Abstract:
Methods and apparatus for complex treatment of contaminated liquids are provided, by which contaminants are extracted from the liquid. The substances to be extracted may be metallic, non-metallic, organic, inorganic, dissolved, or in suspension. The treatment apparatus includes at least one mechanical filter used to filter the liquid solution, a separator device used to remove organic impurities and oils from the mechanically filtered liquid, and an electroextraction device that removes heavy metals from the separated liquid. After treatment within the treatment apparatus, metal ion concentrations within the liquid may be reduced to their residual values of less than 0.1 milligrams per liter. A Method of complex treatment of a contaminated liquid includes using the separator device to remove inorganic and non-conductive substances prior to electroextraction of metals to maximize the effectiveness of the treatment and provide a reusable liquid.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
       [0001]    The present application claims priority to U.S. Provisional Application No. 60/978,927, filed on Oct. 10, 2007, and U.S. Provisional Application No. 60/978,924, filed on Oct. 10, 2007. The present application is related to PCT Application PCT/U.S.08/075,378, filed on Sep. 5, 2008, and is also related to PCT Application No. ______, filed on ______ (attorney docket 30029-002WO1). The disclosures of said provisional applications and said PCT applications, including the specification, claims and figures, are incorporated herein by reference. 
     
    
     TECHNICAL FIELD 
       [0002]    The current invention relates to the field of complex treatment of liquid media using various technologies. 
       BACKGROUND 
       [0003]    Obtaining clean water from liquids contaminated by discharge of industrial effluents as well as other anthropogenic activities and natural processes is of great social and economic importance. With particular attention to industrial effluents, contaminated liquids are produced as by-products of manufacturing processes in many industries. Such contaminated liquid solutions are typically water solutions that include many different types of contaminants, including substances which may be metallic (including dissolved ions of heavy metals), non-metallic, organic, inorganic, dissolved, or in suspension. 
         [0004]    Conventionally, methods of treatment of liquids, including aqueous solutions containing ions of heavy metals together with organic substances, are based on various types of chemical coagulation techniques with subsequent sedimentation of the impurities, followed by removal and disposal and/or reclamation of sediments. These conventional methods require preparation of the liquids for coagulation, which may include chemical treatment of the liquid. However, such conventional methods sometimes produce a treated liquid which includes residual chemicals, as well as sediments which must be disposed of. 
         [0005]    Reagent treatment is another conventional treatment technique in which chemical reagents are added to the liquid solution for bringing the liquid&#39;s acidity or alkalinity to a level which results in sedimentation of the contaminant. Although still in use at some older industrial plants, this method has major disadvantage and may often provide only low-quality purification. 
         [0006]    Electrochemical processes are also known for use in treatment of contaminated liquids. The concentration of ions of heavy metals in water solutions can substantially influence the choice of electro chemical technology to be used for the treatment and clearing of the contaminated water solutions. Examples of electrochemical processes include electro-coagulation and electroextraction. 
         [0007]    In an electroextraction process, a current is passed from a chemically inert anode through a liquid solution containing one or more metals so that metal is extracted as it is deposited in an electroplating process onto the cathode. Technology exists that allows for electrochemical sedimentation of heavy metals on the cathodes of electrochemical cells using galvanic sedimentation. In this process, additional treatment of the liquid solution is not necessary because the metal is yielded in a solid form. However, this advantage cannot be employed in industry for several important reasons. For example, many electroextraction processes may only be carried out at the starting concentrations of heavy metals exceeding 5 grams per liter. These processes are often incapable of purifying water to a degree permitting its reuse. In addition, the electroextraction process depends on the starting concentrations of mineral oil and common organic substances in water; their presence often diminishes the process speed and efficiency and hinders its use in an automated manufacturing environment. Moreover, the equipment used in this process is often complicated and can require stoppage for performing maintenance and service operations. Furthermore, some special modes of energizing the electrodes of a flow-through electrochemical reactor may result in hetero-coagulation, an effect that boosts the process of coagulation even when several different metals are dissolved in the liquid. 
         [0008]    Electro-coagulation is a more advanced method with a number of applications. In an electro-coagulation process, precipitation of heavy metals (ions) from a liquid solution is achieved by adding ions of opposite charge to the liquid solution via an electrode pair. For example, an anode is dissolved within a flow of liquid to be treated, the anode being formed of a material causing formation of fluxes in the treated liquid. This has the effect of facilitating agglomeration or coagulation of the metals, resulting in separation of the metals from the liquid. However, the shortcomings of an electro-coagulation process often do not allow for its use as an integral part of modern flexible automated production processes. For example, in some cases the electro-coagulation process is very sensitive to the acidity level of the treated liquid. In a liquid with a noticeable acidity or alkalinity, the efficiency of flux formation and of the subsequent coagulation is low. As a result, a pre-adjustment of the liquid&#39;s acidity or alkalinity may be required in order to assure a reliable coagulation. Another considerable drawback is related to the post-treatment of sediments requiring disposal and/or reclamation. Various types of waste resulting from such a treatment may be toxic and require special technologies for their disposal and/or reclamation. At the same time the treated liquids often contain traces of the substances removed in the process of treatment, which usually renders the treated liquids unfit for reuse. 
         [0009]    For the reasons described above, the conventional methods of water treatment may not provide the advantage of permitting wastewater regeneration and its reuse in the manufacturing process. 
         [0010]    Because the contaminated liquids comprise such a broad variation in types of contaminants, a complex treatment of the liquid is required in which one or more treatment techniques are applied in a series of treatment steps to remove contaminants and thereby obtain clean water which can be re-used in industrial, agricultural and technological processes. 
       SUMMARY OF THE INVENTION 
       [0011]    A number of aspects of the current invention are directed to the complex treatment of a contaminated liquid solution by sequential application of treatment technologies. The complex treatment includes performing a preliminary selective separation of non-electrically conductive and nonmetallic substances from a liquid solution, followed by an electrochemical extraction of concentrated electrically-conductive substances from the liquid solution. The complex treatment of the liquid is achieved using apparatus and methods that exclude the use of chemical reagents, while assuring a substantially innocuous treatment by-product. That is, the treatment waste is substantially free of substances that would otherwise require special methods for its disposal and/or reclamation. In addition, the volume of waste and the level of residual substances in the treated liquid are reduced. As a result, a closed cycle of liquid regeneration is achieved. Moreover, when the treatment apparatus and method are used as part of an industrial process, full liquid recirculation within the process is obtained. 
         [0012]    In some aspects, a treatment apparatus for complex treatment of liquids is configured to extract particular substances from a liquid solution. The substances to be extracted may be metallic, non-metallic, organic, inorganic, dissolved, or in suspension. In order to extract matter suspended in the liquid, the treatment apparatus may include at least one mechanical filter used to filter the liquid solution. A separator device is then used to remove organic impurities and oils from the mechanically filtered liquid. Within the separator device, the filtered liquid undergoes flotation, whereby organic impurities, oils, and other non-conductive impurities may be removed from the liquid. The treatment apparatus further includes an electroextraction device. In some examples, the electroextraction device is capable of removing heavy metals from contaminated water solutions containing electrically active components at starting concentrations varying in a range from about 5 grams per liter to a minimum of about 0.01 grams per liter. After treatment within the treatment apparatus, metal ion concentrations within the liquid may be reduced to their residual values of less than 0.1 milligrams per liter. In some examples, complex treatment of contaminated liquids within the treatment apparatus results in a clean liquid adequate for re-use in industrial processes. 
