Abstract:
An electrochemical cell for use within a system and process for removing contaminants from water and wastewater, where the water or wastewater is transported through several stations for purification and is ultimately transformed into purified water that can be safely discharged to the environment. The electrochemical cell includes a housing, a removable cartridge and oppositely charged electrical headers, the removable cartridge having conductive plates that are in electrical communication with the electrical headers, such that successive conductive plates are oppositely charged.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS  
       [0001]    This application is a continuation of application Ser. No. 10/038,220, filed Jan. 3, 2002, now U.S. Pat. No. 6,495,048, which is a continuation of application Ser. No. 09/494,219, filed Jan. 28, 2000, now U.S. Pat. No. 6,346,197. 
     
    
     
       FIELD OF THE INVENTION  
         [0002]    The present invention relates generally to the field of water and wastewater treatment systems, and more particularly to systems utilizing an electrochemical cell to facilitate flocculation of particles in the water or wastewater to permit the discharge of treated wastewater to the environment or purification of potable water.  
         BACKGROUND OF THE INVENTION  
         [0003]    Contamination occurring in aqueous-based solutions has become a serious concern to society. In particular, problems associated with the disposal of industrial wastewater have been mounting. Disposing of the wastewater is not only very expensive and time consuming, but also extremely harmful to the environment. Some areas of concern in the disposal of wastewater, which are particularly suited to treatment using the subject system, are:  
           [0004]    a. Removal of emulsified oils, both petroleum hydrocarbons and food base oils.  
           [0005]    b. Partially dissolved contaminants which add to turbidity and color of water.  
           [0006]    c. Negatively charged metals such as arsenic, molybdenum, and chromium.  
           [0007]    d. Positively charged heavy metals such as copper, cadmium, nickel, lead, and zinc.  
           [0008]    e. Contaminants such as ammonia, mercury, arsenic and iron which react with oxygen.  
           [0009]    f. Contaminants which react with aluminum or iron such as chlorinated organics.  
           [0010]    g. Poorly settling TSS (total suspended solids) such as silt, ink, wood extractives, clay and microorganisms.  
           [0011]    One example of a particular contaminant of concern is petroleum hydrocarbon contaminants in shipyard wastewater, including the oily wastewater resulting from cleaning out ship bilges and fuel tanks. The primary concern with this wastewater is finding an effective method for its disposal. While various methods have been developed to deal with this oily waste, none have been entirely successful given the extremely varied nature and content of the contaminants in the water, with oil content ranging anywhere from 0.5% to 50% in volume. Included among the methods attempting to control these waste streams are a wide variety of chemical and physical procedures.  
           [0012]    Chemical procedures have attempted to cause a predetermined reaction between chemical additives and impurities contained within the waste stream. The most common reactions are designed to cause the impurities and the chemical additives to coagulate, wherein the particles increase in size and then separate by either floating on or settling below the treated water. The most popular chemical utilized is alum, which when added to the wastewater, separates much of the waste out of the water. There are several problems with chemical coagulation in general, including the generation of very large quantities of residuals that need to be disposed of and imprecision because the amount of chemical necessary for a given volume must always be estimated due to the varying nature of the waste streams.  
           [0013]    Physical procedures are designed to achieve similar results as chemical additive procedures, but to a lesser degree of purity in the final aqueous solution. Filters, centrifuges, plate separators, and clarifiers are the most common physical procedures employed to remove contaminants from aqueous solutions. In most cases, the impurities that are removed physically are suspended solids or poorly emulsified contaminants.  
           [0014]    While the chemical and physical procedures of treating waste streams were thought to be adequate at one time, the results of disposal of solutions treated in this manner have been disastrous. Oceans, streams, lakes and underground wells have all fallen victim to the contamination resulting from the impurities that were not removed by these methods. In fact, because of the dumping of contaminated solutions, many rivers and streams are considered waste sites and entire lakes have been drained so that the lakebeds can be hauled away to be treated as hazardous waste. The main problem is that regardless of whether chemical procedures, physical procedures, or a combination of the two are utilized, the content of impurities in the wastewater remains in an unacceptable range.  
