smoothing, anodizing, electrophoretic polymer coating, and physical coating, as well as in the general field of spouted bed applications. 
     BACKGROUND OF THE INVENTION 
     Barrel plating, in which objects are tumbled in a perforated horizontal rotating drum, is a common method of electroplating small parts. Representative technology is disclosed in U.S. Pat. No. 4,822,468 by Kanehiro and U.S. Pat. No. 4,769,117 by Shino, et al. Many very small parts cannot be plated effectively in a barrel due to poor contact with the current feeder or fouling on the interior of the drum. These problems often necessitate the addition of plating media (typically some type of smooth metal shot) to the barrel to improve cathodic contacting and part motion. The use of media significantly increases the required plating time and current because the media is also plated and, therefore, the plating cost per part is increased. Additionally, many small parts are fragile or can interlock and may be damaged by tumbling with heavy media. Consequently, these parts cannot be plated successfully in barrels. 
     U.S. Pat. No. 5,487,824 by Greigo discloses and integrated electroplating system designed specifically to electroplate very small parts which employs a horizontal accelerating rotating drum to maintain a packed bed of parts in motion during electroplating. 
     U.S. Pat. No. 3,1124,098 by Backhurst et al. and U.S. Pat. No. 3,703,446 by Haycock et al. disclose fluidized bed cathodes. Although fluidized beds have excellent liquid-solid contacting, fluidized bed cathodes suffer from poor electrical contact between the fluidized particles, non-homogeneous electrical potentials and particle segregation effects. Additionally, it is difficult to maintain the entire bed fluidized when the particles are changing in size, and possibly density, due to metal deposition. It is unlikely that the potential benefits of the fluidized bed approach will be realized in a practical electrodeposition system. 
     Typical spouted beds consist of a cylindrical vessel with a conical bottom section. The vessel contains a bed of particles which form the spouted bed. Fluid is introduced into the spouted bed vessel at the bottom of the conical section as a jet. This fluid jet penetrates the bed of particles contained in the spouted bed vessel, entraining particles and forming a “spout” of upward moving particles and fluid. The particles disengage from the fluid flow in a region above the particle bed and then fall on top of the downward-moving annular bed. The “pumping action” provided by the spout circulates the particles through the vessel in a torroidal fashion; upwards in the spout and downwards in the annular moving bed. A “draft pipe” may be incorporated into the vessel to assist in the fluid transport of the particles. The draft pipe consists of a tube which is fixed coincident with the location of the spout, directly above and aligned with the liquid jet. The draft pipe delays the dispersion of the liquid jet and allows particle transport over a broader range of fluid velocities while also stabilizing the liquid flow. 
     U.S. Pat. No. 4,272,333 by Scott discloses the use of a moving bed electrode (MBE), in which conductive particles move downward vertically in a packed bed between two electrodes, the anode being shielded with a membrane. The necessity of using a membrane to shield the anode makes this configuration less attractive for practical applications, since the mechanical abrasion of the moving bed of particles can damage the membrane in a short time. Additionally, metal deposition on the membrane may be a complication. 
     An article by Hadzismajlovic et al. published in Hydrometallurgy, Vol. 22, pages 393-401 (1989), and U.S. Pat. No. 1,789,443 by Levin disclose the use of spouted bed cathodes with nodes suspended above the spouted bed surface. Although this configuration may eliminate the complication of shielding electrodes using membranes, several operational problems may be encountered with this configuration. Many electrolytes have poor electrical conductivity; therefore, it is advantageous to have the cathode and anode in close proximity in order to reduce the voltage drop over the cell. This cannot be accomplished in these prior art systems, since the spout would collide with the anode. Additionally, the projected spouted bed geometric surface area is very limited, impairing electrode performance. 
     Conventional spouted beds also suffer from a particle recirculation problem commonly referred to as “dead spots”, where a portion of the particle bed is stagnant. Dead spots usually exist at the outer edge of the spouted bed surface and are attributable to a failure of the spout to deposit particles at the circumference of the spouted bed. In an attempt to remedy this problem, spouted beds with very steep bottom cone angles have been adopted. In all cases, the radius of the spouted bed has been strictly limited to the distance to which particles in the spout can be transported radially outward by the fluid flow. 
     SUMMARY OF THE INVENTION 
     In the present invention, a distribution shield consists of a solid conical section extending from the vicinity of the upper edge of a draft pipe downward and radially outward towards the vessel sidewall above or beyond the outer edge of a downwardly moving packed bed surface, and is used to convey parts, pieces, particles or other small objects to the outer edge of the spouted bed by preventing the objects from falling near the center of the spouted bed surface. Instead, the 
     objects disengage from the spout and are deposited on the upper surface of the distribution shield. The objects then move along the top surface of the distribution shield until they are deposited at or beyond the outside edge of the moving bed surface. 
     Use of the distribution shield totally eliminates stagnant areas at the circumference of the spouted bed. Moreover, the distribution shield allows very large diameter spouted beds to be constructed at modest fluid flow rates, since it is no longer necessary to transport objects to the spouted bed circumference dynamically via the fluid flow. Additionally, when a distribution shield is used, large diameter shallow spouted beds with shallow bottom cone angles may be employed. In this type of bed, the motion of the objects is more radially inward rather than downward. This type of spouted bed is particularly advantageous for circulating fragile objects where the weight of a deep bed may crush or break the objects and is particularly useful for spouted beds of conductive or partially conductive parts used as high performance electrodes where large projected areas and shallow bed depths are desirable. 
     A portable electroplating apparatus, which incorporates a pump and a vessel which defines a spouted bed electrolytic reaction chamber, is also provided by the present invention. The portable electroplating vessel can be conveyed from process tank to process tank by hand, automated plating system, or hoist. The spouted bed vessel is mounted on a platform with a pump to provide the necessary electrolyte flow for the spouted bed chamber. It is advantageous to incorporate a liquid by pass circuit and adjustment valve so that the liquid flow to the spouted bed chamber can be adjusted. It is also desirable for the spouted bed vessel to be easily detachable from the portable apparatus and also for the internal components to be easily detachable from the vessel to facilitate access to the vessel interior. 
     In the practice of the present invention, conductive parts are electroplated while being circulated in a liquid spouted bed, in which the liquid is an electrolyte containing metal ions. The parts form a moving packed bed which is maintained under cathodic current by being in contact with a current feeder. The passage of current through the parts causes metal to be deposited from the electrolyte onto the parts as they circulate in the apparatus. Typically, the parts are retained in a non-conductive cylindrical vessel with a conical bottom section, although vessels with other geometries may also be used. The vessel may be made of a non-electrically conductive plastic material, for example polypropylene. 
     The electrolyte is introduced into the vessel as a jet at the bottom of a conical section into the bed of parts to be plated. The liquid jet entrains parts which disengage from the liquid flow in a region above the moving bed and then move radially inward and downward as a moving packed bed of parts. The action provided by the liquid jet thus circulates the parts through the vessel; first upwards and radially outward in the jet and then downward and radially inward in the packed bed. 