         [0013]    In some aspects, the electroextraction device employs at least one reactor cell which includes a volume-porous electrode pair. The volume-porous electrodes permit three-dimensional flow through the porous electrode body, and provide an extensive and highly reactive surface area, whereby a considerable intensification of the electro-sedimentation process may be achieved as compared to electroextraction employing conventional electrodes. The electroextraction device also provides, concurrent with the metal extraction, a process of reduction and oxidation of toxic components in aqueous solutions, with the metal extraction performed at the cathode, and the decontamination of aqueous solutions performed at the anode. In some examples, these features of the electroextraction device are optimized by forming the volume-porous electrodes of composite material membranes. 
         [0014]    In some aspects, the separator device employs flotation to achieve removal of organic impurities, oils, and other non-conductive impurities from the liquid, without the addition of chemical reagents to the liquid. The separator device includes at least one activator unit disposed within a lower portion thereof configured to receive a supply of compressed gas. The activator unit serves to introduce the compressed gas into the liquid, while violently agitating the gas and liquid together to form a mass of micro-bubbles, which rise upwards. In some examples, in the course of upward movement of the microbubbles, organic and other nonmetallic impurities present in the liquid are captured and suspended, resulting in a foam layer which forms on a surface of the liquid. The foam, which may include one or more of organic impurities, oils, and other non-conductive impurities, is then separated from the liquid. 
         [0015]    In some aspects, a method of treating liquids that include conductive and non-conductive substances includes separating an organic substance and a non-conductive substance from a volume of liquid. The method also includes, subsequent to separating the organic substance and the non-conductive substance from the whole volume of liquid, treating a flow of the liquid by passing the liquid through a volume of electrodes. In some examples, the electrodes are electrically connected to a source of electric potential and are separated by a neutral membrane. 
         [0016]    In some aspects, a method of treating a liquid that includes at least some of conductive substances, non-conductive substances, ions of heavy metals, organic substances, and inorganic substances includes physically treating a flow of the liquid using a filter. The method may also include, subsequent to physically treating the flow of the liquid, dividing the flow of liquid into a first phase and a second phase, the first phase comprising a liquid phase and the second phase comprising a foamy liquid and gas mixture. The method may also include treating a flow of the liquid phase within a permeable volume of electrodes electrically connected to a source of electric potential and separated by a neutral membrane. 
         [0017]    In some aspects, a method of electrochemical regeneration of a liquid includes selectively separating organic substances and inorganic substances from an aqueous solution that includes ions of heavy metals to form a separated aqueous solution. The method may also include, subsequent to separating the organic substances and inorganic substances from the aqueous solution, electrochemically treating the separated aqueous solution by using gravitational force to pass the separated aqueous solution through permeable electrodes separated by a neutral membrane. 
         [0018]    In some aspects, a method of electrochemical regeneration of an aqueous solution that includes ions of heavy metals, organic substances, and inorganic substances, includes selectively separating the organic substances from the aqueous solution in a reagent-free process to form a separated aqueous solution. The method may also include, subsequent to separating the organic substances from the aqueous solution, electrochemically treating the separated aqueous solution by passing, in a laminar mode, the separated aqueous solution through permeable electrodes. In some examples, the permeable electrodes can be formed of a nonmetallic material. In some examples, the electrodes can be disposed sequentially along a path of the aqueous solution movement and separated with a neutral membrane and the electrodes can be connected to a source of electric potential by an elastic permeable nonmetallic woven material. 
         [0019]    In some aspects, a method of electrochemical regeneration of an aqueous solution includes separating organic substances from the aqueous solution by aerodynamic flotation and foaming in a reagent-free process to form a separated aqueous solution. The method may also include, subsequent to separating the organic substances from the aqueous solution, electrochemically treating the separated aqueous solution using electrochemical precipitation of metals onto surfaces of a permeable cathode separated from a permeable anode by a neutral membrane. In some examples, the permeable cathode is electrically connected to a source of electric potential by an elastic permeable nonmetallic woven material. 
         [0020]    In some aspects, a method of electrochemical regeneration of metal-containing aqueous solutions includes performing an aerodynamic treatment of a volume of the aqueous solution using one or more aerodynamic activating devices. The method may also include forming a foam layer from the aqueous solution. The method may also include separating the foam layer from a remaining volume of the aqueous solution. The method may also include supplying of the remaining volume of the aqueous solution to an accumulating reservoir. In some examples, the accumulating reservoir includes at least two vertically installed electrochemical reactors. In some examples, the electrochemical reactors include three-dimensional porous electrodes and having an inlet to an inter-electrode space in the lower part of the reservoir and an outlet from the inter-electrode space in an upper part of the reservoir. The three-dimensional porous electrodes of the electrochemical reactors may be connected with at least two power supply units by an elastic nonmetallic conductive aqueous solution-permeable contact fabric. The method may also include performing electrical precipitation of metals from the aqueous solution. In some examples, performing electrical precipitation includes directing the aqueous solution through the accumulating reservoir, directing the aqueous solution into the inlet to the inter-electrode space, directing the aqueous solution across the anode, directing the aqueous solution through the membrane, directing the aqueous solution across the cathode and directing the aqueous solution out of the outlet from the inter-electrode space. 
         [0021]    In some aspects, an apparatus for electrochemical regeneration of metal-containing aqueous solution of wastewater by selective separation of organic and inorganic components of the aqueous solution and electrical precipitation of metals onto a surface of negatively charged three-dimensional porous electrodes includes an aerodynamic module and an electrochemical module. The apparatus may also include an accumulating reservoir hydraulically interconnecting the aerodynamic module and the electrochemical module. The apparatus may also include a system of sources of electric potential electrically interconnecting aerodynamic module and the electrochemical module. In some examples, the sources of electric potential are electrically connected to each other and to electrodes of the electrochemical module by elastic permeable nonmetallic conductive fabric contacts. 
         [0022]    In some aspects, an apparatus for electrochemical regeneration of aqueous solutions include one or more of ions of heavy metals, organic substances, and inorganic substances is provided. The apparatus may include a mechanism configured to separate organic substances and inorganic substances from the aqueous solution. The apparatus may also include a mechanism configured to electrochemically treat the aqueous solution by pressing the aqueous solution through permeable electrodes separated by a neutral membrane. In some examples, the permeable electrodes are electrically connected to a source of direct electric potential, and the connection to the source of direct electric potential may include an elastic permeable contact fabric. 
         [0023]    In some aspects, an apparatus for electrochemical regeneration of aqueous solutions that include one or more of ions of heavy metals, organic substances, and inorganic substances is provided. The apparatus may include a mechanism configured to separate the organic substances from the aqueous solution in a reagent-free process to form a separated aqueous solution to generate a remaining solution. The apparatus may also include a mechanism configured to perform electrochemical treatment of the remaining solution. The mechanism configured to perform electrochemical treatment of the remaining solution may include a system configured to perform, in a laminar mode, hydraulic pressing of the remaining solution through permeable electrodes formed of a nonmetallic material and located sequentially along the path of the aqueous solution movement. In some embodiments, the anodes and cathodes of the permeable electrodes are separated by permeable neutral membranes and the anodes and cathodes are connected to a source of electric potential. In some embodiments, the connection to the source of electric potential may include an elastic permeable nonmetallic woven material that substantially encloses the permeable electrodes. 
         [0024]    In some aspects, an apparatus for electrochemical regeneration of aqueous solutions that include ions of heavy metals in combination with organic and inorganic substances forming various metal-organic complexes with the ions of heavy metals may include an aerodynamic flotation and foaming module configured to separate organic substances from the aqueous solution in a reagent-free process to generate a remaining solution. The apparatus may also include a mechanism configured to electrochemically treat the remaining solution by electrochemical precipitation of metals onto surfaces of a permeable cathode. In some examples, the permeable cathode is separated from a permeable anode by a neutral membrane and connected to a source of electric potential by a conductive elastic permeable nonmetallic woven material. 
