Patent Publication Number: US-2016221842-A1

Title: System for separating contaminants from fluids

Description:
RELATED APPLICATIONS 
     This patent application claims the benefit of earlier filed U.S. Provisional Patent Application No. 61/881,366 filed on Sep. 23, 2013 and titled SYSTEM FOR REMOVING CONTAMINANTS FROM WATER. The entire contents of earlier filed U.S. Provisional Application No. 61/881,366 is expressly incorporated herein, in its entirety, by this reference. 
    
    
     BACKGROUND OF INVENTION 
     1. Technical Field 
     The present invention relates generally to filtration systems for separating and removing contaminants from fluids. 
     2. Background Art 
     Fluid is defined as a continuous, amorphous substance where molecules move freely past one another and that has the tendency to assume the shape of its container. Many substances are fluids including but not limited to water. For purposes of this patent disclosure the fluid is described as being water but it is to be expressly understood the fluids described herein are not limited to water. Water at the molecular level is formed of two Hydrogen (H) atoms bonded to one Oxygen (O) atom. The chemical formula for water is H 2 O. Water is one of the most abundant substances on Earth and is essential for animal life and plant life. Most life and particularly animal life requires water that is free from contaminants and more particularly free from harmful contaminants. There are a variety of known processes for separating contaminants from water, and such processes may be as simple as a screen filter and as complex as reverse osmosis. Generally it is the type of contaminant that is to be removed from the water, and the subsequent use of the water that dictates the complexity of the process used to remove the contaminants. For example, if human consumption (potable water) is the desired end product, the system/process must remove all harmful contaminants and such systems can be both complex and expensive. Conversely, if the desired end product is water suitable for industrial purposes, the system may not need to be so complex, robust and expensive. 
     One industrial process that produces large volumes of contaminated fluid as a byproduct is induced hydraulic fracturing. Induced hydraulic fracturing or hydro-fracturing, sometimes termed “fracking”, is a technique in which water is mixed with sand and chemicals, and the mixture is injected at high-pressure into a well bore to create small fractures (typically less than 1 mm), along which desirable fluids including gas, petroleum and hydrocarbons may migrate to the well for collection and harvesting. 
     The hydraulic fractures are created by pumping fracturing fluid into the well bore at a rate sufficient to increase down-hole pressure above the fracture gradient (pressure gradient) of the rock. The rock cracks and the fracturing fluid continues propagating into the rock, extending the crack still further. Introducing a proppant, such as grains of sand, ceramic, or other particulates into the fracturing fluid prevents the fractures from closing upon themselves when the pressure of the fluid is removed. 
     During the fracturing process, some amount of fracturing fluid is lost through “leak-off” when the fracturing fluid permeates into the surrounding rock. If not adequately controlled, fracturing fluid leak off can exceed 70% of the injected volume. The portion of the fracturing fluid that is not lost through “leak off” returns to the surface through the well and is called “waste water”, “flow back water” or “produced water”. The waste water may be heavily contaminated. 
     Hydraulic fracturing equipment usually consists of a slurry blender and one or more high-pressure high-volume fracturing pumps, a monitoring unit and associated equipment including, but not limited to, fracturing fluid tanks, units for the storage and handling of proppant, a variety of testing, metering and flow rate equipment and storage tanks and/or ponds for contaminated waste water. Typically, fracturing equipment operates in high-pressure ranges up to approximately 15,000 psi and at volume rates of approximately 9.4 ft. 3  per second. This is approximately 100 barrels fluid per minute at 42 gallons per barrel. (4200 gallons per minute). 
     The fracturing fluid injected into the well is typically a slurry of water, proppants, poly-coagulants and chemical additives comprising approximately 90% water, approximately 9.5% sand and approximately 0.5% chemical additives. A typical fracturing fluid composition, many of which are proprietary and considered industrial trade secrets, uses between three (3) and twelve (12) chemical additives which may include: acids, sodium chloride, poly acrylamide, ethylene glycol, sodium carbonate, potassium carbonate, flutaraldehyde, guar gum, citric acid and isopropanol. Some portion of the additives maybe charged particulates and/or ionic molecules. 
     A typical fracturing process requires between approximately two million and five million gallons of water per well. Approximately 10%-40% of the fracturing fluid pumped into the well returns to the surface as wastewater and commonly contains a variety of contaminants including, but not limited to, hydrocarbons, carbon dioxide, hydrogen sulphide, nitrogen, helium, iron, manganese, mercury, arsenic, lead, particulates, chemicals and salts as well as the chemical additives added to the fracturing fluid before injection into the well. Wastewater production commonly averages between approximately 3,000 barrels and 5,000 barrels per day at 42 gallons per barrel. (126,000-210,000 gallons). 
     The wastewater flowing back to the surface and exiting the well bore is collected and pumped into wastewater storage tanks or into wastewater ponds that are lined with plastic or the like to prevent the wastewater from leaching into the ground. After the fracking operation is complete, the wastewater storage tanks and/or wastewater storage ponds are drained and the wastewater therein is transported to salt water dumps (SWDs) or hazardous waste sites for permanent disposal. 
     Beginning in 2015, a United States Government Environmental Protection Agency (EPA) regulation will require a “paper-trail” that documents when and where all hydraulic fracturing wastewater originates and where the wastewater is taken for disposal. These new regulations create additional expenses and increase future potential liabilities of drillers and fracking operators. 