     The cathodic connection is made with the packed bed via metallic contacts or a current feeder attached to the inside of the conical section, or inserted into the packed bed from above. If the surfaces of the parts to be plated are entirely conductive, the current feeder may be small in size with respect to the particle bed. If the parts are partially conductive by having non-conductive elements, as is the case with surface mounted electronic components, it is desirable to employ current feeders with a much larger surface area to insure that electrical contact is made with the conductive portions of the parts during their movement in the moving bed. For example, a majority of the surface of the bottom conical section may be lined with a conductive material and used as a current feeder. The counterelectrode (anode) maybe suspended above the moving packed bed in the spouted bed chamber, or may be external to the vessel defining the spouted bed chamber. 
     The invention also may use a current feeder with a bumpy or otherwise textured surface to facilitate movement of the objects and to prevent the objects from sticking to the current feeder during electrodeposition. Bumps about the size of the objects are particularly useful for preventing rectangularly shaped objects from jamming together and “tiling” as they slide over the current feeder. Moreover, a bumpy or otherwise textured current feeder surface reduces the contact area between the objects and the current feeder, thereby decreasing the possibility that the objects will become fused to the current feeder during electroplating. 
     It is preferable to incorporate a “draft pipe” into the vessel to assist in the hydraulic transport of the parts. The draft pipe consists of a tube which is fixed coincident with the location of the spout, directly above and aligned with the liquid jet. The draft pipe delays dispersion of the liquid jet and allows part transport over a broader range of liquid velocities. 
     Additionally, it is preferable to employ a parts deflector located above the draft pipe. The parts deflector is a conical point or a flat disk or a downwardly facing concave surface which is located above the spout. The reflector prevents the parts in the spout from exiting the chamber and directs the part trajectories toward the sidewall of the vessel. It also prevents the jet of entrained parts from colliding with any overhead components in the chamber. The parts deflector is particularly advantageous in conjunction with the draft pipe, since the presence of the draft pipe strengthens the flow of the spout. 
     It is also preferred to employ a distribution shield. The distribution shield may be conical and extends from the vicinity of the upper edge of the draft pipe to above the outer edge of the inclined bottom wall of the vessel. This shield aids in distributing the parts to the outer edge of the spouted bed by preventing parts from falling near the center of the reaction chamber. Instead, these parts move along the top surface of the shield until they are deposited at the outside edge of the moving bed of parts. 
     In the present invention, the counter electrode, which is typically the anode, may be located inside the spouted bed vessel above the moving packed bed of parts, either under the distribution shield, or above the particle deflector. Alternately, external counter electrodes may be used, i.e., electrodes that are external to the spouted bed vessel. In the case of external counter electrodes, the counter electrodes are located in proximity to the spouted bed vessel which is at least partially immersed in the electrolyte. Openings are provided in the immersed portion of the sidewall(s) and/or bottom wall(s) of the spouted bed vessel to allow the passage of current via the electrolyte from the external counter electrodes to the moving packed bed of objects contained in the spouted bed vessel. The submerged vessel openings may be covered by a mesh, cloth or membrane which allows the passage of electrical current and prevents the loss of the objects from the spouted bed vessel. These openings may also serve as means for the electrolyte to enter and exit the spouted bed vessel. 
     Typically, external soluble anodes comprised of the same metal as is dissolved in the electrolyte are desirable in electroplating applications where the spouted bed vessel is conveyed between a plurality of processing tanks. On the other hand, an internal insoluble anode is desirable in stationary electroplating applications and in electrowinning. The present invention may also be practiced using rectangular vessels with slanted bottoms. In this case, the distribution shield would be an angled flat plate or plates, and the draft pipe and inlet pipe may be either tubular or rectangular. 
     The liquid electrolyte is injected into the reaction chamber via a pump and, during operation, this arrangement presents no difficulties. However, when operation of the device is interrupted, the parts from the bed may fall into the outlet of the pump via gravity, effectively fouling the pump. Therefore, a means of retaining the parts in the vessel is provided. One approach is to incorporate a screen at the jet inlet which will not allow the parts to pass. If a screen is used, it is preferable to filter the fluid upstream of the screen to prevent fouling. An alternate approach is to utilize a solid “trap” arrangement. This can be a simple “U” pipe on the inlet line, or can consist of two concentric pipes which cause the liquid to reverse direction. In either case, the 
     parts are trapped due to their density difference with respect to the electrolyte. An access port can be incorporated into the trap to allow the parts to be conveniently removed from the spouted bed chamber. 
     The present invention also contemplates that the spouted bed vessel may be used in a stationary configuration in which the various cleaning, plating and rinse solutions are sequentially introduced from separate holding tanks, circulated through the reaction chamber for the appropriate time, and then purged from the spouted bed vessel via a manifold piping system connected to solution reservoirs, control valves, control system and pumps. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       The invention and its assembly and operation may be further understood from the following description of the preferred practices thereof, which are shown by way of example in the accompanying drawings wherein: 
         FIG. 1  is a cross-sectional elevational view of a portable spouted bed electrochemical reactor vessel and a stationary electrolyte tank and docking system made in accordance with the present invention; 
         FIG. 2  is a cross-sectional elevational view of a modification of the portable spouted bed electrochemical reactor vessel of  FIG. 1  wherein both bottom wall and sidewall openings are covered with mesh and current feeders are suspended from above the chamber bottom; 
         FIG. 3  is an exterior top view of a spouted bed plating apparatus as modified to provide a elf contained portable unit in accordance with the invention; 
         FIG. 4  is a cross-sectional elevational view of the apparatus of  FIG. 3  as taken along line 4—4 of  FIG. 3 ; 
         FIG. 5  is a cross-sectional elevational view of a modified spouted bed electrochemical reactor vessel having a shallow conical bottom and a concentric annular parts trap with a parts removal port; 
         FIG. 6  is a diagrammatic illustration of a fluid system for providing multiple treatment solutions to a reactor of the type shown in  FIG. 1 ,  2  or  5 ; 
         FIG. 7  is an enlarged fragmentary sectional view of a detail of the invention shown in  FIG. 1 ; 
         FIG. 8  is a graph showing current efficiency as a function of current density for the electrolytic recovery of silver from a cyanide solution in a spouted bed electrochemical reactor of the invention using 3 mm and 6 mm spheres as compared to using a plane electrode, with and without agitation; 
         FIG. 9  is a graph showing the silver recovery rate from a cyanide solution as a function of current density in a spouted bed of the invention, as compared to using a plane electrode in an agitated solution; and, 
         FIG. 10  is a graph showing the copper concentration as a function of time for recovery of the metal from a copper sulfate solution at pH 1.9 using a shallow 12″ diameter spouted bed reactor of the invention as compared to using a deeper 7.5″ spouted bed reactor. 
     