         [0025]    In some aspects, an apparatus for electrochemical regeneration of a metal-containing aqueous solutions includes a mechanism for aerodynamic treatment of a volume of the metal-containing aqueous solution. The apparatus may also include an accumulating reservoir. The mechanism for aerodynamic treatment may include one or more aerodynamic activating devices configured to form a foam layer on the metal-containing aqueous solution, a device configured to separate the foam layer from the remaining volume of the aqueous solution, and a device configured to supply of the remaining volume of the aqueous solution to the accumulating reservoir. The accumulating reservoir may include at least two vertically installed electrochemical reactors. In some examples, the electrochemical reactors include three-dimensional porous electrodes. In some examples, the electrochemical reactors also include an inlet to an inter-electrode space in a lower part of the reservoir. In some examples, the electrochemical reactors also include an outlet from the inter-electrode space in an upper part of the reservoir. In some examples, the electrochemical reactors including at least two power supply units electrically connected to the three-dimensional porous electrodes of the electrochemical reactors by an elastic nonmetallic conductive aqueous solution-permeable contact fabric. The apparatus may also include a device configured to perform electrical precipitation of metals from the aqueous solution. The device configured to perform electrical precipitation of metals may be configured to direct the aqueous solution through the accumulating reservoir, direct the aqueous solution into the inlet to the inter-electrode space, direct the aqueous solution across the anode, direct the aqueous solution through the membrane, direct the aqueous solution across the cathode, and direct the aqueous solution out of the outlet from the inter-electrode space. 
         [0026]    In some aspects, an apparatus for electrochemical regeneration of metal-containing aqueous waste water solutions includes an aerodynamic module and an electrochemical module. The apparatus may also include an accumulating reservoir hydraulically interconnecting the aerodynamic module and the electrochemical module. The apparatus may also include a system of sources of electric potential electrically interconnecting the aerodynamic module and the electrochemical module. In some examples, the sources of electric potential are connected to the electrodes of the electrochemical module by elastic permeable nonmetallic conductive fabric contacts. In the apparatus, an outlet of said aerodynamic module for outputting a treated liquid may be located above the accumulating reservoir and an inlet to the electrochemical module may be located at the same level as a bottom of the accumulating reservoir. 
         [0027]    In some aspects, a method of treating a liquid solution is provided. The method may include separating organic substances and non-conductive substances from the liquid solution; and subsequent to separating organic substances and non-conductive substances from the liquid solution, electrochemically treating the liquid solution such that conductive substances are removed from the liquid solution. 
         [0028]    In some embodiments, electrochemically treating the liquid solution comprises passing the liquid solution through a reactor. In some examples, the reactor includes a pair of volume-porous electrodes separated by a neutral membrane, and the electrodes are electrically connected to a source of electric potential such that one electrode is anodic and the other electrode is cathodic. In some examples, the liquid solution passes through a volume of each respective electrode of the electrode pair, whereby galvanic deposition of conductive substances on an active working surface of the cathodic electrode occurs. 
         [0029]    In some embodiments, separating includes generating violent agitation within the liquid such that a foam comprising the organic substance and the non-conductive substance is formed on a surface of the liquid. In some embodiments, subsequent to electrochemical treatment, the method further comprises outputting a treated liquid that is substantially free of organic substances, non-metallic impurities, and metal ions. In some embodiments, the method is a reagent-free method such that no reagents are added during the method to enhance any of separation and electrochemical treatment. 
         [0030]    In some embodiments, prior to separating an organic substance and a non-conductive substance from the liquid solution, the method further includes directing a stream of the liquid solution through a filter to generate a filtered liquid. In some embodiments, the liquid solution comprises conductive and non-conductive substances. In some embodiments, the liquid solution includes at least some of conductive substances, non-conductive substances, ions of heavy metals, organic substances, and inorganic substances. 
         [0031]    In some aspects, a method of electrochemical regeneration of a liquid is provided. The method includes providing the liquid, the liquid comprising an aqueous solution that includes at least ions of heavy metals, selectively separating organic substances and non-conductive inorganic substances out of the liquid to form a modified solution, and subsequent to separating the organic substances and non-conductive inorganic substances out of the liquid, electrochemically treating the modified solution by using gravitational force to drive the modified solution through a pair of permeable electrodes of opposed charge, the electrodes separated by a neutral membrane. 
         [0032]    In some embodiments, the aqueous solution further includes organic substances and inorganic substances. In some embodiments, the pair of permeable electrodes includes volume-porous electrodes, each electrode comprising a volume configured to permit fluid through-flow in three orthogonal directions. In some embodiments, selectively separating organic substances and non-conductive inorganic substances from an aqueous solution includes generating flotation within the aqueous solution such that the liquid separates into the modified solution and a second solution comprising the organic substances and non-conductive inorganic substances. In some embodiments, selectively separating organic substances and non-conductive inorganic substances from an aqueous solution includes generating flotation within the aqueous solution such that the liquid separates into the modified solution and a second solution comprising the organic substances and non-conductive inorganic substances, wherein the flotation generation is achieved without addition of chemical reagents to the aqueous solution. 
         [0033]    In some aspects, a method of electrochemical regeneration of an aqueous solution is provided. The method includes separating organic substances from the aqueous solution in a reagent-free process by aerodynamic flotation of the aqueous solution to form a foam comprising the separated organic substances, and a separated aqueous solution. Subsequent to separating the organic substances from the aqueous solution, the method includes electrochemically treating the separated aqueous solution to achieve removal of metals from the separated aqueous solution. 
         [0034]    In some embodiments, electrochemically treating the separated aqueous solution includes providing a reactor cell including a permeable cathode separated from a permeable anode by an electrically-neutral membrane, the permeable cathode being electrically connected to a source of negative electric potential by an elastic conductor, and passing the separated aqueous solution through the reactor cell. In some examples, the removal of metals from the separated aqueous solution is achieved through electrochemical deposition of metals onto surfaces of the cathode. 
         [0035]    In some embodiments, the elastic conductor comprises permeable, nonmetallic, woven material. In some embodiments, electrochemically treating the separated aqueous solution comprises providing volume-permeable electrodes disposed sequentially along a path of the aqueous solution movement and separated with an electrically-neutral membrane, each electrode comprising a nonmetallic material and being connected to a source of electric potential by an elastic conductor, and passing the separated aqueous solution through permeable electrodes. In some embodiments, the elastic conductor comprises permeable, nonmetallic, woven material. In some embodiments, the aqueous solution includes wastewater containing ions of heavy metals in combination with organic and inorganic substances forming various metal-organic complexes with the ions of heavy metals. In some embodiments, the aqueous solution includes ions of heavy metals in either ionic or complex form. 
         [0036]    In some aspects, a method of electrochemical regeneration of a metal-containing aqueous solution is provided. The method includes performing a flotation treatment of a volume of the aqueous solution using one or more activating devices configured to aerate and agitate the contents of said volume, forming a foam layer within the volume of the aqueous solution, separating the foam layer from a remaining volume of the aqueous solution and supplying the remaining volume of the aqueous solution to an accumulating reservoir, the accumulating reservoir including at least two vertically installed electrochemical reactors. In some examples, the electrochemical reactors include volume-porous electrode pairs, the volume-porous electrodes permitting liquid permeation through a volume of the electrode in three orthogonal directions, the volume-porous electrodes each connected with a power supply unit by an electrically-conductive contact such that one electrode of an electrode pair is an anode and the other electrode of the electrode pair is a cathode. The reactors may also include an electrically neutral membrane disposed between electrodes of an electrode pair, an inlet to an inter-electrode space in the lower part of the reservoir; and an outlet from the inter-electrode space in an upper part of the reservoir. In the method, electrical separation of metals from the aqueous solution may be performed by the following method steps: Directing the aqueous solution through the accumulating reservoir. Directing the aqueous solution into the inlet to the inter-electrode space. Directing the aqueous solution across the anode. Directing the aqueous solution through the membrane. Directing the aqueous solution across the cathode, and directing the aqueous solution out of the outlet from the inter-electrode space. 