     In the Marcellus Shale deposit of North Dakota USA, it is estimated to cost more than approximately $3 per barrel (42 gallons/158.98 liters) to dispose the wastewater and approximately $7 to $10/per barrel (42 gallons/158.98 liters) to transport wastewater to an approved disposal site. There is also a cost for sweet water (fresh water) needed for conducting the hydraulic fracturing operation. In arid and semi-arid areas fresh water is an additional cost factor. For example the hydraulic fracturing of a horizontal well may use approximately 4.2 million gallons (15.89 million liters) of fresh water which must be purchased and available for the fracking operation. 
     Fresh water sourcing is becoming a revenue business as some municipalities and landowners in the Western United States are selling water rights to the petroleum drilling industry for hydraulic fracturing. 
     For example, Texas has small amounts of available fresh water but has the geography to properly dispose of contaminated wastewater. Pennsylvania, on the other hand, has abundant supplies of fresh water but has no place to dispose of wastewater. In the Northeast United States, disposal of wastewater is problematic and as a result wastewater disposal has moved generally West toward Ohio and Indiana and Virginia where the wastewater is being dumped into pits. It is estimated in the near future, wastewater “dumpers” may have to pay as much as approximately $5,000 to $6,000 per truckload in disposal site charges not including the cost of transporting the waste water to the dump site. 
     There are four primary methods for dealing with hydraulic fracturing wastewater. A first method reuses the untreated wastewater in the hydraulic fracturing process. Unfortunately, reuse is problematic as high levels of contaminants tend to plug the well with “residual chemicals”, particulates, or shale fines” which may negatively impact production of the well. 
     A second method is “deep well injection,” which entails drilling a deep disposal well into which the wastewater is pumped for permanent disposal. Deep well injection is problematic as seismologists and the scientific community have alleged earthquakes “were almost certainly induced by the disposal of fracking wastewater in deep disposal wells.” The drilling of a disposal well is also expensive and such disposal increases the volume of fresh water required for fracturing operations as the wastewater is not re-used. 
     A third method is on-site treatment of the wastewater which removes the most harmful chemicals and contaminants from the wastewater. Some portion of the treated water may then be reused in the fracturing. On-site treatment generally has negligible transportation costs, but with known systems and known technology is more expensive than other options due to the high maintenance costs of know systems and the need to repeatedly shut the system down for cleaning and backwashing. Further, such known systems and technology operate under high pressures typically exceeding 250 psi, are readily known for being easily damaged and even destroyed by small amounts of hydrocarbons that may accidentally pass through the system to filter membranes. Such filter membranes have a limited amount of membrane surface area available for filtration, are expensive, and difficult to replace. Further, membrane replacement is a time consuming process during which the system must be shut down. 
     The fourth method is off-site treatment and disposal of the wastewater. Similar to deep well injection, off site treatment and disposal increases the volume of fresh water required for fracturing operations as the wastewater is not reused or recycled. This fourth option is the most expensive as transportation costs and disposal costs may be enormous. 
     One industry estimate places the cost of treating wastewater, including costs for equipment, operation, labor, chemicals, and sludge handling, at up to approximately $20 per barrel. Because hydraulic fracturing may produce upwards of 3,000-5,000 barrels (126,000-210,000 gallons, or 476,961-794,936 liters) of wastewater per well, per day, this cost may be as high as $60,000-$100,000 per day. 
     The huge volume of fresh water necessary for fracturing operations, many of which occur in arid and semiarid areas, is another significant cost that must be recouped. Any ability to reuse or recycle wastewater can offset some portion of the cost. Water, be it the acquisition of fresh water, the handling of the wastewater, and the ultimate disposal of the wastewater is a significant and burdensome cost that is necessarily borne in the cost of the well. Further, because the wastewater may be so contaminated with pollutants, chemicals, salts and the like, the wastewater may be characterized as “hazardous waste” that must be inventoried, tracked, and handled with extreme care prior to, during and after disposal. Further, disposal of “hazardous waste” leads to more hazardous waste sites that permanently damage the environment. 
     Any means by which wastewater may be filtered or otherwise treated to remove contaminants and allow reuse and/or recycling of the water, or disposal of the water in sites other than “hazardous waste sites” or “saltwater dumps” will reduce the cost of bringing wells into production and will reduce the hazardous byproducts and environmental impacts of hydraulic fracturing operations. 
     The instant invention resolves various of these known problems by providing a mobile truck mounted system comprising a combination of known and new filtration and separator technology and salt removal technology for wastewater generated as a byproduct of hydraulic fracturing operations, wastewater from industrial processes and wastewater from agricultural operations, including, but not limited to feed lots. 
     The instant invention allows the wastewater to be recycled for re-use by separating and removing contaminants in a series of steps which provides savings by reducing the need for fresh water and reducing costs of transportation to and from fresh water sources, reducing the need to transport wastewater to dump sites, reduction in dump fees and by reducing the amount of wastewater that requires governmental regulated disposal. 
     The removal of contaminants, including but not limited to solids, oils, BTEX compounds, diesel, benzene, toluene, xylene, ethyl-benzene, distillates, dissolved salts, phosphates, iron, manganese, arsenic, poly-coagulants, fertilizers and animal waste is achieved through use of the instant inventor system. 