    
    
     DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS 
     Turning now in greater detail to the appended drawings,  FIG. 1  shows a detailed cross-sectional view of a portable spouted bed reaction chamber or reactor  1 , removably situated in a stationary process tank  40 . The stationary process tank  40  is equipped with a pumping system to supply a liquid stream of electrolyte to spouted bed chamber  1 , and is further equipped with stationary electrodes  8 , which are external to the chamber  1  and function as counter electrodes to the objects contained in chamber  1 . When electroplating objects, electrodes  8  function as anodes. The contained objects may be the same as objects  124  in  FIG. 5 , but these objects have been omitted from  FIG. 1  for clarity. Tank  40  may be one of a series of process tanks between which portable spouted bed chamber  1  is conveyed during an electroplating process that will circulate through chamber  1  successive processing solutions, such as cleaning, plating and rinsing solutions. As an alternative, chamber  1  (or chamber  1 ′ in  FIG. 2 ) may be fixed to tanks  40  and successive processing solutions passed through tank  40  from a plurality of process tanks as shown in FIG.  6 . 
     The spouted bed chamber  1  consists of a cylindrical vessel  2  with a conical bottom  11  and a detachable top  12 . Vessel  2  is made of a material, such as polyethylene, that is not electrically conductive. The spouted bed chamber  1  is partially immersed in the electrolyte contained in tank  40 , as is indicated by liquid surface S. The electrolyte is injected into the chamber  1  by an external pump  34  via a ball flow regulating valve  32 , a socketed fitting  30  and an inlet pipe  18  having an attached mesh screen  17 . Pump  34  is connected in a closed loop that is completed by tank  40 , a tank outlet fitting  38 , a liquid strainer  36  and associated plumbing. 
     The portable spouted bed chamber  1  may be detachably connected to tank  40  by inserting inlet pipe  18  into socketed coupling  30  as shown in FIG.  1 . The inlet pipe is connected to the spouted bed vessel  2  via socketed receptacle  19 . Pin  15  is used to retain inlet pipe  18  in socketed receptacle  19 . Mesh screen  17  is attached to the end of inlet pipe  18  and retains the treated objects in the vessel  2  when the liquid flow through the vessel is discontinued. Pin  15  and inlet pipe,  18  and attached mesh  17  can be easily removed to allow the unloading of objects from the bottom of vessel  2  of the spouted bed chamber  1 . 
     Liquid enters vessel  2  via the inlet pipe  18  and forms a jet which entrains parts or objects that are fed below draft pipe  4 . The liquid jet with entrained objects (not shown) moves through the draft pipe  4  and impinges on a deflector  6  having a downwardly facing concave surface  7 . Deflector  6  directs the entrained objects radially outward and downward, thereby disengaging the objects from the liquid jet. The disengaged objects are deposited on the top surface of a distribution shield  20  where they move radially outward and downward until they slide off the outer edge of shield  20  and are deposited on the upper surface of a clamping ring  28  around the upper edge of the chamber bottom  11  where they move downward and radially inward in a moving packed bed towards the gap between the upper end of inlet pipe  18  and the lower end of draft pipe  4 . 
     The distribution shield  20  is attached to the chamber top  12  via vertical supports  22 . The chamber top  12 , supports  22 , distribution shield  20 , deflector  6  and draft pipe  4  form a detachable assembly which is readily removed by lifting the chamber top  12  from the spouted bed vessel  2 , thus providing internal access to vessel  2 . A small hole (not shown) may be provided in a top portion of the draft pipe adjacent the shield to vent any cathode gases from under the shield to the moving liquid stream in the draft pipe. 
     Electrical contact with the moving bed of objects is made by a conical current feeder  16  that is electrically conductive and lines the conical vessel bottom wall  11 . Current feeder  16  is connected to an external electrical power supply by a cathodic connection comprising an electrically conductive cylindrical plunger  10  that penetrates the chamber bottom wall  11  and makes sliding contact with a current feeder block  25  having a cylindrical socket for receiving a lower portion of plunger  10  and a coil spring  9 , as shown in greater detail in the enlarged view of FIG.  7 . Spring element  9  is situated below plunger  10  and provides resilient pressure to maintain positive electrical contact between the upper face of plunger  10  and the bottom surface of current feeder  16 . Current feeder block  25  is insulated by a polymeric layer or covering  13 , and is connected to a cathodic connector  23  by an insulated conductor  27 . As an alternative, current feeder  16  may be connected to the external power supply by contact with a countersunk flat head bolt (not shown), which penetrates the bottom wall  11  and is threaded into the insulated metal connecting block  25  to thereby affix it to the bottom wall. 
     Current feeder  16  may be a conical metal sheet held in place by a clamping ring  28 , which is made of an electrically insulating material and prevents the treated objects from fouling on the outside edge of the current feeder  16 . Current feeder  16  instead may be a metal layer coated or deposited onto the bottom wall  11 . The upper (outer) surface of current feeder  16  may have bumps, or be roughened or otherwise textured to facilitate movement of the objects thereover. 
       FIG. 7  also shows that a gap G may be provided between the bottom surface of clamping ring  28  and the upper surface of current feeder  16 . Gap G is preferably from about 0.2 to 1.0 mm and should be smaller than the parts being plated. Gap G dissipates a high current density area which tends to form at the insulated edge of a conductor that is under current in an electrolyte. Providing a gap lowers the current density in this area and inhibits nodular growth of deposited metal at the intersection of the lower edge of ring  28  and the upper surface of current feeder  16 . This is particularly beneficial when electroplating partially conductive parts, such as surface mounted components. If a gap is not provided, nodular growth of metal deposited in this area can interfere with part recirculation. 