         [0037]    In some embodiments, the foam layer comprises inorganic and non-electrically conducting inorganic substances previously in solution within the metal-containing aqueous solution. In some embodiments, the method is a chemical reagent-free method. In some embodiments, the contact comprises an elastic, nonmetallic, aqueous solution-permeable fabric. In some embodiments, when the aqueous solution is directed across the anode, the metals become positively charged, and when the aqueous solution is subsequently directed across the cathode, the positively charged metals deposit on surfaces of the cathode, whereby metals are separated from the aqueous solution. 
         [0038]    In some aspects, an apparatus for wastewater treatment is provided for wastewater that includes an aqueous solution including metals and metal ions, organic substances, and inorganic substances. The apparatus may include an aeration module configured to provide selective separation of organic and non-electrically conducting inorganic components of the aqueous solution from the aqueous solution. The apparatus may include an electrochemical module, the electrochemical module connected to the aeration module such that wastewater treated within the aeration module is hydraulically driven to the electrochemical module. The apparatus may also include a power supply and a control module which coordinates operation of the aeration module with operation of the electrochemical module. In some examples, the electrochemical module includes at least one pair of volume porous electrodes, the volume-porous electrodes each connected with the power supply by an electrically-conductive contact such that one electrode of an electrode pair is an anode and the other electrode of the electrode pair is a cathode, and the electrochemical module is configured to provide electrical deposition of metals from the wastewater treated within the aeration module such that the metals deposit onto a surface of the cathode. 
         [0039]    The apparatus may include one or more of the following features: The contact comprises an elastic, liquid-permeable, nonmetallic fabric. The control module is configured to provide a pulsed source of electrical power to the electrodes. 
         [0040]    In some aspects, an apparatus for treatment of an aqueous solution is provided. The aqueous solution may include one or more of ions of heavy metals, organic substances, and inorganic substances. The apparatus may include a separation device configured to separate organic substances and inorganic substances from the aqueous solution, and an electrochemical treatment device configured to electrochemically treat the aqueous solution such that conductive substances including ions of heavy metals are removed from the aqueous solution. 
         [0041]    The apparatus may include one or more of the following features: The electrochemical treatment device includes at least one pair of volume porous electrodes separated by a neutral membrane, the volume-porous electrodes each connected with a power supply such that one electrode of an electrode pair is an anode and the other electrode of the electrode pair is a cathode, and the electrochemical treatment device is configured to electrochemically treat the aqueous solution such that electrical deposition of metals occurs on a surface of the cathode. The flow of the aqueous solution through a volume of the volume porous electrodes is achieved by pressing the aqueous solution through the volume, wherein pressing comprises use of gravitational force. The apparatus is configured such that the aqueous solution is delivered to the electrochemical treatment device subsequent to separation in the separation device. 
         [0042]    In some aspects, an apparatus for electrochemical regeneration of an aqueous solution is provided. The aqueous solution includes one or more of ions of heavy metals, organic substances, and inorganic substances. The apparatus may include a separation mechanism configured to separate at least the organic substances from the aqueous solution in a reagent-free process. In some examples, the separation mechanism providing a separated aqueous solution which is organic-substance-free. The apparatus may include a reactor mechanism configured to electrochemically separate at least ions of heavy metals from the separated aqueous solution. The reactor mechanism may include volume-permeable electrodes disposed sequentially along a movement path of the separated aqueous solution. In some examples, the electrodes are separated with an electrically-neutral membrane. In some examples, each electrode includes a nonmetallic material and is connected to a source of electric potential by an elastic conductor. In some examples, the reactor is configured to hydraulically press the separated aqueous solution in a laminar mode through respective volumes of the electrodes. 
         [0043]    The apparatus may include one or more of the following features: The elastic conductor comprises a liquid-permeable, nonmetallic fabric. The elastic conductor comprises a liquid-permeable, nonmetallic fabric that substantially entirely encloses the permeable electrodes. The elastic conductor comprises a viscose fabric saturated, in the course of a multi-stage pyrolysis, with graphite and displaying an absorption ability. 
         [0044]    In some aspects, an apparatus for electrochemical regeneration of an aqueous solution is provided. The aqueous solution may include at least one of metals and metal ions. The apparatus may include an aeration device configured to dynamically aerate a volume of the aqueous solution, an accumulating reservoir, and at least two electrochemical reactors disposed within the accumulating reservoir. The aeration device may include one or more activators which dynamically activate the contents of the volume such that a foam layer is formed in the aqueous solution, a separating portion configured to separate the foam layer from the remaining volume of the aqueous solution; and a supply portion configured to supply the remaining volume of the aqueous solution to the accumulating reservoir. In some examples, the electrochemical reactors each include volume-porous electrodes, an inlet to an inter-electrode space in a lower part of the reservoir, an outlet from the inter-electrode space in an upper part of the reservoir, and at least one power supply unit electrically connected to the electrodes by an elastic contact. In some examples, the electrochemical reactor is configured to direct flow of the remaining volume of the aqueous solution through the inter-electrode space in a substantially vertically direction to generate electrical separation of metals from the remaining volume aqueous solution. 
         [0045]    The apparatus may include one or more of the following features: The volume-porous electrodes include at least one pair of volume-porous electrodes separated by a neutral membrane, and each electrode is connected with the power supply by an electrically-conductive contact such that one electrode of the electrode pair is an anode and the other electrode of the electrode pair is a cathode. The apparatus is configured to direct the aqueous solution through the accumulating reservoir, direct the aqueous solution into the inlet to the inter-electrode space, direct the aqueous solution across the anode, direct the aqueous solution through the membrane, direct the aqueous solution across the cathode permitting electrical deposition of metals and metal ions onto a surface of the cathode; and direct the aqueous solution out of the outlet from the inter-electrode space. The at least one power supply comprises at least two power supplies. The elastic contact comprises a liquid-permeable, nonmetallic fabric. An outlet of the aeration device is located above the accumulating reservoir and an inlet to the electrochemical module is located at the same level as a bottom of the accumulating reservoir. A switching processor is provided that is configured to form electrical current pulses, and to apply the current pulses to the electrodes. 
         [0046]    Modes for carrying out the aspects of the invention are explained below by reference to embodiments of the aspects shown in the attached drawings. The above mentioned aspects of the invention, other aspects, characteristics and advantages will become apparent from the detailed description of the embodiments presented below in conjunction with the attached drawings. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0047]      FIG. 1  is a schematic illustration of an apparatus for complex treatment of liquids. 
           [0048]      FIG. 2A  is a sectional view of a separator. 
           [0049]      FIG. 2B  is a sectional view of a foam generator. 
           [0050]      FIG. 2C  is a sectional view of the foam generator of  FIG. 2B , showing liquid flow paths within the foam generator. 
           [0051]      FIG. 3  is a sectional view of an electrochemical reactor cell. 
           [0052]      FIG. 4  is a sectional view of an embodiment of an electrochemical reactor cell. 
           [0053]      FIG. 5  is an end view of the electrochemical reactor cell of  FIG. 4 . 
           [0054]      FIG. 6  is a first perspective view of the electrochemical reactor cell of  FIG. 4 . 
           [0055]      FIG. 7  is a second perspective view of the electrochemical reactor cell of  FIG. 4 . 
           [0056]      FIG. 8  is a perspective view of an electrically conductive band. 
           [0057]      FIG. 9  is a side sectional view of a reactor module. 
           [0058]      FIG. 10  is a perspective view of the reactor module of  FIG. 8 . 
           [0059]      FIG. 11  is a schematic illustration of the treatment process using the apparatus of  FIG. 1 . 
           [0060]      FIG. 12  is a schematic diagram of the control system of the apparatus for complex treatment of liquids. 
       