           [0015]    While it was known that the purification of waste streams, and in particular the coagulation of contaminants without the addition of chemicals, could be accomplished through electrolytic treatment in a process called electrocoagulation, the wide range of contaminants, varying contaminant concentrations and large and variable volumes of wastewater in the industrial waste streams generally discouraged its use. However, patents directed to electrolytic treatment apparatuses, methods and systems can be found dating back to the early part of this century. Electrocoagulation is the process of de-stabilizing suspended, emulsified or dissolved contaminants in an aqueous medium by introducing an electrical current into the medium. Electrocoagulation generally takes place inside a substantially sealed treatment chamber, where the impurities are coagulated out of the aqueous medium.  
           [0016]    Many other systems and cells have been disclosed and patented, each trying to convert contaminated water to purified water by separating the contaminants from the water. Unfortunately, none of these systems have been able to solve the problems of variability, number and concentration of contaminants associated with the treatment of industrial wastewater. These previous systems created large quantities of metal sludge and other contaminant sludge that added to the cost of disposal. Even systems that were able to overcome these problems had other problems such as high labor cost (batch and dump methods); large areas necessary for increased residence time, and high capital costs due to electrical power and maintenance (on-line electrical systems); and low efficiency (dilution with non-conductive materials). Other systems suffered from design problems such as not accounting for the production of generated gases or the build up of impurities onto the working electrodes, or creating an electrolytic cell that is too complex and which cannot be easily maintained.  
           [0017]    Accordingly, there is a need for a wastewater treatment system and process that removes contaminants, such as petroleum hydrocarbons, resulting in a product with impurities of considerably less than 15 parts per million (PPM), that is cost effective, energy conscious, easy to use and easy to maintain.  
         BRIEF SUMMARY OF THE INVENTION  
         [0018]    The present invention is directed to a treatment for water and wastewater and a process for removal of contaminants by utilizing chemical, mechanical, and electrolytic devices.  
           [0019]    It is an object of this invention to provide a treatment system and process of removal that removes impurities from water and wastewater.  
           [0020]    It is also an object of this invention to provide a treatment system and process of removal of contaminants from wastewater that is cost effective and energy efficient.  
           [0021]    It is a further object of this invention to provide a treatment system and process of removal of contaminants from water and wastewater that is easy to use and easy to maintain.  
           [0022]    In general, the subject invention has potential application to treat water and wastewater rather than using chemical methods such as inorganic cationic coagulants including the salts of aluminum (aluminum sulfate or “alum”, aluminum chloride, or poly aluminum chloride), iron (chlorides or sulfates), or calcium (chlorides or sulfates). In addition, sediments may be removed in the preparation of potable water. The subject invention may also be used as an aid to clarify water following biological treatment of wastewater.  
           [0023]    A more complete understanding of the waste water treatment system and process for the removal of contaminants will be afforded to those skilled in the art, as well as a realization of additional advantages and objects thereof, by a consideration of the following detailed description of the preferred embodiments. Reference will be made to the appended sheets of drawings, which will first be described briefly.  
       
    
    
     BRIEF DESCRIPTION OF THE DRAWINGS  
       [0024]    [0024]FIG. 1 is flow chart of the wastewater treatment process of the present invention.  
         [0025]    [0025]FIG. 2 is a side cross-sectional view of the electrochemical cell of the present invention.  
         [0026]    [0026]FIG. 3 is an end sectional view of the electrochemical cell of FIG. 2.  
     
    
     DETAILED DESCRIPTION OF THE INVENTION  
       [0027]    The following detailed description illustrates the invention by way of example, not by way of limitation of the principles of the invention. This description will clearly enable one skilled in the art to make and use the invention, and describes several embodiments, adaptations, variations, alternatives and uses of the invention, including what we presently believe is the best mode of carrying out the invention.  
         [0028]    The present invention satisfies the need for a water and wastewater treatment and contaminant removal process that is efficient and effective to purify water or to produce disposable water from industrial wastewater. This is accomplished by using a novel system and process of contaminant removal that includes an electrochemical cell for the coagulation of organic and inorganic materials.  
         [0029]    Referring now to the drawings, in which like reference numbers represent similar or idendical structures throughout, FIG. I illustrates the wastewater treatment process through the use of simple flow diagram. The wastewater, containing varying amounts of contaminants, is fed into a strainer  11  in step  10  to remove larger debris. In this embodiment, which is exemplary of the system and process of the present invention, the contaminants consist primarily of petroleum hydrocarbons that are found, for example, in shipyard wastewater, including “bilge water.” Other contaminants include larger debris that can be separated out initially through the use of strainer  11 . Following the initial straining, the wastewater stream, free of the larger sized debris, is sent to a classifier  13  in step  20 .  