     It is also sometimes beneficial to extend clamping ring  28  further down to cover a greater portion of current feeder  16  to help maintain particle movement if there is a tendency for plated parts to fuse to an upper portion of the current feeder. Insulating more of the upper portion of the feeder  16  by extending clamping ring  28  downward creates greater downward pressure on the parts in contact with the lower portion of the current feeder to maintain part movement. The optimum width of the clamping ring  28  can be determined by a few trial runs and will depend on the shape of the parts being plated, the load size and the plating electrolyte. On the other hand, increasing the width of clamping ring  28  will increase the voltage when plating partially conductive parts, since the active feeder surface area will be reduced. Therefore, it is desirable to use as narrow a clamping ring as possible while still maintaining adequate part motion. 
     In the embodiments shown in the drawings for coating objects with a metal constituent of the electrolyte, the electrodes in contact with the moving bed of objects are connected to the negative terminal of the power source and function as cathodes, and the counterelectrodes  8  mounted in the stationary tank  40  in proximity to vessel  2  are connected to the positive terminal of the power source and function as anodes. Current is conducted from the anodes to the moving objects via one or more openings  26  in the sidewall of vessel  2 , these openings being covered by a porous mesh, cloth or membrane for retaining the objects within the vessel while passing the liquid. Thus, liquid exits the vessel  2  via the mesh openings  26 . 
     In implementing the embodiment of  FIG. 1 , as well as the embodiments of  FIGS. 2-4 , a pumping means and a docking means may be provided for each of a series of process tanks. An automated means for detecting the presence of a reactor vessel in each process tank may also be provided and used to automatically switch on the pump serving the tank. The detection means may be a physical contact switch (not shown) in the tank, or a magnetic hall effect sensor  72  on the outside of the tank and a magnet  73  attached to the inlet pipe  18  of the reactor vessel as shown in FIG.  1 . The detection means may also include a relay module  74  responsive to inputs from sensor  72  to control the A.C. power supply  76  for operating the pump  43 . In the embodiment of  FIGS. 3 and 4 , the sensor  72  could be located under the lip  71  in the vicinity of the position for a rail  70  and the magnet  73  attached to the corresponding rail. For such a physical or magnetic detection means, there may be substituted an optical detector, or any other means which can be effectively implemented to serve this purpose. Thus, it is an object of the present invention that the pump for each tank used with the embodiments of  FIGS. 1-4  may be automatically activated when a reactor vessel is present and deactivated when the tank is empty. 
       FIG. 2  illustrates a spouted bed electrochemical reactor  1 ′ similar to that depicted in  FIG. 1  except that there are openings  31  in the vessel bottom wall and these openings are covered with a plastic mesh  33  to retain the circulated parts (not shown) within vessel  2 ′. Components that are essentially the same as those in  FIG. 1  have the same numerical designations with the addition of a prime symbol (′). Cathodic contact is made with the moving bed of parts via conductive rods  35  that have an insulating sleeve  37  and are attached to the chamber sidewall an to electrical connectors via bolts  39 . The conductive rods are coated or covered with the insulating sleeve  37  except for exposed tips which are in contact with the moving bed of parts. The circulation of parts in the apparatus of  FIG. 2  is the same as that in the apparatus of FIG.  1 . The mesh covered openings  31  in the bottom wall of the chamber allow a more direct current path between the cathodic moving bed of parts and the external anodes  8 ′ than the apparatus in FIG.  1 . which has sidewall openings only. This results in significantly reduced voltages during electroplating. 
     The openings  31  in the chamber bottom wall also enhance the draining of solution from the chamber vessel  2 ′ after cleaning, electroplating and rinsing processes. On the other hand, the apparatus of  FIG. 1  has a much greater current feeder surface area than that of FIG.  2 . Therefore, the apparatus of  FIG. 1  is more suitable for the electroplating of partially conductive parts such as surface mounted electrical components, whereas the apparatus of  FIG. 2  is more suitable for the electroplating of metal parts or components. A small hole  43  may be provided in a top portion of the draft pipe  4 ′ adjacent the shield  20 ′ to vent any cathode gases from under the shield to the moving liquid stream in the draft pipe. 
       FIG. 3  shows a top view of a portable plating apparatus  41  having a spouted bed reactor vessel  50  removably situated in a process tank  87  containing a process solution L. This apparatus may be used in an analogous manner to a plating barrel or plating rack in that it is designed to be conveyed from tank to tank for circulating through vessel  50  successive processing solutions, such as cleaning, rinsing, and plating solutions. 
       FIG. 4  shows a sectional view of apparatus  41  taken along line  4 — 4  of FIG.  3 . The lower portion of the apparatus is immersed below the surface S of the process solution L, and the entire apparatus is supported by side rails  70 ,  70 , which rest on a sidewall lip  71  of each process tank  87  and are equipped with handles  86 ,  86 . The apparatus includes transverse platforms  52  and  54 , which connect the side rails  70 ,  70 . A submersible head centrifugal pump  88  is mounted on platform  54 . The inlet of the pump is attached via an elbow  94  to a liquid strainer  95 . The outlet  96  of the pump is connected via a short segment of plastic pipe to a plastic T fitting  97 . 