    
    
     DESCRIPTION 
       [0061]    An illustrative embodiment of an apparatus  100  for electrochemically processing liquids will now be described with respect to the figures. The apparatus  100  is configured to selectively separate organic and inorganic components of an aqueous solution and perform electrical precipitation of metals onto a developed active surface of negatively charged three-dimensional porous electrodes. Although one illustrative embodiment is described herein, it is understood that the inventive concepts disclosed herein are not limited thereto the illustrated embodiment. Moreover, it should be understood that only structures necessary for clarifying the present invention are described herein. Other conventional structures, and those of ancillary and auxiliary components of the system, are assumed to be known and understood by those skilled in the art. 
         [0062]    Referring to  FIG. 1 , an apparatus  100  for complex treatment of liquid comprises an input reservoir  102  for accumulating and storing a contaminated liquid prior to treatment. The liquid may be in the form of an aqueous solution, and in some aspects can include substances which are metallic (including dissolved ions of heavy metals), non-metallic, organic, inorganic, dissolved, or in suspension. In other aspects, the aqueous solutions can be wastewater. In still other aspects the aqueous solution can be wastewater containing ions of heavy metals in combination with organic and inorganic substances forming various metal-organic complexes with the ions of heavy metals. In still other aspects, the aqueous solution can include ions of heavy metals in either ionic or complex form. 
         [0063]    The apparatus  100  further includes a pump  104 . An inlet of the pump  104  is connected to, and draws liquid from, the internal volume of the reservoir  102 . An outlet of the pump  104  is connected, through a flow rate adjustment valve  106  and a flow meter  108 , with the inlet of a first mechanical filter  110 . 
         [0064]    The first mechanical filter  110  includes a screen configured to remove sediments and other non-dissolved particulate matter from the liquid. The filtering properties (e.g., pore size) of the filter  100  are selected based on the requirements of the specific application. By passing the liquid through the mechanical filter  110 , sediments and other non-dissolved particulate matter are removed from the liquid received from the reservoir  102 . 
         [0065]    Liquid that has been filtered through mechanical filter  110  is directed into a separator device  200  ( FIG. 2A ) which aerates the liquid stream, dividing it into a first portion having a first phase and a second portion having a second phase. 
         [0066]    The separator device  200  comprises a tank formed of an outer cylindrical housing  210  arranged coaxially with an inner cylindrical housing  212 . A bottom surface  240  extends between a lower end  242  of the outer housing  210  and a lower end  246  of the inner housing  212  so that the tank is in the form of an annular trough  250 . The inner housing  212  is arranged so that its open upper end  248  is disposed at a height which is lower than the height of the open upper end  244  of the outer housing  210 . Liquid exiting the mechanical filter  110  is directed into the trough  250  via a liquid inlet  216  formed adjacent to the lower end  242  of the outer housing  210 . 
         [0067]    An annular gas manifold  226  is disposed within a lower portion of the trough  250 , and receives a supply of compressed gas from a gas compressor  232  via a gas inlet  220  formed in the outer housing  210 . In addition, several foam generating units  228  are disposed within a lower portion of trough  250  and are connected to the manifold  226  so as to receive a supply of compressed gas from the manifold  226 . The foam generators  228  serve to generate foam within the annular trough  250  by introducing the compressed gas into the liquid, while violently agitating the gas and liquid together to form a mass of micro-bubbles  238  within the lower end of the trough  250 . 
         [0068]    Referring to  FIGS. 2B and 2C ,  FIG. 2B  shows a cross-sectional view of an exemplary foam generator  228  and  FIG. 2C  shows the flow of liquids and air within the foam generator  228  of  FIG. 2B . 
         [0069]    The foam generator  228  includes a generator housing  262  that receives a stream of compressed gas and transforms a direction of the flow of the compressed gas. The generator housing  262  is connected to a device  266  for input of the gas to the foam generator  228  which is connected to a pipeline (for example, manifold  226 ) allowing the input of gas into the foam generator  228  through the device  266  (as indicated by arrow  290 ). The generator housing  262  of the foam generator  228  forms a cavity  268  having a conical shape that receives the compressed gas from the pipeline  226 . 
         [0070]    A cone  270  is located inside the cavity  268  such that gas passing through the cavity  268  passes over the cone  270 . The cone  270  has a conical shape with a tip pointing toward the end of the cavity  268  where the compressed gas enters from the pipeline  226 . The inclusion of the cone  270  in the cavity  268  decreases the area in which the gas can flow and increases the pressure of the gas. The cone  270  also modifies the direction of the air flow in the foam generator  228  (as indicated by arrow  291 ) and directs the compressed air into a set of longitudinal channels  272  (as indicated by arrow  292 ). 
         [0071]    The longitudinal channels  272  are distributed in regular intervals about the base of cone  270  and divide the stream of the compressed gas into capillary micro-streams of compressed gas. In general, the spacing of the longitudinal channels  272  and the number of longitudinal channels  272  can be based on the size of the foam generator  228 . The longitudinal channels  272  are connected at one end to the cavity  268  near the base of the cone  270  and at the other end to a system of radial channels  276 . 
         [0072]    The radial channels  276  are disposed at an angle from the longitudinal channels  272  such that the compressed gas passing through the longitudinal channels  272  and into the radial channels  276  changes direction (as indicated by arrow  293 ). For example, the radial channels  276  can be disposed at about a ninety degree angle with respect to the longitudinal channels  272 . The change in the direction of the airflow increases the turbulence in the airflow such that the gaseous working agent is dispersed at high speed, creating a local area of low pressure. 
         [0073]    The reflector of a hydraulic part of the generator of foam, corresponding to cone  264  in  FIG. 2B , has two basic functions. The external conical surface of the reflector distributes and allocates a volume of liquid, which is performed in a conical funnel, and distributes and allocates a liquid in such a manner that on the conical surface of a reflector, the liquid flows down in a bottom of a cavity  274  and cuts off a part of a stream of gas that moves in the radial channel  276 . 
         [0074]    The base of the cone  264  has a function of reflecting streams of gas that move in channels  272  and turning the specified streams in the channel formed by the bottom of the generator housing  262  and the base of the cone and forming a certain thickness of the moving stream of gas therein. The distance between a surface of the base of cone  264  and the bottom of generator housing  262  is equal to the diameter of the bubbles of gas that are formed in this channel. For example, the micro-bubbles are formed in this channel. 
         [0075]    The reflector of an aerodynamic part of the generator of foam, corresponding to cone  270  in  FIG. 2B , has a function of transforming a stream of gas in such a manner that a zone with a laminar level is not formed in the center of the stream. The cone  270  forces the gas stream out to the periphery of cavity  268  where the stream has a high level of turbulence, and then the stream is input into regularly dispersed channels  272 , whose design eliminates aerodynamic resistance. 
         [0076]    Due to the high speed of movement of the stream of compressed gas through the system of radial channels  276 , when the compressed gas exits the system of radial channels  276  a local zone of low pressure  278  is formed at the point where the compressed gas exits the system of radial channels  276  (as indicated by arrow  294 ). Because of this low pressure, higher pressure liquid is drawn toward conical reflector  264  and toward low pressure zone  278 . The liquid in a truncated conical cavity  274  is mixed with the air from the system of radial channels  276  in the local zone of low pressure  278 . The liquid is delivered into the local zone of low pressure  278  through the cavity  274  (as indicated by arrow  310 ). The cavity  274  is conical in shape with a decreasing cross-sectional area such that the cavity  274  has a greater diameter at an entrance to the cavity and a smaller diameter near the low pressure zone  278 . The decreasing diameter of the cavity  274  increases the turbulence in the flow of liquid in cavity  274 . A cone  264  is located inside the cavity  274  such that liquid passing through the cavity  274  passes over the cone  264 . The cone  264  has a conical shape with the tip of pointing toward the entrance to the cavity  274 . The conical shape of the cavity  274  and cone  264  increases turbulence in the liquid due to the increased contact of the liquid with its surfaces. 
         [0077]    The mixture of gas and liquid generates a pseudo-boiling volume in the low pressure zone  278  of the foam generator  228 . The liquid and gas mixture flows away from the low pressure zone  278  and into an area with a larger diameter. The pressure in the liquid and air mixture increases as the pseudo-boiling volume flows away from the low pressure zone  278  forming a foam of micro-bubbles  238  of the liquid that exit the foam generator  228  and rise to the surface of the foam generator  228  (as indicated by arrow  296 ). As the microbubbles  238  are displaced from the low pressure zone  278 , some of the bubbles of gas start to burst and turn to finer bubbles. Thus, foam leaves the area of the hydrodynamic conical reflector  264  and the liquid from the burst bubbles goes towards the jets of the gaseous working agent (rather than rising to a surface of the liquid in the cavity). This recycling of some of the liquid from burst bubbles creates additional turbulent flow and increased foam. 
         [0078]    Due to their buoyancy, the micro-bubbles  238  rise upwards. In the course of the upward movement of the micro-bubbles  238 , impurities present in the liquid adhere to the surfaces of the micro-bubbles  238 , and are captured within the foam, and thus are suspended in a resulting foam layer  236  which accumulates on the surface of the liquid. Captured impurities may include one or more of organic matter, oil, heavy metals, minerals and oxides. 
         [0079]    In this configuration, the foam  236  which accumulates on the surface of the liquid, and which contains captured impurities, is discharged over the upper end  248  of the inner housing  212  and is drawn down through the interior cavity  214  of the inner housing  212  by force of gravity. The foam  236  is directed to a storage tank  234  via a conduit  224 . As a result, the organic and other nonmetallic impurities are separated from the liquid without addition of chemical reagents to the liquid solution. 
         [0080]    The outer housing  210  further includes a liquid outlet  218  formed in the outer housing  210  at a height that is just below the height of the upper end  248  of the inner housing  212 . While the foam is discharged over the upper end of the inner housing  212 , the liquid, which risen to the upper portions of the trough  250  along with the micro-bubbles  238 , has been substantially cleared of impurities, and exits the outer housing  210  via the liquid outlet  218 . 
         [0081]    The liquid outlet  218  of the outer housing  210  communicates with, and directs liquid into an electrochemical reactor module  300  ( FIG. 3 ). In some embodiments, the separator device  200  and the electrochemical reactor module  300  may be relatively arranged so that the liquid outlet  218  of the separator device  300  is located above the electrochemical reactor module  300  so that liquid flows under the force of gravity into the electrochemical reactor module  300 . It is understood, however, that in alternative relative arrangements of the separator device  200  and the electrochemical reactor module  300 , an external driving force may be used to direct liquids from the liquid outlet  218  to the electrochemical reactor module. 