         [0030]    The classifier  13  is a large tank with an inlet located in an intermediate area of the tank that receives the wastewater stream from the strainer  11 . The wastewater stream is pumped into the classifier  13  by means of a pump  302 . A pump  304  is used to remove the wastewater from the classifier  13  and is located such that wastewater is pumped from the top region of the classifier  13 . This causes flow of the wastewater from the classifier inlet upwardly to the top region of the classifier  13  where it is pumped out. Heavier particles in the incoming wastewater stream settle downwardly in the classifier by force of gravity to come to rest at the bottom of the classifier  13 . An auger extends into the bottom of the classifier  13  to direct the heavy solids into a disposal container  15 . When the auger is activated, the solids at the bottom of classifier  13  are moved upwardly and out of the auger into the disposal container  15  in step  24 . The solids in the container  15  may be removed to a suitable solids disposal site such as a landfill.  
         [0031]    The overlying liquid in the classifier  13  is pumped to a solid-liquid hydrocyclone  17  in step  22  by pump  304 . The coarse solids that have not sunk to the bottom and that have entered the hydrocyclone  17  with the overlying liquid are returned to the classifier  13  for further separation, while the wastewater stream is sent to feed tanks  19  in step  30 . The number and capacity of feed tanks  19  used in the system is dependent on the amount of wastewater stream throughput. When more than one feed tank  19  is necessary, they are aligned in a parallel configuration. Once in the feed tanks  19 , the free oil in the wastewater rises to the top in the first decant to be removed by a surface skimmer. The free oil from the skimmer then flows by gravity to the free oil storage tank  21  in step  32  where it undergoes a second decant. The oil is pumped from the top of the free oil storage tank  21  in step  34  and is re-used for various applications. The wastewater underneath the oil (underflow) in the free oil storage tank  21  is returned to the classifier  13  in step  36 .  
         [0032]    The wastewater in the feed tanks  19 , underneath the oil remaining after the first decant, is transported by pump  306  through an in-line basket strainer  61  to an electrochemical cell  200  in step  40 . The wastewater is pumped to the bottom inlet  210  (FIG. 2) of the electrochemical cell  200 , which will be described in more detail in reference to FIGS. 2 and 3, below. Inside the electrochemical cell  200 , the wastewater is passed over electrically charged plates arranged to create a serpentine path for the wastewater. In a process of coagulation, the negatively charged contaminants in the wastewater form clusters or “flocs” with the positively charged ions being released by the charged plates. The clusters join with other clusters to form larger flocs that are easier to remove. In addition, the electrocoagulation process causes hydrolysis of the wastewater, releasing hydrogen gas and oxygen gas into the wastewater and forming hydroxyl ions. The oxygen acts to oxidize contaminants and the hydroxyl ions act to precipitate metals out of the wastewater. This process of electrocoagulation will be described in more detail below. The treated wastewater and gases exit from the top outlet  220  (FIG. 2) of the electrochemical cell  200  and are sent toward an in-line static mixer  23  in step  50 . A portion of the wastewater that enters cell  200  is re-circulated through the electrochemical cell  200  in step  42  by pump  308  at a rate sufficient to provide turbulent mixing and scouring of the plates in cell  200 . In the preferred embodiment and as an example only, with a flow rate of 10 gallons per minute to cell  200 , a re-circulation flow rate of about 50 gallons per minute to 100 gallons per minute is acceptable.  
         [0033]    After exiting outlet  220 , the wastewater is injected with compressed air in step  52  and anionic polymer in step  54 . The mixture is then introduced into the in-line static mixer  23 , which mixes the polymer and air with the wastewater stream. Because the mixer is a static mixer and because compressed air (or other suitable gas) is used, the amount of mechanical sheer on the polymer and coagulated solids from cell  200  is limited, minimizing the breakup of the polymer and flocs. At the same time, the use of a static mixer with compressed air in the wastewater stream provides significant enhancement of the mixing of polymer with the wastewater stream. This enables the use of much lower amounts of polymer in the system generally, while still providing significant coagulation and separation of solids from the wastewater stream. The compressed air mixed into the wastewater stream by the in-line static mixer  23  facilitates the contact of polymer with the coagulated solids and creates flocs containing entrained gases. This results in easier separation of the flocs from the wastewater in the flotation cell  27 . The negatively charged polymer combining with the positively charged flocs make larger diameter flocs with lower overall densities, since larger sized flocs are more effective at accumulating gas bubbles on their surfaces and in their void spaces. As a result, the overall densities of the floes are lower than the density of the wastewater, causing a portion of the flocs to rise to the surface and float. Later, when the gas bubbles escape from the floc, the overall density increases beyond that of the wastewater and a portion of the floes sink.  