     The inlet pipe  98  of the spouted bed vessel  50  is detachably coupled to the T fitting  97 . The third opening of the T fitting  97  is attached via a plastic pipe and elbow  99  and a plastic pipe  60  to a bypass ball valve  90 . The outlet of ball valve  90  returns solution to the process tank  87  via the segments of plastic pipe and elbows shown in  FIGS. 3 and 4 . The amount of solution circulated through the spouted bed vessel  50  can be adjusted by using the bypass valve  90 . The spouted bed vessel  50  is open to the atmosphere and has mesh covered openings  56  in the lower chamber sidewall. Solution is returned to the process tank via the mesh enclosed openings  56 . 
     The negative direct current electrical connection (cathode) to the circulated objects in vessel  50  is via an electrical connector  48  passing through the sidewall of vessel  50 . The counter electrodes or anodes  44  are suspended in the process tank  87  in proximity to the vessel  50  by conductive connectors  43  carried by conductive support rods  42 , which are connected to the positive terminal of a direct current power supply. Current passes between anodes  44  and the circulated objects contained in vessel  50  via openings  56  in vessel  50 . The internal components of vessel  50  are identical to those illustrated in vessel  2  of FIG.  1 . 
       FIG. 5  shows a spouted bed electrochemical reactor  100  with a vessel  119  containing a draft pipe  116 , object deflector  101  and distribution shield  123 . The vessel  119  is cylindrical with a conical bottom  106  and a conical top  120 . The liquid  5  electrolyte is injected into a chamber of the vessel through an objects trap consisting of an inner inlet pipe  113  and a concentric outer pipe  112 . The outer pipe  112  has a threaded access port  111 . The access port  111  is sealed by a cap  109  held in place by a threaded clamping ring  110 . Liquid enters the annulus formed by concentric pipes  112  and  113  via a threaded pipe  108 . Parts  113 ,  112 ,  111 ,  110 , and  109  form the objects trap, which retains the objects  114  of the conductive bed  124  in the chamber when the liquid flow through the chamber is discontinued. The trap may also be used to discharge the coated objects from the chamber by removing cap  109  from the access port  111 . Liquid enters the chamber via the inlet pipe  113  and forms a jet stream which entrains objects  114  as they are fed through a gap  115  below the draft pipe  116 . 
     The liquid jet, with entrained objects, moves through the draft pipe and impinges on the deflector  101 . The deflector  101  directs the entrained objects outward and disengages them from the liquid jet. The disengaged objects fall onto the distribution shield  123  and move radially outward until they are deposited at the outer edge of the bottom wall  106 , where they move downward and radially inward towards the draft pipe  116  and gap  115  in a moving packed bed  124 . The distribution shield  123  is mounted in the chamber via supports  118  resting on the chamber bottom wall  106 . The angle A from the horizontal to the bottom wall  106 , and the angle B from the horizontal to the upper surface of the distribution shield  123 , are preferably in the range of 10° to 70°, more preferably in the range of 20° to 60°, and most preferably 20° to 50° for round objects and 35° to 60° for non-round objects. 
     Electrical contact with the bed  124  is made by flat head bolts  107  which penetrate the chamber bottom wall  106  and contact the moving bed of objects  124 . The counterelectrode  105  is located under the particle distribution shield  123  and is connected to the external power supply (not shown) via a connector strip  104  and a bolt  103 , which penetrates the sidewall of the vessel  119 . The bottom surface of the distribution shield  123  is sloped upwards and radially outward so that evolved gases easily exit the chamber without being trapped under the shield. A deflector ring  117  mounted around the draft pipe  116  prevents objects from impinging against the counterelectrode  105 . Liquid exits the spouted bed chamber via a threaded pipe fitting  122  having inlet apertures  121  and  10  attached to the conical cover  120 , which seals the spouted bed vessel  119  via an O-ring  102 . A conical cover facilitates the complete removal of gases evolved during electrolysis. 
       FIG. 6  shows a schematic diagram of an electroplating fluid system which incorporates a stationary spouted bed electrochemical reactor of type  100  of FIG.  5 . Reactor  100  is connected via electrical cables  134  and  135  to a stationary power supply and control panel  132 . Solutions for the electroplating process may include cleaners, acids, plating solutions and rinses contained respectively, in tanks T 1  to T 6 . The objects to be plated are loaded into the spouted bed vessel  100 . Then, solutions from tanks T 1  to T 6  are delivered separately to the spouted bed reactor  100  via inlet line  138 , solenoid valves  142 , inlet manifold  146  and pump  136 . Solution exits the spouted bed reactor  100  via outlet line  144 , outlet manifold  147  and solenoid valves  140 . 
     During the electroplating process, the inlet and outlet solenoid valves to one process tank will be opened and the pump actuated to circulate the solution to and from the process tank in a closed loop. Each tank will be circulated in turn so that an electroplating process may be accomplished. The solenoid valves  140  and  142 , power supply and control panel  132 , and pump  136  may be actuated manually by switches  139  or may be computer controlled. At the end of the plating process, the plated objects are removed from vessel  100  and the process is repeated. Since only one inlet and outlet set of solenoid valves connected to process tanks T 1  to T 6  will be open at any time, remotely actuated, multi-port rotary selector valves may be substituted for separate solenoid valves  140  and  142 . 
     EXAMPLES OF ELECTROPLATING 
     Example 1 
     A portable plating apparatus with a 7.5 inch diameter spouted bed chamber having a draft pipe and particle distribution shield was used to electroplate 2 mm long, 0.7 mm diameter, stamped copper connector clips. These clips cannot be easily electroplated in a barrel since they are very light and tend to interlock when tumbled with media. 50 ml of clips, comprising approximately 20,000 pieces, were loaded in the spouted bed chamber. This is the minimum load for this size apparatus. The apparatus was conveyed by hand between process tanks and was subjected to the following treatment sequence: 
     