         [0082]    The electrochemical reactor module  300  includes module housing  301 , which is discussed further below. A plurality of electrochemical reactor cells  313  are included in the module housing  301 . In general, the electrochemical reactor cells  313  ( FIG. 3 ) provide electrolytic extraction of metals from a liquid solution. As seen in  FIGS. 3-7 , the electroextraction cell  313  includes a cell housing  314 . The cell housing  314  includes closed sidewalls  314   a  and a bottom  314   b  configured to form a container having an open upper end. The cell housing  314  is illustrated as having a vertically-elongated rectangular shape, but it is well within the scope of the invention to employ alternative shapes such as cylindrical or trapezoidal. The cell housing  314  is formed of a dielectric material. For example, the cell housing  314  may be formed of a chemically-inert plastic, such as, but not limited to, polypropylene. 
         [0083]    The cell housing  314  is segmented into two symmetric wells  326 ,  327  each having a separate well volume, using an electrically neutral membrane  328 . Membrane  328  serves to electrically isolate liquids within the two wells  326 ,  327 , effectively separating the electrical charge provided in the first well  326  from an electrical charge provided in the second well  327 . Membrane  328  is a rigid, porous plate formed of a electrically neutral and chemically non-reactive fabric, the fabric being formed of materials such as, but not limited to, polypropylene or polyamide. In some embodiments, the membrane  328  is formed of a filtering fabric that includes polypropylene strings. The edges of the membrane  328  are fixed to the cell housing  314 . In some embodiments, the edges of the membrane  328  are received in grooves  315  formed in the inner surface of the ell housing  314 , whereby the position of the membrane  328  within the cell housing  314  is maintained ( FIG. 3 ). In other embodiments, the edges of the membrane  328  are secured between parallel rails  325  provided on an interior surface of the housing  314  for that purpose ( FIG. 4 ). 
         [0084]    In the symmetric electrochemical reactor cell  313 , the membrane  328  is positioned within the housing  314  so as to provide a first well  326  which has substantially the same working volume as the second well  327 . The membrane  328  may be provided having a thickness in a range from about 0.2 mm to about 1 mm (for example, from about 0.2 mm to about 0.4 mm, from about 0.3 mm to about 0.5 mm, from about 0.6 mm to 0.9 mm, and from 0.8 mm to 1.0 mm). In some aspects, the membrane  328  is formed having a maximum thickness of less than about 0.5 mm. The membrane  328  provides a region of reduced flow volume between the electrodes, creating an active zone having a small volume relative to the corresponding volume without a membrane  328 . The effect of the region of reduced flow volume is to accelerate fluid flow from the first well  326  to the second well  327 . 
         [0085]    An inlet opening  320  is formed in the sidewall of the housing  314  adjacent to the bottom of the cell housing  314 . The inlet opening  320  permits input of a liquid requiring treatment and processing into the internal cavity of the cell housing  314 . Specifically, the inlet opening  320  permits fluid flow into the first well  326 . In addition, an outlet opening  321  is formed in the sidewall adjacent to an upper edge of the housing  314 . After treatment and processing of the liquid, the outlet opening  321  permits output of the liquid from the well  327 . Specifically, the outlet opening  321  permits fluid flow to the exterior of the cell  313 . As seen in  FIGS. 5-7 , the inlet opening  102  and outlet opening  103  are provided having a width that extends substantially across a width of the respective housing side so as to maximize fluid flow into and out of the housing  314 . 
         [0086]    A first electrode  322  is disposed within the first well  326 , and a second electrode  324  is disposed within the second well  327 . During processing of the contaminated liquid, the first electrode  322  is connected with a source of positive electric potential, and the second electrode  324  is connected with a source of negative electrical potential, provided, for example, by one or more power supply units  316 . In some embodiments, the power supply units  316  are interconnected by means of an electrical circuit such that sources of electric potential can be connected to the respective electrodes  322 ,  324  and their respective conductive bands  330  by a switching processor  160  ( FIG. 12 ). The switching processor  160  is configured to form electrical current pulses and apply the pulses in a predetermined order to the electrodes  322 ,  324  and their respective conductive bands  330 . 
         [0087]    The first and second electrodes  322 ,  324  are formed to be substantially structurally similar. For this reason, only the structure of the first electrode  322  will be described herein. 
         [0088]    The first electrode  322  is made of a carbon carbon composite material, graphitic cotton wool, graphitic carbon wool, coal carbon wool or from coal cotton wool. For example, in some embodiments, the first electrode  322  is formed of coal carbon wool, which is an electrically conductive fabric that is chemically inert, flexible, can withstand very high temperatures, and can be formed into a desired shape. The coal carbon wool is pressed into plates, each plate having a thickness of approximately 5-8 mm. Each plate is folded back on itself one or more times, and one or more folded plates are stacked to obtain a volume of material which is approximately the size of the first well  326 . Thus, the electrode  324  is sized and shaped to fit within, and substantially fill, an interior space of the first well  326  such that the active working volume of the first electrode  322  generally corresponds to the volume of the first well  326 . The volume of the first electrode  322  is determined by the requirements of the specific application, and is based on requirements for the productivity of the electroextraction cell  313 . As an example, for a cell  313  in which a flow rate of up to three cubic meters per hour is required, a corresponding electrode  322  would have a volume measured in cubic centimeters. Of course, requirements of greater flow rates can be accommodated by electrodes having volumes measured in cubic meters. 
         [0089]    At one end of the first electrode  322 , the stacked plates of coal carbon wool are bent and compacted into a substantially rectangular compressed region  340 . The end of the first electrode  322  is bent in a direction away from the corresponding end of the second electrode  324 , whereby inadvertent contact of the electrodes  322 ,  324  is avoided, and overall height of the electrochemical cell  313  is reduced. In some embodiments, compressed region  340  has an alternative shape, such as cylindrical. In some embodiments, the compressed region  340  may surrounded by a correspondingly-shaped metal plug  342 , which in turn is connected to a source of positive electric potential  201 . Compression of the electrode material in the compressed region  340  promotes efficient transfer of electrical charge from the plug  342  to the electrode material. 
         [0090]    The above described electrode configuration provides a porous electrode of a predetermined working volume, the working volume defined by the dimensions of the volume of the carbon-carbon wool material disposed within the first well  326 . It is understood that, due to the large surface area inherent to the carbon carbon wool fabric, and because the fabric permits liquid to pass through the entire working volume of the electrode, a very large active working surface area is provided within the working volume. In addition, the electrode configuration permits liquid to pass through the working volume in three orthogonal directions. 
         [0091]    The first electrode  322  is bound by an elastic conductive band  330 , and another elastic conductive band  330  surrounds the second electrode  324 . The conductive band  330  made of a carbon composite fabric created by a multi-step pyrolysis process in which a viscose fabric matrix is saturated with carbon (graphite). The resulting band structure is non-metallic, electrically conductive, porous, elastic, absorptive, and flexible. The band  330  is wrapped about the electrode in a stretched configuration so that it remains in place due to the elastic properties of the band  330  and so that good electrical contact is made between the band  330  and first electrode  322 . The conductive band  330  surrounds at least a portion of the outer periphery of the first electrode  322 . In some embodiments, the band  330  is in the form of a strip that extends about a circumference of the electrode. 
         [0092]    For example, the conductive band  330  may be formed in a U-shape ( FIG. 8 ), including a closed lower end  330   c  joining opposed first  330   a  and second  330   b  band sides. The electrode  322  may be press fit between the opposed band sides  330   a ,  330   b  such that a lower end of the electrode abuts against the inner surface  330   d  of the lower end  330   c  of the conductive band  330 . The upper portion of the opposed first and second sides may be bent to correspond to the bent shape of the electrode  322 , and may also include connectors  330   f  for connecting to an external source of electric power. In other aspects, the conductive band  330  may be provided in other shapes such that the outer peripheral surfaces of the first electrode  322  may be essentially enclosed by the conductive band  330 . In addition, the conductive band  330  is directly connected to a source of positive electric potential. The ends of the conductive band  330  are provided with vertically aligned holes  330   f , and an electrical conductor from a power source passes through the upper hole  330   f , through the electrode  322 , and through the corresponding lower hole  330   f.    
         [0093]    The first electrode  322  is disposed within the first well  326  so as to be interposed between the membrane  328  and the sidewall  314   a . In some embodiments, a rigid plate  346  may optionally be used to maintain a desired geometric shape of the first electrode  322 . As seen in  FIG. 3 , a rigid plate  346  is disposed between the sidewall  314   a  and conductive band-covered side of the first electrode  322 . 
         [0094]    The first electrode  322  serves as an anode due to its connection with a source of positive electric potential through metal plug  342  which acts in the compressed region  340 , and through the conductive band  330 , which acts along the entire outer periphery of the first electrode  322 . This configuration provides an electrode in which the charge density over the electrode  322  is highly controllable and substantially uniform throughout its volume. 
         [0095]    In a similar manner, the second electrode  324  is disposed within the second well  327 . The second electrode  324  is formed to have a volume of material which is approximately the size of the second well  327 . The second electrode  324  is bound by a conductive band  330 , which is connected with a source of negative electric potential through a metal plug  340 . As a result, the second electrode  324  serves as a cathode. 
         [0096]    In summary, the cell  313  for electrolytic extraction of metals from metallic liquids includes a housing  314  segmented into at least two generally symmetric wells  326 ,  237  separated by an electrically neutral, porous membrane  328 , an electrode  322 ,  324  disposed within each well, at least one source of constant electric potential connected to the electrodes, and a covering  330  on the external surface of the electrodes, the covering  330  providing a porous, elastic, nonmetallic woven contact for connection to a source of constant electric potential. The electrolytic cell  313  further includes an input  320  for inputting of a metal-contaminated liquid into the volume of the first electrode  322 , which is connected to a source of positive electric potential, and an output  321  for outputting the processed liquid from the volume of the second electrode  324 , which is connected to a source of negative electric potential. 
         [0097]    The following tables provides examples of technical parameters of the illustrated embodiment of the electrolytic cell  313 : 
         [0000]    
       