     The instant contaminant removal system is modular and is carried on trailers allowing the entire system to be mobile. The kilowatt (KW) requirement for the complete system is approximately 500 KW which may be supplied by portable skid mounted generator sets. 
     The performance of the instant system for removal of contaminants and recovery of the fluid is between approximately 350 gallons per minute (GPM) and approximately 450 GPM. 
     The instant system for separating contaminants from fluid removes even small amounts of oil that destroy Poly-Pan filtration membranes of salt removal systems which are costly to repair, replace and maintain. 
     Some or all of the problems, difficulties and drawbacks identified above and other problems, difficulties, and drawbacks may be helped or solved by the inventions shown and described herein. The instant invention may also be used to address other problems, difficulties, and drawbacks not set out above or which are only understood or appreciated at a later time. The future may also bring to light currently unknown or unrecognized benefits which may be appreciated, or more fully appreciated, in the future associated with the novel inventions shown and described herein. 
     BRIEF SUMMARY OF THE INVENTION 
     A system for separating contaminants from fluids provides a modular continuously operable mobile system having an oil-water separator, an optimizer, a dwell tank, a waste tank, a first particulate filter, a parallel second particulate filter, a first step down membrane filter, a parallel second step down membrane filter, a mixing station, a sensor array and a totalizer. An ultra-filtration system, a reverse osmosis filter and a chemical blender may be optionally added to the system to further contaminant removal. 
     In providing such a system for the separation of contaminants from fluids it is: 
     a principal object to provide a modular mobile system that is continuously operable even when components are being backwashed. 
     a further object to provide a modular mobile system that removes hydrocarbons. 
     a further object to provide a modular mobile system that provides a means for blending treated/filtered fluid with water to attain the desired standards. 
     a further object to provide a modular mobile system that will process acids and alkaline fluid through pH neutralization and balancing to attain desired standards. 
     a further object to provide a modular mobile system that provides an adjustable bypass where 100% of the fluid need not pass through the entire system. 
     a further object to provide a modular mobile system that allows the pH to be adjusted to desired standards to facilitate effective flocculation, coagulation, precipitation and contaminant separation/removal. 
     a further object to provide a modular mobile system that separates/removes micron size contaminants. 
     a further object to provide a modular mobile system that provides a variety of sensors and gauges to monitor head pressure, flow rate, flow volume and system performance. 
     a further object to provide a modular mobile system having parallel filter paths for continuous operation. 
     a further object to provide a modular mobile system that operates at low-pressure of approximately between 60 PSI and 100 PSI. 
     a further object to provide a modular mobile system that utilizes magnetic fields and electric fields between filter elements to exert ionic influences on charged and ionic particulates. 
     a further object to provide a modular mobile system that uses low pressure membranes to separate contaminants from fluids. 
     a further object to provide a modular mobile system that uses a “step down” process through plural fluidically interconnected bodies to facilitate continuous operation using membrane filters. 
     a further object to provide a modular mobile system having an optional ultra filtration manifold using replaceable filter cartridges. 
     a further object to provide a modular mobile system having an optional chemical blender to modify, buffer and pH balance the fluids. 
     a further object to provide a modular mobile system having an optional reverse osmosis filter. 
     a further object to provide a modular mobile system that provides an optional dwell tank to facilitate flocculation, precipitation and settling of contaminants and particulates. 
     a further object to provide a modular mobile system having a chemical meter for precisely metering additives into the fluids to facilitate and promote flocculation, coagulation, settling and precipitation and contaminant removal. 
     a further object to provide a modular mobile system that oxygenates fluids. 
     a further object to provide a modular mobile system that supplies ozone to the fluids. 
     a further object to provide a modular mobile system having filtration vessels that utilize a variety of filter medias. 
     a further object to provide a modular mobile system having filtration vessels that utilize crushed glass filter media. 
     a further object to provide a modular mobile system having filtration vessels that utilize IMA-65® as a filter media. 
     a further object to provide a modular mobile system that provides for continuous and “on demand” addition of chemicals to enhance and facilitate separation of contaminants and coagulation and precipitation of contaminants. 
     a further object to provide a modular mobile system having easily replaceable membrane filters. 
     a further object to provide a modular mobile system having variable membrane filter surface area. 
     a further object to provide a modular mobile system having a magnetic field and an electric field to exert magnetic field and electric field influences on charged and ionic particles within the fluids. 
     a still further object to provide a modular mobile system that provides a means to heat the fluid. 
     Other and further objects of the instant system for separating contaminants from fluids will appear from the following specification and accompanying drawings which form a part hereof. In carrying out the objects of the invention it is to be understood that its structures and features and steps are susceptible to change in design and arrangement and order with only one preferred and practical embodiment of the best known mode being illustrated in the accompanying drawings and specified as is required. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       Preferred forms, configurations, embodiments and/or diagrams relating to and helping to describe preferred aspects and versions of my invention are explained and characterized herein, often with reference to the accompanying drawings. The drawings and features shown herein also serve as part of the disclosure of my invention, whether described in text or merely by graphical disclosure alone. The drawings are briefly described below. 
         FIG. 1  is a block diagram of the instant inventive system for separating contaminants from fluids showing the relationship of the various components with fluid flow therethrough indicated by arrows. 