       
         
               
               
               
               
               
             
           
               
                   
                   
               
             
             
               
                   
                 1. 
                 Soak cleaner 
                 5 min 
                   
               
               
                   
                 2. 
                 Cathodic electrocleaner 
                 5 min 
                 6V, 6A 
               
               
                   
                 3. 
                 Water rinse 
                 3 min 
               
               
                   
                 4. 
                 HCl (50%) Activator 
                 5 min 
               
               
                   
                 5. 
                 Water rinse 
                 5 min 
               
               
                   
                 6. 
                 Cyanide dip 
                 3 min 
               
               
                   
                 7. 
                 Copper cyanide plating 
                 5 min 
                 6V, 8A 
               
               
                   
                 8. 
                 Dragout rinse 
                 1 min 
               
               
                   
                 9. 
                 Water rinse 
                 3 min 
               
               
                   
                 10. 
                 Sulfuric acid (5%) 
                 5 min 
               
               
                   
                 11. 
                 Water rinse 
                 3 min 
               
               
                   
                 12. 
                 Sulfamate nickel plating 
                 20 min 
                 6V, 8A 
               
               
                   
                 13. 
                 Water rinse 
                 3 min 
               
               
                   
                 14. 
                 Sulfuric acid (5%) 
                 5 min 
               
               
                   
                 15. 
                 Water rinse 
                 3 min 
               
               
                   
                 16. 
                 Hard Gold Plating 
                 25 min 
                 6V, 6A 
               
               
                   
                 17. 
                 Dragout rinse 
                 3 min 
               
               
                   
                 18. 
                 Water rinse 
                 3 min 
               
               
                   
                 19. 
                 Hot DI water rinse 
                 3 min 
               
               
                   
                   
               
             
          
         
       
     
     A sampling of 10 clips was tested for nickel and gold deposit thickness by x-ray diffraction analysis. An average thickness of 124.9 micro inches of nickel was measured with a standard deviation of 18.0 micro inches. An average thickness of 32.7 micro inches of gold was measured with a standard deviation of 2.1 micro inches. No interlocking of the clips was observed. 
     Example 2 
     3 mm diameter flat sensor disks were electroplated using a portable plating apparatus with a 7.5 inch diameter spouted bed chamber equipped with a draft pipe and particle distribution shield. Disks were also electroplated in a conventional barrel plating apparatus as a means of comparison. The plating sequence given below was used for both trials: 
     
       
         
               
               
               
               
               
             
           
               
                   
                   
               
             
             
               
                   
                 1. 
                 Soak cleaner 
                 5 min 
                   
               
               
                   
                 2. 
                 Cathodic electrocleaner 
                 5 min 
                 6V, 6A 
               
               
                   
                 3. 
                 Water rinse 
                 3 min 
               
               
                   
                 4. 
                 HC1 (50%) Activator 
                 5 min 
               
               
                   
                 5. 
                 Water rinse 
                 5 min 
               
               
                   
                 6. 
                 Cyanide dip 
                 3 min 
               
               
                   
                 7. 
                 Copper cyanide plating 
                 5 min 
                 6V, 8A 
               
               
                   
                 8. 
                 Dragout rinse 
                 1 min 
               
               
                   
                 9. 
                 Water rinse 
                 3 min 
               
               
                   
                 10. 
                 Sulfuric acid (5%) 
                 5 min 
               
               
                   
                 11. 
                 Water rinse 
                 3 min 
               
               
                   
                 12. 
                 Sulfamate nickel plating 
                 20 min 
                 6V, 8A 
               
               
                   