         [0034]    The polymer and air can optionally be added to the wastewater stream before the electrochemical cell  200 . In that case, the introduction of air promotes turbulence in the cell which promotes contact of the contaminants with the plates, thereby enhancing coagulation, and the introduction of anionic polymer acts to scavenge positively charged contaminants, forming embryonic flocs, also enhancing coagulation in the electrochemical cell  200 . The addition of polymer and compressed air prior to the electrochemical cell  200  is useful as well where it is desired to remove positively charged ions from the wastewater. This procedure is described in more detail below with respect to an alternative embodiment of the present invention.  
         [0035]    The mixture of polymer, wastewater and air leaving the in-line static mixer  23  flows past a vertical pipe  25  in step  60 . The vertical pipe  25  allows the majority of gases to vent in step  62  so that the rise of flocculated particles in the flotation cell  27  is not disrupted by excessive turbulence due to escaping gases. After passing vertical pipe  25 , the wastewater flows into a flotation cell  27  in step  70 . In the flotation cell  27 , the entrained gases associated with the coagulated solids still remaining in the wastewater result in a decreased density of the flocs, which is less than that of the wastewater, causing the floes to rise to the surface of the wastewater in the flotation cell  27 . The floating floes flow over an overflow weir into a solids collection tank  29  in step  72 . The solids in the solids collection tank  29  are pumped to a filter press  31  in step  74  by pump  310 . The filter press  31  removes the water from the solids and returns the filtrate to the classifier  13  in step  78 . The solids are removed from the filter press  31  after a pressure drop indicates that it is full. The solids are stored in a disposal container  38  in step  76  and may be removed to a suitable solids disposal site such as a landfill.  
         [0036]    The underflow of the flotation cell  27 , which is substantially free of flocs, flows by gravity to a settling tank  33  in step  80 . In the settling tank  33 , further separation of the coagulated solids can occur through gravity as the solids remaining in the underflow will generally have a density greater than the wastewater and will sink to the bottom. These solids are pumped to the filter press  31  in step  92  along with the flocs from the solids collection tank  29 . The water, now substantially free of solids, leaves the settling tank  33  over an overflow weir where it enters into a polymeric filter feed tank  35  in step  90 . This water is pumped to a plurality of in-line bag filters  37  in step  100  by pump  312 , and finally to a polymeric filter  39  in step  110  where most of the residual contaminants are removed. This final discharge of water with substantially reduced contaminants is released into the ground or sewer in step  120 .  
         [0037]    The primary advantage this process enjoys over chemical systems is a significantly lower quantity of residuals for disposal, at lower cost and with better operational simplicity. The primary advantage of this process over physical systems is greatly improved contaminant removal from the wastewater. The only contaminants that require disposal are the concentrated solids in the disposal containers.  
         [0038]    Referring now to FIGS. 2 and 3, the electrochemical cell  200  is illustrated. In FIG. 2, a cross-sectional view of the electrochemical cell  200  is shown as it would be viewed from the front of the device. The cell  200  is equipped with conductive plates  250  and  255  that are alternatingly connected to oppositely charged electrodes as will be explained in more detail in reference to FIG. 3 below. The plates  250  and  255  are evenly numbered so that there are an equal amount of anode and cathode conductive plates. In order to provide easy replacement of the plates  250  and  255 , they are installed into the cell  200  in cartridge  257 . The cell housing  205  has a removable cover  204  to allow the interchanging of the cartridges  257 . Further, the plates  250  and  255  are large in area and few in number, which permits lower pressure and voltage drops. The plates  250  and  255  are made of aluminum in the preferred embodiment but may be composed of any one of a number of materials based on the type of contaminants that are to be removed. For example, iron, platinum, carbon or titanium plates could be utilized. The plates  250  and  255  are separated by spacers  230  that are fabricated from non-conductive material such as nylon to maintain a plate spacing that in the preferred embodiment is approximately 0.5 inches. To achieve a seal at the end of the cartridge  257  and thus create a serpentine flow path, electrically insulated end plates  207  and  208  are used. The end plates  207  and  208  are held in compression against the cartridge  257  by mechanical means. The plates  250  and  255  are arranged in a manner that creates a serpentine flow path for the wastewater. This is done by leaving a gap between plates  250  and the end plate  207  on one end of the cartridge  257  and between plates  255  and the end plate  208  on the opposite end of the cartridge  257 . The wastewater enters at the bottom inlet  210  and is pumped through the cell  200  to the top outlet  220 . As the wastewater winds its way through the cell  200 , the electric field that is generated when a voltage is applied to the plates  250  and  255  causes the dissolved and suspended solids within the wastewater to coagulate and form larger flocs. At the same time, gas bubbles are generated by the electrolysis of wastewater, causing the larger flocs to float. This entire process is referred to as electrocoagulation.  