         FIG. 2  is an orthographic cross section of an oil water separator with arrows showing the direction of fluid flow therethrough. 
         FIG. 3  is an orthographic partial cutaway side view of one optimizer body with arrows showing the direction of fluid flow therethrough. 
         FIG. 4  is an orthographic partial cutaway side view of one particulate filter showing the filter medias therein with arrows showing the direction of fluid flow therethrough. 
         FIG. 5  is an orthographic partial cutaway side view of a step down membrane filter showing a membrane filter cartridge therein with arrows showing the direction of fluid flow therethrough. 
         FIG. 6  is an exploded orthographic side view of a membrane filter cartridge. 
         FIG. 7  is an orthographic plan view of an optional ultra-filtration manifold carrying plural screw on filter cartridges. 
         FIG. 8  is an orthographic partial cross section view of an ultra filtration canister carrying a paper filter cartridge therein taken on line  8 - 8  of  FIG. 7 . 
         FIG. 9  is an orthographic cross section view of an optional reverse osmosis filter. 
         FIG. 10  is an orthographic partial cutaway side view of a dwell tank with arrows showing the direction of fluid flow therethrough. 
         FIG. 11  is an orthographic partial cutaway side view of a waste tank. 
     
    
    
     DETAILED WRITTEN DESCRIPTION 
     Introductory Notes 
     The readers of this document should understand that dictionaries were used in the preparation of this document. Widely known and used in the preparation hereof are  The American Heritage Dictionary , (4th Edition© 2000),  Webster&#39;s New International Dictionary , Unabridged, (Second Edition© 1957),  Webster&#39;s Third New International Dictionary , (© 1993),  The Oxford English Dictionary  (Second Edition © 1989), and  The New Century Dictionary , (© 2001-2005), all of which are hereby incorporated by this reference for interpretation of terms used herein, and for application and use of words defined in such references to more adequately or aptly describe various features, aspects and concepts shown or otherwise described herein using words having meanings applicable to such features, aspects and concepts. 
     This document is premised upon using one or more terms with one embodiment that may also apply to other embodiments for similar structures, functions, features and aspects of the inventions. Wording used in the claims is also descriptive of the inventions, and the text of both the claims and the abstract are incorporated by this reference into the description entirely. 
     The readers of this document should further understand that the embodiments described herein may rely on terminology and features used in any section or embodiment shown in this document and other terms readily apparent from the drawings and language common or proper therefore. This document is premised upon using one or more terms or features shown in one embodiment that may also apply to or be combined with other embodiments for similar structures, functions, features and aspects of the inventions and provide additional embodiments of the inventions. 
     As used herein, the term “bottom” and its grammatical equivalents means that portion of the system for removing contaminants from fluids, or a component thereof, that is closest to a supporting ground surface. The term “top” and its grammatical equivalents means that portion of the system for removing contaminants from fluid, or a component thereof, that is vertically distal from the supporting ground surface. 
     A system for separating contaminants from fluids generally provides a modular mobile continuously operable multistage system having an oil water separator  100 , an optimizer  200 , a dwell tank  220 , a waste tank  250 , a particulate filter  300 , a step down membrane filter  400 , a mixing station  700  and a totalizer  900 . Optionally, the system for system contaminants from fluids may also provide an ultra filtration system  500 , a reverse osmosis filter  600  and a chemical blender  800 . 
     In a most simple description, the instant system takes contaminated fluid, such as but not limited to waste water from induced hydraulic fracturing operations and/or waste water from agricultural operations, or juice from fruit/vegetable pulping as an input, separates contaminants from the fluid through multiple stages of coagulation, precipitation and filtering and produces as an output, a fluid that is reusable, and separated concentrated contaminants that are graduated by particle site. The system is economical, continuously operable, is modular and is mobile. 
     The oil-water separator  100 , which may be a vertical tube coalescing filter, or a gravimetric API filter, or a parallel plate separator operating on the principals of specific gravity and Stokes Law is similar to an oil-water separator manufactured by Oil Water Separator Technologies, LLC of Florida USA. In the preferred embodiment the oil-water separator  100  is a parallel plate separator. The oil-water separator  100  ( FIG. 2 ) comprises a body  101  defining an interior volume  102  carrying plural parallel angulated separator plates  108  therein. The body  101  defines a fluid inlet  103  at a one end portion through which contaminated fluid enters the volume  102 . A sludge catch basin  104  is within the volume  102  proximate a bottom portion of the body  101 . Sludge drains  105  defined in the body  101  provide a means for removing sludge and the like from the volume  102 . A rotary skimmer  106  is carried within the volume  102  proximate a top portion and spaced apart from the fluid input  103 . The rotary skimmer  106  rotates on an elongate axis and removes contaminants agglomerating on an upper surface of fluid within the volume  102 . The plural parallel angulated plates  108  are carried within the volume  102  spacedly below the rotary skimmer  106 . Contaminants such as oil agglomerate on bottom surfaces of the plural parallel angulated plates  108 . As the agglomerations of oil become larger the agglomerations tend to move upwardly along the bottom surface of the plural parallel angulated separator plates  108  and ultimately “float free” from the plural parallel angulated separator plates  108  to rise to the surface of the fluid within the volume  102  to be removed by the rotary skimmer  106 . Sediments within the fluid fall onto top surfaces of the plural parallel angulated separator plates  108  and collect in the sludge basin  104 . Adjustable wire plates  110  allow the fluid levels to be adjusted as needed to promote contaminant removal. A fluid outflow  109  is defined in the body  101  distal from the fluid input  103 . 