                 13. 
                 Water rinse 
                 3 min 
               
               
                   
                 14. 
                 Sulfuric acid (5%) 
                 5 min 
               
               
                   
                 15. 
                 Water rinse 
                 3 min 
               
               
                   
                 16. 
                 Hard Gold Plating Spout, 
                 222 min, 
                 6V, 5A 
               
               
                   
                   
                 versus Barrel 
                 382 min, 
                 6V, 15A 
               
               
                   
                 17. 
                 Dragout rinse 
                 3 min 
               
               
                   
                 18. 
                 Water rinse 
                 3 min 
               
               
                   
                 19. 
                 Hot DI water rinse 
                 3 min 
               
               
                   
                   
               
             
          
         
       
     
     The disks electroplated in the barrel required the addition of plating media (metal shot) to maintain proper cathodic contacting in the barrel. The volume ratio of media to plated parts was approximately 3 to 1. The parts and plating media were plated in the barrel using gold electrolyte at 6 V and 15 A for 6.36 hours to achieve an average thickness of 222.8 micro inches with a standard deviation of 12.0 micro inches. 
     The disks were plated in the spouted bed plating apparatus at 5A, 6V for 3.7 hours to achieve an average thickness of 220.1 micro inches with a standard deviation of 7.4 micro inches. The spouted bed apparatus not only deposited metal 42% faster than the barrel, but since no media was required, all the gold deposited was on the product parts, not the media. Thus, approximately five times more gold was required to plate the parts in the barrel than to plate the parts in the spouted bed apparatus. 
     Examples of: Electrowinning 
     The present invention is also suitable for electrowinning to recover metal values from process solutions, wastewaters, or mining leachants, and as a method of pollution prevention and wastewater treatment. Presently-employed technologies for treating metal-bearing aqueous waste streams, such as chemical precipitation and ion exchange, do not leave the metal in a form where it can be recycled economically. The need for toxic waste reduction and recycling of usable materials necessitates the development of technologies that will reduce the concentration of dissolved metal in waste streams and allow the recycling of the recovered metals. 
     The performance, cost, and maintenance requirements of conventional electrowinning systems make them economically attractive only for certain limited applications. The present invention is a significant improvement in this technology, as it will lower equipment cost, reduce maintenance requirements and improve performance, thereby making a much wider range of electrolytic recovery applications possible. 
     The operating goals for electrowinning are somewhat different than those for electroplating. In electroplating, the quality and uniformity of the deposit are of paramount concern, with the current efficiency being of secondary importance. In electrowinning, maximizing current efficiency and current density are the primary goals. 
     The present invention may be used for electrowinning by using conductive media as the spouted bed cathode. The media may consist of metal shot, cut wire shot, metallized glass spheres, or graphite or carbon spheres or granules. The use of spherical media is particularly advantageous since very shallow chamber bottom and distribution shield angles (angles A and B in  FIG. 5 ) may be used while maintaining excellent bed movement. When metal shot or metallized glass spheres are used as the bed media, the metal is recovered in a valuable, easily recycled form. 
     In conventional electrowinning, flat electrodes (cathodes and anodes) are immersed in the solution to be treated. A potential is imposed between the electrodes and a direct current is passed through the solution. At the cathode, charged metal ions diffuse to the surface where they receive electrons from the cathode and are reduced to their metallic state. The metal can be present in the solution as a free metal cation or as a complex metal anion, for example, a cyanide complex. It should be noted that the primary mechanism transporting metal ions to the cathode is ordinary Fickian diffusion and is not electrical in nature. 
     At very low current densities, the rate of reduction at the cathode will be proportional to the current density (current per unit area of electrode). At higher current densities, however, the rate of metal reduction is limited by the rate of diffusion of the metal ions to the cathode surface. This puts a practical limit on the current density that can be effectively applied. The limiting current density can be calculated using Fick&#39;s first law for steady state diffusion, and invoking the Nernst assumption of a linear concentration variation in the diffusion layer. The equation for the diffusion-limited current density is:
 