         [0039]    The most commonly used electrode plates are iron or aluminum because they give trivalent ions; most other cheap and easily accessible metals give only bivalent ions. Trivalent ions have a higher ability than bivalent ions to absorb onto particles in the wastewater because they have a higher charge density. In the preferred embodiment of the present invention, aluminum electrode plates are used.  
         [0040]    The effectiveness of the release of the metal ions into the wastewater is crucial to the coagulation of the solids and to the capability of the process in removing impurities. The release of metal ions is dependent on several factors, including the amount of current sent through the conductive plates, the residence time that the wastewater is in contact with the plates, and the level of turbulence created by the flow of wastewater through the system. In addition, the release of metal ions must be balanced with the injection of polymer, with the goal being to run the lowest possible current but still release sufficient levels of metal ions to initiate coagulation of the contaminants in the wastewater. If the current is set a level that is too high, excessive metal ions are released, thereby increasing the consumption of the plates. When the consumption of the plates is increased, additional polymer is required to coagulate the excess metal ions, which increases the density of the flocs. Thus, it is important to find a current that is high enough to release the metal ions from the plates, but low enough to maintain an acceptable floc density.  
         [0041]    The key parameters in designing and operating the cell, are plate surface area, wastewater flow rate and current. With a cell having approximately 20 square meters of total plate surface area and with a flow rate of 50 liters per minute, we have found that a suitable current is in the range of 300 to 450 amperes. While the cell  200  has been operated using current less than 300 amperes and current exceeding 450 amperes, the preferred range has produced the desired results. Prior systems have had difficulty perfecting the residence time/turbulence conditions, that is, being able to increase turbulence while maintaining adequate residence time of the wastewater within the electrochemical cell. The present invention has solved this problem by introducing a re-circulation stream at step  42  back into the bottom of the electrochemical cell  200  which, in the preferred embodiment, re-introduces approximately 2 to 10 times the throughput rate of 10 gallons/minute. The re-circulation stream creates high turbulence in the cell  200 , scouring the conductive plates  250  and  255  so that the contact of wastewater with the plate surface is increased. This can be further enhanced, if required, by introducing compressed air into the wastewater stream before it enters the cell  200 .  
         [0042]    The electrochemical cell  200  is constructed using stainless steel that is internally vulcanized so that it is not conductive. Alternatively, rubber lined carbon steel or other materials or composites that provide structural strength without conducting electricity could also be used. Wedges  242  are placed on both ends of the cell  200  in area  240 , providing a seal at the ends of the plates to avoid bypassing of wastewater flow. The cell  200  also contains a removable cover  204  to permit access to the inside of the cell and for cartridge replacement as explained above. The cover  204  is electrically insulated from the cartridge ( 250 ,  255  and  230 ) by a non-conductive gasket  206  and from the electrical headers  260  and  270  by a non-conductive fitting  209  that also provides a water tight seal.  
         [0043]    The cell  200  is also unique in its ability to manage the gas build-up associated with the process. By directing the flow of wastewater from the bottom  210  of the cell  200  to the top  220 , as opposed to prior art, which directs the flow from side to side, there is no gas build-up and thus, no pockets of gas created to disrupt the process. The upward serpentine flow coupled with an outlet at the top of the cell allows gas to exit the cell without creating problems. Several benefits are realized by removing accumulated gases, including even plate consumption, turbulent mixing, consistent gas flow, low voltage requirements, and prevention of plate overheating.  