         
               
               
             
           
               
                   
               
             
             
               
                 DC current load per one electrochemical 
                 150 A 
               
               
                 reactor 
               
               
                 Voltage 
                 6 to 12 V 
               
               
                 Number of anode chambers 
                 1 
               
               
                 Number of cathode chambers 
                 1 
               
               
                 Maximum amount of metal precipitated at 
                 8 kg 
               
               
                 the electrochemical reactor&#39;s cathode 
               
               
                 Percentage of metal extraction 
                 99.5% 
               
               
                 Production capacity 
                 0.3 cubic meters per hour 
               
               
                   
               
             
          
         
       
     
         [0098]    Due to the high rate of the liquid exchange at the volume-porous electrodes&#39; active surface which corresponds to the extensive surfaces provided within the volume of the electrodes, it is possible to raise the effective current density by a factor of 10 relative to that of conventional electrochemical reactors with planar electrodes, resulting in a 100-fold increase in the production capacity of the cell, and in the metal extraction speed. 
         [0099]    Of a special importance is the design of electrodes  322 ,  324 , particularly the pioneering design of elastic conductive bands  330  manufactured of a composite viscose based fabric pyrolytically saturated with carbon. The conductive bands  330  are is completely chemically inert, and assure electrical connection over substantially the whole electrode surface, which reduces the current loss, and avoids the destruction which occurs when conventional metallic contacts are used within an electrochemical reactor. 
         [0100]    Referring again to  FIG. 3 , operation of an individual cell  313  will now be described in detail. In operation, the liquid to be treated and processed is forced to enter inlet opening  320 . The liquid may be driven using conventional techniques, which may include using the influence of forces of gravitation, and/or pumping. In the preferred embodiment, the housing  314  is disposed within an module housing  301  filled with the liquid to be treated, whereby the head of liquid above the inlet opening  320  generates the required driving force. 
         [0101]    The stream  360  of the liquid to be processed, enters the first well  326  in a laminar mode and moves inside the working volume of the first electrode  322  by passing through porous contact  330 . At this time, the working volume of the first electrode  322  is under the influence of positive electric potential, owing to the connection of contact  330  and metal plug  342  to the source of positive electric potential, provided by a power supply  316 . Under gravitational force, the liquid rises upwards in the working volume of electrode  322 , and under influence of the same forces, filters through the membrane  328  into the second well  327 . Within the second well  327 , the liquid passes through conductive band  330  into the internal working volume of the second electrode  324 , which is connected to a source of negative electric potential, provided by the power supply  316 . Metal ions, being positively charged due to passage through the working volume of the positively charged first electrode  322 , are attracted to the surfaces of the negatively charged second electrode  324 , and thus are extracted from the liquid. After being processed through the working volume of the second electrode  324 , the treated, substantially metal-free liquid leaves in stream  362  through the output opening  321 . 
         [0102]    In this embodiment, since the working volume of the respective electrodes  322 ,  324  is substantially the same as the volume of the corresponding well  326 ,  327 , the distance between electrodes is determined only by the thickness of the membrane  328 . As a result, this distance is only a maximum of about 0.8 to 1.0 mm, and may be as little as 0.2 mm, whereby the efficiency of the galvanic pair is very high. 
         [0103]    Moreover, the entire volume has an active galvanic function. Specifically, from the moment of input of a liquid into the working volume of the second electrode  324 , which is connected to a source of negative electric potential, a high-speed process of electro-sedimentation of the metals begins. 
         [0104]    The volumetric structure of the electrodes  322 ,  324 , which are made from carbon fibers, results in a significantly large active working surface area within the respective electrodes  322 ,  324 . This large active working surface area is provided with a source of uniform, constant electric potential. In some aspects, at least about 50% of the active working volume of the one or more electrodes of the electrode cell is provided with this uniform, constant source of electric potential, and as much as about 99% or more of the active working volume of the one or more electrodes of the electrode cell may be provided with the uniform, constant source of electric potential. This is turn results in a significant gain of the electro-sedimentation of metals is achieved on the surface of the carbon fibers from an increased current density in the electrode relative to conventional electrodes. 
         [0105]    The electroextraction cell  313  can also include a sensor  370  located on an external surface of the housing  314  in the vicinity of the cathode  324 . The thickness of a cathode metal sedimentation is determined by a means of the sensor  370 , which may be a magnetic resonance sensor. In use, the cathode metal can be configured such that for a specific definition of the thickness of the cathode metal the electrical resistance of the cathode is changed, and the change in resistance is determined by the sensor  370 . 
         [0106]    As described above, metal ions are attracted to the surfaces of the negatively charged second electrode (cathode)  324 , and thus are extracted from the liquid. The metal is deposited within the cathode&#39;s  324  volume. After the internal volume of the cathode  324  is filled with metal, the cathode may be removed from the cell  313  and a new cathode  324  may be installed and the process can be repeated. Metal can be subsequently be removed from the electrode  324  as an ingot using pyrometallurgic, electrochemical or chemical methods processes. 
         [0107]    Module Including Plural Symmetric Electrode Cells 
         [0108]    A plurality of electrochemical reactor cells  313  can be arranged together within the module housing  301  of the electrochemical reactor module  300  in order to achieve improved process throughput. Referring now to  FIGS. 9 and 10 , the module housing  301  is formed of a pair of concentric hollow cylinders joined at their respective lower ends to form an annular trough. 
         [0109]    A bottom surface  304  closes the lower side of the module housing  301 , and extends between a lower end of the external cylinder wall  310  and a lower end of the internal cylinder wall  312 . The height of the external cylinder wall  310  is greater than height of the housing  314  of the electrochemical reactor cells  313 , and the height of the internal cylinder wall  312  is less than the height of the housing  314  of the electrochemical reactor cells  313 . In particular, an upper edge of the internal cylinder wall  312  terminates at a height that is below that of the outlet opening  321 . As seen in  FIGS. 9 and 10 , in which the power supply  316 , the electrodes  322 ,  324 , and membrane  328  for each electrochemical reactor cell  313  are omitted for purposes of clarity, when electrochemical reactor cells  313  are disposed within the module housing  301 , the radial distance d 1  between the internal cylinder wall  312  and the external cylinder wall  310  is greater than the corresponding dimension d 2  of the trough in the radial direction. In addition, the electrode cells are arranged within the trough so that a cavity  334  is provided between the external cylinder wall  310  and the confronting surface of the housing  314  of each electrochemical reactor cell  313 . 