λ L   =−DnFC/d 
 
     Where: 
     λ L —Limiting current density 
     D—Diffusion coefficient of the metal ions 
     n—The charge of the metal ions 
     F—Faraday&#39;s number 
     C—Bulk liquid concentration of metal ions 
     d—Thickness of the Nernst diffusion layer 
     The thickness of the Nernst metal ion depleted layer depends on the extent of agitation in the solution adjacent to the electrode. For a stationary solution, the thickness of the Nernst layer is about 0.05 cm. For an agitated solution, the thickness will be between 0.01 to 0.005 cm. The rate of diffusion of metal ions through the ion depleted layer will be linearly proportional to the concentration gradient in the layer. The metal concentration at the cathode surface can be assumed to be zero, so the concentration gradient will be the bulk metal ion concentration divided by the Nernst layer thickness. These two factors control what the limiting current density will be on a flat cathode. 
     As an example, the limiting current for recovery of silver from a 1000 ppm silver cyanide solution with moderate agitation is approximately 0.6 A/cm. The current efficiency, however, typically falls off at current densities approximately an order of magnitude less than this, because as the metal ion concentration at the cathode decreases, other electrode reactions begin to predominate. To maintain high current efficiencies, therefore, low current densities are required, which restricts the deposition rate. 
     In a cathode which is porous or consists of a packed bed of solid objects, the situation is quite different. The surface area is considerably larger than that of a geometrically equivalent flat electrode, and the current density will vary with the surface features of the cathode. The highest current density will be at the sharp points on the surface, while the lowest current density will be in the recesses. Additionally, the diffusion of ions will no longer take place through a layer of uniform thickness. The increased surface area decreases the current density, thereby increasing the current efficiency. Furthermore, if the average pore radius provided by the objects making up the electrode is smaller than the Nernst layer thickness, and the solution can be replenished in the pores, the diffusion path will be shortened to less than the pore radius, and even higher current efficiencies and current densities can be achieved. 
     Although the above analysis indicates the potential performance improvement that porous or packed bed cathodes offer, the ability of most electrolytes to chemically dissolve back the electrodeposited metal complicates the design of packed bed or porous cathodes Most electrolytes are capable of back dissolution of the constituent metal. Some examples are cadmium cyanide solution, copper etchants, copper nitrate, copper sulfate, and nickel sulfate. The net metal recovered from these types of solutions is the difference between the electrodeposited metal and the metal dissolved back. The rate of back dissolution in acidic solutions, such as sulfates and nitrates, is a function of pH and can be minimized to some extent by pH control during electrolysis. 
     However, the extremely large surface areas of porous or packed bed cathodes in conjunction with strong liquid-solid contacting results in significant back dissolution of metals. This is further complicated by the fact that the vast majority of current transfer from the cathode to the electrolyte is concentrated at the electrode surface closest to the anode with the current being conducted within the packed bed cathode via object to object conduction. Thus, the current density within the cathode bed is very low. These factors result in a net loss of metal from the interior of the bed due to chemical dissolution. This phenomenon significantly impedes the deposition of metal using packed bed cathodes when the projected bed surface area to volume ratio is small, such as with the system used by Hadzismajlovic et al. mentioned above. 
     This problem can be ameliorated by using thin or shallow beds as in the  FIG. 5  embodiment of the present invention where the projected area to volume ratios are high. The use of a distribution shield allows the spouted bed diameter to be increased without increasing the liquid flow rate. Furthermore, a conical bottom with a shallow slope may be used, which effectively increases the bed projected surface area without increasing the bed volume. When a spouted bed with a shallow bottom, a draft pipe and a distribution shield is used, the objects move radially inward towards the center of the bed, rather than downward as in a conventional spouted bed. 
     The loading of the parts, particles or other objects can be maintained so that a layer one, two or three objects thick moves inward along the chamber bottom. The liquid-solid contacting is significantly less in this configuration than in conventional spouted beds, since the liquid flows over the moving bed electrode rather than through the bed, as is the case in conventional spouted beds such as the system disclosed by Scott as mentioned above. Additionally, when the bed is shallow, most of the objects receive current from the electrolyte, in contrast to deeper beds where only a small fraction of the objects at the surface of the bed receive current from the electrolyte. These two effects are particularly advantageous for electrolytic recovery of metals from solutions which can chemically dissolve the metal being recovered. 
     The following examples illustrate the use of the spouted bed cathode in electrowinning applications. 
     Example 3 
       FIG. 8  shows the current efficiency as a function of current density for a spouted bed cathode in a spouted bed reactor. The experiments were conducted using a silver cyanide solution containing 34.1 g K(AgCN) 2  and 42.5 g of KCN per gallon. As shown in this figure, the spouted bed cathode comprised either 3 mm diameter spheres or 6 mm diameter spheres, and produced considerably better performance at much higher current densities than a plane electrode without agitation, as well as a plane electrode in a mechanically agitated cell. This means that for the same amount of expended electrical energy, a much greater amount of metal can be removed at a much higher rate. 
     In order to emphasize the considerable increase in recovery rate of the spouted bed cathode, the data in  FIG. 8  are replotted in  FIG. 9  as the rate of silver recovery from the silver cyanide solution per unit area of cathode material vs. the current density, in order to compare the 3 mm spheres in the spouted bed with the plane electrode exposed to the agitated solution. The rate of metal recovery is calculated by multiplying the current efficiency by the current density and the electrochemical equivalent for silver (4.024 g/A-hr). As shown, the spouted bed recovered metal as much as a factor of six times faster than the plane electrode. 
     Example 4 
     Copper was recovered front copper sulfate solution at pH 1.9 in a spouted bed reactor using a cathode comprising 500 ml of 2 mm diameter metallized glass spheres. One experiment was conducted at 7.5 amperes in a 7.5 inch diameter chamber equipped with a draft pipe and a particle deflector, but no distribution shield. The second experiment was conducted with a 12″ diameter chamber equipped with a draft pipe, a particle deflector and a distribution shield.  FIG. 10  shows that the 7.5″ chamber resulted in almost no reduction in copper concentration while the 12″ chamber rapidly recovered copper. This is due to the reduction in back etching when a shallow spouted bed with a distribution shield is used instead of a deeper spouted bed without the shield. 
     Persons skilled in the art, upon learning of the present disclosure, will recognize that various modifications to the components and elements of the invention are possible without significantly affecting their functions. For example, the specific vessel structure described above may be varied widely in accordance with spouted bed technology, and may have shapes other than cylindrical, such as four sidewalls defining a rectangular chamber and either a single rectangular bottom wall inclined downwardly to the vessel inlet or opposing rectangular bottom walls converging downwardly toward the vessel inlet. 
     Similarly, the positions of the anode and cathode may be reversed so that metal objects may be polished by having an outer layer removed electrolytically. Furthermore, the apparatus disclosed may be used with a gaseous fluid in combination with a chemical coating composition in order to coat recirculating objects with the chemical composition instead of a metal, thereby providing a spouted bed coating apparatus of the type represented in general by that disclosed in U.S. Pat. No. 5,254,168 issued Oct. 19, 1993, to Littman, et al., the entire contents of this patent being incorporated herein by reference. Accordingly, while the preferred embodiments have been shown and described in detail by way of example, further modifications and embodiments are possible without departing from the scope of the invention as defined by the claims set forth below.