     In the preferred embodiment, the oil-water separator  100  is trailer mounted and is mobile. The oil water separator  100  fluidically and electrically interconnects with the other components of the system by known plumbing and electrical interconnections and apparatus. From the oil water separator  100  the fluid flows through the fluid outflow  109  to the optimizer  200 . 
     The optimizer  200  ( FIGS. 1 and 3 ) comprises plural bodies  201  fluidically communicating with one another by known plumbing apparatus. Each body  201  has a top  202 , a bottom  203 , a side portion  204  extending from the top  202  to the bottom  203  and defines an interior volume  205 . An inflow port  206  defined in the side portion  204  generally medially between the top  202  and bottom  203  communicates with the interior volume  205  and allows fluids from the oil-water separator  100  to flow into the volume  205 . An outflow port  208  is defined in the side portion  204  of each body  201  preferably at a position vertically above the inflow port  206 . A chemical input port  209  communicating with the volume  205  is defined in a top portion  202  of each body  201 . A chemical additives meter  214  communicates with the chemical input port  209  to add/meter into the interior volume  205  precise amounts of chemical additives, such as but not limited to, pH buffers, acids, bases, flocculants, poly-coagulants and the like which may enhance coagulation and precipitation of contaminants within the fluid. 
     The chemical additive meter  214  will automatically or manually add various types of coagulants and/or other chemical additives to the fluid within the optimizer  200 . Coagulants (not shown) added to the fluid within the optimizer  200  causes contaminants and small particulates within the fluid to coagulate together and form floccules which are more readily filtered from the fluid. A solids draw off port  207  is defined proximate the bottom  203  of the optimizer  200  to allow coagulated and/or precipitated solids to be removed from the volume  205 . 
     Heater  210  communicates with each body  201  proximate the bottom  203  to heat fluid within each body  201  to a desired optimal temperature for coagulation and precipitation. It is anticipated the heater would be electrically powered using heating elements (not shown) but it is also possible the heater may be operated by other known means. A diffuser plate  211  defining a plurality through holes therein is carried within the interior volume  205  spaced above the bottom  203  and an air input port  212  and an ozone input port  213  is defined in the body  201  below the diffuser plate  211  to allow air and/or ozone to be injected into the interior volume  205  creating a plurality of bubbles to “bubble up” through the diffuser plate  211  and the fluid within the interior volume  205  to enhance coagulation and precipitation of contaminants. The addition of ozone to the fluid within the interior volume  205  provides the added benefit of rapidly oxidizing a variety of chemicals and contaminants and also killing various bacteria, algae and molds that may be present in the contaminated fluid. The use of ozone reduces the need for adding biocides and similar chemicals to kill plants and organisms within the fluid. 
     A pump  215  communicates with plumbing means to move fluid into and out of the interior volume  205  of each body  201 . As shown in  FIG. 1  plural bodies  201  are interconnected to provide an efficient optimizer  200  that provides adequate time for metered-in chemical additives, pH balancers, coagulants and the like to react with the fluid. 
     An optional dwell tank  220  ( FIG. 10 ) fluidically communicates with the optimizer  200  and provides a location where the fluid, which has had pH buffers, chemical additives, flocculent, precipitates, acids, bases and the like added thereto may “rest” while precipitates “fallout” of the fluid column therein. The dwell tank  220  is preferably a generally cylindrical and mobile tank having a top  221 , a bottom  222 , a side portion  223  extending from the top  221  to the bottom  222  and defines an interior volume  224 . Inflow port  225  is defined in the dwell tank  220  spacedly between the top  221  and the bottom  222 . An outflow port  226  is defined in the side portion  223  preferably at a position vertically above the inflow port  225  so that precipitates and solids “falling out” or otherwise precipitating in the fluid column within the interior volume  224  may settle to the bottom  222  and not flow outwardly from the interior volume  224  when the fluid is removed from the dwell tank  220 . The treated fluid within the dwell tank  220  is moved into the dwell tank  220 , and out of the dwell tank  220 , by means of pump  215  and valves communicating with known plumbing means. 
     A waste tank  250  ( FIG. 11 ) has a top  251 , a bottom  252 , a side portion  253  extending from the top  251  to the bottom  252  and defines an interior volume  254 . An inflow port  255  communicates with the interior volume  254  and provides an access through which waste, sludge and the like may be deposited in the waste tank  250  interior volume  254 . An outflow port  256  is defined in the waste tank  250  proximate the bottom  252  and provides a means for draining, or otherwise removing waste from within the interior volume  254 . The waste tank  250  fluidically communicates with the oil-water separator  100 , with the optimizer  200 , with the dwell tank  220  by means of known plumbing interconnections and pumps and valves. The waste tank  250  provides a secure and safe location for storage of hazardous chemicals and waste products filtered out of the fluid passing through the instant system for removing contaminants from fluids. It is anticipated waste collected within the waste tank  250  would be transported, on an as needed basis, to a hazardous waste site, or other approved disposal site for waste chemicals. The waste tank  250 , because it defines a completely enclosed volume  204  prevents evaporation and volatization of chemicals and additives therein and also protects the environment, wildlife and surroundings. 