         [0110]    The cavity  334  between the electrochemical reactor cell  313  and the external cylinder wall  310  is filled with liquid delivered from the separator  200 , that is, liquid containing metals in solution. The level of the liquid in the module housing  301  is sufficient to create internal pressure forces acting under the influence of gravity (head) that press the liquid into the inlet openings of the respective cells  313 . In addition, a sensor  352  is provided to determine the level of liquid in the module housing  301 , and the level of the liquid in the module housing  301  is regulated to an upper limit which is less than the height of the housing  314  of each electrochemical reactor cell  313 . 
         [0111]    Under the influence of gravity, the liquid is forced to enter inlet opening  320  of the electrochemical reactor cell  313 , passes through the volume of the anodic electrode  322 , the membrane  328 , and the volume of the cathodic electrode  324 , to effect the removal of metal ions from the liquid. A processed liquid L out , that is, a liquid that is substantially without metals in solution, exits outlet opening  321  of the cell  313 . The housing  314  of the cell  313  is arranged to abut the internal cylinder wall  312  of the module housing  301  such that the outlet opening  321  faces radially inward. As a result, the liquid exiting from the outlet opening  321  is directed into the open internal space  318  within the internal cylinder wall  312 , which provides an outlet for the module housing  301 . 
         [0112]    Referring again to  FIG. 1 , the outlet  318  of the module housing  301  is connected with a pump  112 , whereby liquid is drawn from the electrochemical reactor module  300  and directed through a flow rate adjustment valve  114  and a flow meter  116 , to an inlet of a second mechanical filter  118 . 
         [0113]    The second mechanical filter  118  includes a screen configured to remove sediments and other non-dissolved particulate matter from the liquid. The filtering properties (e.g., pore size) of the filter  100  are selected based on the requirements of the specific application. In some embodiments, the filtering properties of the second mechanical filter  118  are more restrictive than that those of filter  110 . By passing the liquid through the mechanical filter  118 , fine sediments and other remaining non-dissolved particulate matter are removed from the liquid received from the electrochemical reactor module  300 . 
         [0114]    Liquid that has been filtered through the second mechanical filter  118  is then directed into a reservoir  120  intended for collecting the treated liquid. 
         [0115]    Although not specifically described herein, the apparatus  100  is equipped with various sensors at appropriate locations to detect the characteristics of the liquid, which may include, but are not limited to, electrical conductivity, density, acidity, alkalinity, flow rates, temperature, and viscosity. In addition, the apparatus  100  is equipped with sensors to detect the operation and status of the pumps  204 ,  112 , filters  110 ,  118 , separator  200 , electrochemical reactor module  300 , and other conventional ancillary and auxiliary components of the system. The apparatus  100  is also equipped with a controller  150  which controls operation of the pumps  204 ,  112 , filters  110 ,  118 , separator  200 , electrochemical reactor module  300 , and the other conventional ancillary and auxiliary components of the system based on sensor input ( FIG. 7 ). 
         [0116]    The process of complex treatment of liquids is now described with reference to  FIG. 11 . Input ducts  130  are provided which supply the contaminated liquid solution to the input reservoir  102 . Contaminated liquid, for example waste from technological processes, is accumulated within the input reservoir  101  until the level of liquid therein achieves a predetermined level as detected by a sensor  152 . When the level of liquid within the input reservoir  102  reaches the predetermined level, the pump  104  commences operation and drives the liquid to the first mechanical filter  110  along the line comprising the adjustment valve  106  and the flow meter  108 . 
         [0117]    The first mechanical filter  110  filters sediments and other non-dissolved particulate from the liquid. 
         [0118]    From the mechanical filter  110 , the filtered liquid is supplied to the separator device  200 , which separates the organic substances and non-metallic impurities from the liquid. Within the separator  200 , the liquid enters the annular gap between the outer cylindrical housing  210  and the inner cylindrical housing  212 . The level of the liquid within the separator trough  250  gradually rises up to a level sensor  252  that issues a signal for turning on the compressor  232 , which supplies compressed air to the activator units  228  that operate to form local areas of micro-bubbles  238 , so that the layer  236  of steady foam is formed within a short period of time. The speed of the liquid rise is so calculated that the liquid undergoes a flotation treatment over a period of about 40 minutes, which is sufficient for the separation organic and other nonmetallic impurities from the main volume of liquid. The foam  236  rises up to the upper part of the coaxial separator device  200 , flows into the internal cavity  214  of the inner cylindrical housing  212 , and is then stored. 
         [0119]    The liquid separated from the foamed impurities is supplied to the cavity  334  formed within the electrochemical reactor module  300 . The level of liquid within the cavity  334  is permitted to rise to a predetermined level  350 , as detected by a sensor  352 . At the same time, in accordance with the law of communicating vessels, the liquid enters the input opening  320 . Concurrent with the liquid&#39;s rising within the annular trough  334 , its level also rises in each of the electrochemical reactors  313  up to the level of the output openings  321 . In the course of the rise, electrical current is applied to the electrodes  322 ,  324  from the power supply units  316 , so that the stream of liquid passing through the reactor housing  314  is electrochemically treated. Specifically, an electrolytic process is performed which results in galvanic deposition of metals on the active working surface of the cathodic electrode  324  within each electrochemical reactor cell  313 . The liquid that has undergone the electrolytic treatment flows from outlet opening  321  of the cell  313 , and is directed into the open internal space  318  within the internal cylinder wall  312 . The liquid is then driven by the pump  112  along the conduit which includes the adjustment valve  114 , the flow meter  116 , to the second mechanical filter  118 . 
         [0120]    The second mechanical filter  118  filters sediments and other non-dissolved particulate from the liquid. 
         [0121]    From the second mechanical filter  118 , the filtered liquid is supplied to the collecting reservoir  120 . Liquid accumulated within the collecting reservoir is substantially free of organic and inorganic substances including metal ions. Thus, the liquid is directed, via ducts  140 , to external systems and processes where it is reused. 
         [0122]    A selected illustrative embodiment of the invention has been described above in some detail. It should be understood that only structures considered necessary for clarifying the present invention have been described herein. Other conventional structures, and those of ancillary and auxiliary components of the system, are assumed to be known and understood by those skilled in the art. Moreover, while a working example of the present invention has been described above, the present invention is not limited to the working example described above, but various design alterations may be carried out without departing from the present invention as set forth in the claims. Other combinations of treatment devices including separator devices and electrochemical reactor modules, as well as alternative embodiments of foam generators and/or electrochemical reactors, as described in PCT/U.S.08/075,378 and PCT/______ ((attorney docket 30029-002WO1), are contemplated and may be employed.