         [0044]    [0044]FIG. 3 illustrates a partial side view of each of the electrical headers. In FIG. 3A, a first electrical header  260  is shown. The bottom or first plate  250  is welded onto the first header  260  by weld  280 , as is every odd numbered plate (counting from the bottom,  3 ,  5 ,  7 , etc.). The second plate  255  is electrically insulated from the header with insulation  290 , as is every even numbered plate ( 2 ,  4 ,  6 , etc.). In FIG. 3B, a second electrical header  270  is shown with the plate attachment reversed from the first electrical header  260 . Thus, the first (bottom) plate  250  is electrically insulated from header  270  by insulation  290 , while the second plate  255  is welded on to header  270  with weld  280 . This configuration permits adjacent oppositely charged plates in parallel alignment to promote superior coagulation in the cell  200 . The current sent to each header  260  and  270  is alternated in timed intervals to avoid the build-up of contaminants at either the anode or cathode. In the preferred embodiment, the polarity is alternated typically between 1 and 10 minutes.  
         [0045]    The process utilizing the electrochemical cell  200  is ideally suited for removal of negatively charged suspended solids, including oils, clays, silt, chlorinated organics, bacteria, microorganisms and metals such as arsenic, molybdenum or chromium which are coprecipitated.  
         [0046]    An alternative embodiment of the present invention is for water purification for potable water. Water purification for potable water would not require the steps prior to treatment in the electrochemical cell  200 . The rest of the process and apparatus of this embodiment is the same as that described above with respect to the first embodiment.  
         [0047]    The process described is also ideally suited for removal of positively charges suspended solids such as heavy metals, including copper, cadmium, nickel and zinc. This can be particularly useful, for example, in removing these contaminants from wastewater effluent of mining operations. In that case, and exemplary of an alternate embodiment of the present invention, polymer is injected into the wastewater prior to the wastewater entering the electrochemical cell  200 , accompanying the addition of polymer into the wastewater after exiting the cell  200 . This embodiment is depicted in FIG. 1 in dotted outline. The wastewater leaving strainer  61  is injected with an anionic polymer at step  63  and compressed air at step  65  in the same manner as described above with respect to steps  52  and  54 . The order in which the compressed air and polymer are injected does not affect the operation of the process in any significant manner. The wastewater with the injected polymer and compressed air is then passed through an in-line static mixer  67 , which may be identical to the in-line static mixer  23 . The negatively charged polymer is attracted to the positively charged metals, forming negatively charged floes with the metal ions. The mixture leaving the mixer  67  is then pumped into inlet  210  (FIG. 2) by pump  306  as previously described. Once in the electrochemical cell  200 , the negatively charged floes containing the metal ions are attracted to the positively charged metal ions released from the plates  250  and  255 , forming even larger floes. The negatively charged particles are coagulated in the electrochemical cell  200  as described above with respect to the first embodiment of the present invention, and further coagulation of all the floes occurs upon injection of compressed air at step  52  and of polymer at step  54 . The rest of the process of this embodiment is the same as that described above with respect to the first embodiment.  
         [0048]    Having thus described preferred embodiments of a wastewater treatment system and process for contaminant removal, it will be apparent by those skilled in the art how certain advantages of the present invention have been achieved. It should also be appreciated that various modifications, adaptations, and alternative embodiments thereof may be made within the scope and spirit of the present invention. For example, the treatment of industrial wastewater has been illustrated, but it should be apparent that the inventive concepts described above would be equally applicable to an endless array of applications including ground water clean-up, storm water treatment, sewage treatment, preparation of potable water, mineral processing and mining water treatment. Moreover, the words used in this specification to describe the invention and its various embodiments are to be understood not only in the sense of their commonly defined meanings, but to include by special definition in this specification structure, material or acts beyond the scope of the commonly defined meanings. Thus, if an element can be understood in the context of this specification as including more than one meaning, then its use in a claim must be understood as being generic to all possible meanings supported by the specification and by the word itself. The definitions of the words or elements of the following claims are, therefore, defined in this specification to include not only the combination of elements which are literally set forth, but all equivalent structure, material or acts for performing substantially the same function in substantially the same way to obtain substantially the same result. The described embodiments are to be considered illustrative rather than restrictive. The invention is further defined by the following claims.