     The outflow port  208  defined in the optimizer  200 , and the outflow port  226  defined in the dwell tank  220  each communicate with a selector valve  230  for directing the fluid from the optimizer  200  to the particulate filter  300  and fluid from the dwell tank  220  to the particulate filter  300 . 
     The particulate filter  300  ( FIGS. 1 and 4 ) has two parallel filter assemblies which are herein referred to as a first particulate filter  300 A and a parallel second particulate filter  300 B. Fluids to be filtered may flow through either the first particulate filter  300 A, or through the parallel second particulate filter  300 B or through both particulate filters  300 A,  300 B by operation valve  230 . Because the particular filters  300 A,  300 B are similar to one another, only the first particulate filter  300 A will be described in detail herein. 
     The particular filter  300  comprises plural fluidically interconnected filter bodies  301 , each having a top  302 , a bottom  303  and a side portion  304  extending from the top  302  to the bottom  303 . Each body  301  defines an interior volume  305 . In the preferred embodiment, each body  301  is an approximately sixty inch (152.4 cm) diameter “vertical barrel type” filter canister such as those made by Yardney®, Inc. of California USA. The bodies  301  are fluidically interconnected with one another by known plumbing apparatus and connections. 
     Each body  301  ( FIG. 4 ) defines an inflow port  306  and a spaced apart outflow port  307 . The interior volume  305  of each filter body  301  contains plural filter medias preferably a first filter media  310 , a second filter media  311 , a third filter media  312 , and a fourth filter media  313 . Each filter media  310 ,  311 ,  312 ,  313  is particulated and the particulates have different sizes and different weights so that the filter medias  310 ,  311 ,  312 ,  313  vertically stack automatically—by gravity due to weight—and will generally “re-stack” automatically subsequent to any backwash cleaning process. 
     The first filter media  310  is preferably particulated small diameter anthracite coal and the particulates thereof form a first upper most layer within the filter body  301  and is between approximately 3 inches (7.5 cm) in depth and 18 inches (46 cm) in depth. The anthracite coal particles preferably have a particle size of approximately between 0.5 mm to 1.15 mm in diameter. 
     The second filter media  311  positioned vertically below the first media  310  is preferably particulated garnet and the particulates are preferably approximately 0.25 mm to 0.5 mm in diameter. Because the particulated garnet is heavier than the anthracite coal it creates a “medial” layer within the filter body  301  and is between approximately 3 inches (7.5 cm) in depth and 18 inches (46 cm) in depth. 
     The third filter media  312  is preferably either particulated garnet or silica having an average particulate size of approximately between 1.15 mm to 2.0 mm in diameter. Because the particulates of the third filter media  312  are larger than those of the second filter media  311  the third media particulates  312  will tend to stack vertically below the second filter media  311 . The third filter media  312  preferably has a depth of between approximately 6 inches (15 cm) and 36 inches (92 cm). 
     The fourth filter media  313  is preferably particulated rock, the particulates having an average particulate size of approximately between 0.3 inches (0.7 cm) and 0.85 inches (2.2 cm) in diameter. The fourth filter media  313  is the bottom layer of the filter medias  310 ,  311 ,  312 ,  313  within the filter body  301  and preferably has a depth of between approximately 6 inches (15 cm) and 36 inches (92 cm) inside the volume  305  of the filter body  301 . A septum (not shown) or other known apparatus retains the filter medias  310 ,  311 ,  312 ,  313  within the volume  305  and prevents the filter medias  310 ,  311 ,  312 ,  313  from passing through the outflow port  307  during filtration. 
     In a second preferred embodiment, at least one of filter medias  310 ,  311 ,  312 ,  313  is crushed glass. The use of crushed glass as a particulated filtration media  310 ,  311 ,  312 ,  313  allows filtration of smaller/finer particles from the fluid due to the configurations and edge portions of the glass particles. Use of crushed glass as the filter media allows the instant system for removing contaminants from fluids to remove particles down to approximately 8 microns in size. 
     In a still further preferred embodiment, at least one of filter medias  310 ,  311 ,  312 ,  313  is a filter media commercially known as IMA-65™ which is manufactured by Yardney™ Water Filtration Systems of Riverside Calif., USA. IMA-65 has a unique property of chemically reacting with contaminants such as, but not limited to, Iron (Fe), and Manganese (Mg), and Arsenic (Ar), and is effective in removing these and other contaminants from the fluid. Further, IMA-65 reduces and/or eliminates the necessity of adding potassium permanganate into the fluid stream to cause effective coagulation, precipitation and filtration. In place of the added potassium permanganate, use of IMA-65 as a filtration media  310 ,  311 ,  312 ,  313  allows small amounts of chlorine (CI) to be used in place of the potassium permanganate. 
     The plural filter bodies  301  are interconnected to one another in parallel by known plumbing apparatus and fittings so that inflow of fluid enters the inflow ports  306  of each of the plural bodies  301  generally simultaneously and percolates through the filter medias  310 ,  311 ,  312 ,  313  and exits the outflow ports  307  generally simultaneously. Known plumbing connections communicating with the outflow ports  307  thereafter communicate with selector valves  330  that may be actuated to initiate backwash cleaning operations. 
     A variety of sensors (not shown) and gauges (not shown) communicate with the volume  305  inflow port  306  and outflow port  307  of each body  301  to monitor head pressure, flow rates and conditions within the volumes  305 . Any increase in “head pressure” or decrease in flow rate is indicative of the filter medias  310 ,  311 ,  312 ,  313  becoming saturated or otherwise plugged with contaminants such that fluid passage therethrough is reduced. When saturation or “plugging” occurs, selector valve  230  may be manually or automatically activated which directs the fluid input from the optimizer  200  and/or dwell tank  220  to flow through known plumbing connections into the parallel second particulate filter  300 B to maintain continuous filtration operations. While the fluid is being filtered by the parallel second particulate filter  300 B, the first particulate filter  300 A may be backwashed by forcing clean water through valve  330  and through backwash in flow port  308  and through the filter medias  310 ,  311 ,  312 ,  313  in a reverse direction which causes the accumulated contaminants within the filter medias  310 ,  311 ,  312 ,  313  to flow outwardly through a backwash outflow port  309  whereupon the out flowing contaminants may be fluidically directed to the waste tank  250  for collection, storage and ultimate disposal. Depending upon the type of contaminants and/or particulates being removed it may be desirable to direct the backwash from the particulate filter  300  in to the optimizer  200  for further precipitation of particulates in order to further save volumes of fluid. 
     The backwash cleaning function/operation is a conventional operation well known to those familiar in the art of fluid filtration systems and requires that the direction of fluid flow be reversed. Various known manual and automatic valves and pumps are utilized to initiate and perform the backwash function. The variety of valves isolate specific components of the system allowing the fluid flow to be reversed only through the selected components while fluid flow through the system in the “filtering direction” continues through the non-backwashing components of the system. 
     The continuous filtration of the coagulated fluids from the optimizer  200  and/or dwell tank  220  continues in uninterrupted by using the parallel second particulate filter  300 B while the first particulate filter  300 A is backwashed, flushed and cleaned. The process is repeated when the parallel second particulate filter  300 B becomes saturated, clogged, plugged or the sensors indicate the flow rate is diminished or the “head pressure” has increased to a predetermined level. Although not shown in the accompanying Figures, it is expressly contemplated that additional parallel particulate filters  300  similar to the first particulate filter  300 A and the parallel second particulate filter  300 B may be plumbed in parallel into the instant system for removing contaminants from fluids to provide additional redundancy and contaminant removal capability. The mobile truck mounted nature of the instant invention further allows the addition of additional particulate filters  300  to be simple, efficient and customizable for geological conditions and user needs. 
     Known plumbing apparatus and connections communicate with the outflow ports  307  of the plural filter bodies  301  of the first particulate filter  300 A and the parallel second particulate filter  300 B to channel the fluid to subsequent components of the instant system for removing contaminants from water. 
     A valve  320  ( FIG. 1 ) allows the fluid existing the first particulate filter  300 A and parallel second particulate filter  300 B to alternatively be directed to a water mixing station  700  or through another valve  430  for directing the fluid to the step down membrane filter  400 . 
     The step down the membrane filter  400  has two parallel filter assemblies which are referred to herein as a first step down membrane filter  400 A and a parallel second step down membrane filter  400 B. Fluid from the particulate filter  300  may flow through either or both the first step down membrane filter  400 A, and/or through the parallel second step down membrane filter  400 B by means of valve  430 . Because the first step down membrane filter  400 A and the second step down membrane filter  400 E are similar to one another, only the first step down membrane filter  400 A will be described in detail herein. 
     The step down membrane filter  400  ( FIG. 1 ) comprises plural fluidically interconnected filter bodies  401 , ( FIG. 5 ) each having a top  402 , a bottom  403  and a side portion  404  extending from the top  402  to the bottom  403 . Each body  301  defines an interior volume  405 . In the preferred embodiment, each body  401  is an approximately sixty inch (153 cm) diameter “vertical barrel type” filter canister such as those made by Yardney®, Inc. of California USA. The plural bodies  401  are fluidically interconnected with one another by means of known plumbing apparatus and connections. 
     Each body  401  defines an inflow port  406  an outflow port  407 , a backwash inflow port  408  and a backwash outflow port  409 . All ports  406 ,  407 ,  408  and  409  communicate with the interior volume  405 . An access hatch (not shown) is defined in the body  401  and provides user access to the interior volume  405  of the body  401  for maintenance, inspection, membrane filter  413  replacement and the like. 
     A removable/replaceable membrane filter cartridge  417  is carried within the interior volume  405  of each filter body  401 . Each removable/replaceable membrane filter cartridge  417  ( FIG. 6 ) has an outer membrane cage  411  and an axially aligned diametrically smaller inner membrane cage  412 . The membrane cages  411 ,  412  are each preferably elongate and tubular in configuration and each defines a plurality of through holes  420  therein to allow fluid to flow therethrough. A filter membrane  413  such as, but not limited to a Poly Nitryl (Poly-Pan) low-pressure reverse osmosis membrane such as the AP Series™ of thin film reverse osmosis membranes manufactured by GE® Power &amp; Water of Fairfield Conn. USA is wrapped circumferentially about an outer circumferential surface of the inner membrane cage  412  in a series of “wraps” to entirely cover the outer circumferential surface of the inner membrane cage  412 . The number of wraps may be varied (increased/decreased) to adjust porosity, surface area, flow rate and the like to suit the contaminated fluid requirements. Thereafter, the outer membrane cage  411  is interconnected with the inner membrane cage  412  exterior of the wraps of filter membrane  413  so that the filter membrane  413  is positionally secured between the inner membrane cage  412  and the outer membrane cage  411 . The plurality of through holes  420  defined in the membrane cages  411 ,  412  allows fluid to pass therethrough and into direct physical contact with the filter membrane  413 . Septums (not shown) which may be electrically conductive may be positioned between the wraps of the filter membrane  413  causing the wraps of filter membrane  413  to be spaced apart from one another. Alternatively, if less porosity is desired a series of filter membrane  413  wraps may be positioned in direct frictional contact with one another. 
     The filter membrane  413  is a low-pressure membrane operating at between approximately 60 PSI and 100 PSI. This low-pressure is sufficient to cause fluid flow through the filter membrane  413  from one surface to the opposing surface. The filter membrane  413  separates contaminants from the fluids by preventing the contaminants from passing through the filter membrane  413  while allowing the fluid to pass therethrough. 
     The membrane filter cartridge  417  ( FIG. 6 ) carries a sealed cap  418  at each opposing end portion that interconnects the outer membrane cage  411  to the inner membrane cage  412  with the filter membrane  413  secured therebetween. 
     A first electrical lead  450  is connected to the inner membrane cage  412  and a second electrical lead  451  is connected to the outer membrane cage  411 . Application of an electrical current to the electrical leads  450 ,  451  creates a magnetic field between the two membrane cages  411 ,  412  which permeates through the membrane filter  413  which causes ionic molecules and charged particulates and poly-coagulants to be attracted to one of the membrane cages  411 ,  412 . In the preferred amendment a voltage of approximately between 12 volts and 36 volts at a current of approximately between 10 amps and 25 amps is applied to the membrane cages  411 ,  412 . If electrically conductive septums (not shown) are carried within the membrane filter cartridge  417  between the wraps of filter membrane  413 , the electrical leads  450 ,  451  may similarly be interconnected to the septums (not shown) to generate magnetic fields and electric fields. The application of electrical current to the membrane cages  411 ,  412  and septums (not shown) further enhances the contaminant removal capability of the instant system by causing ionically charged particulates and/or molecules to migrate towards one of the membrane cages  411 ,  412 . During backwashing/cleaning functions the polarity of the electrical current is reversed to “drive” the ionic molecules and/or particulates away from the filter membrane  413  and membrane cages  411 ,  412  and septums (not shown) to be removed during the backwash cleaning operation. 
     Filter connections  419  are carried by each body  401  within the volume  405  and provide a watertight connection between the sealed caps  418  and top and bottom interior portions (not shown) of the filter body  401 . Bottom filter connection  419  fluidically communicates with the outflow port  407  and top filter connection  419  provides a fluid tight seal about the backwash inflow port  408 . The watertight interconnection between the sealed caps  418  and the filter connections  419  forces fluid within the interior volume  405  to flow in a single direction through the membrane filter cartridge  417 . As shown by direction allows in  FIG. 5 , fluid enters the volume  405  through the inflow port  406  and physically contacts the exterior surface of the membrane filter cartridge  417  and exterior surface of the outer membrane cage  411 . The fluid tight engagement between the sealed caps  418  and the filter connections  419  prevent the fluid from communicating with the outflow port  407  without having first passed through the membrane filter cartridge  417 . The fluid pressure within the bodies  401  forces the fluid through the filter membrane  413  where the particulates and contaminants are separated from the fluid by the filter membrane  413  and by the magnetic field generated by the electrical current. The porosity of the filter membrane  413  is engineered so that only fluid, but not particulates, may pass therethrough to the interior portion of the membrane filter cartridge  417  wherein the fluid may exit the body  401  through the outflow port  407 . 
     Membrane type filters are known in the industry, but heretofore have not been used to filter heavily contaminated fluids because membrane filters generally require high pressures to force contaminated fluid through the membrane material because only a small amount of membrane surface area is available for contaminant removal due to the high pressures required and because membranes are easily plugged, damaged and destroyed by oils, hydrocarbons and the like. Further, membrane filters have a well-recognized drawback of completely preventing fluid pass-through once a contaminant saturation point has been reached. For this reason, among others, membrane filters require tremendous amounts of maintenance and observation during use and are not well suited for heavily contaminated fluids or fluids that contain hydrocarbons that will cause saturation points to be quickly reached. 
     The instant invention overcomes these and other known drawbacks to membrane type filters by providing a “step down” series of membrane filters that are operated in series and by providing multiple times the amount of membrane surface area available for contaminant separation. The “step down” configuration of the instant system for separating contaminants from fluids is functional because a first step down membrane filter body  401  carries a removable and replaceable membrane filter cartridge  417  therein having a lesser number of membrane “wraps” around the inner membrane cage  412 . The filter membrane  413  is relatively thin and relatively porous so that only larger particulates and larger size contaminants are removed as the fluid passes therethrough under low-pressure. A second step down membrane filter body  401  fluidically communicates in series with the first step down membrane filter body  401  by means of known plumbing connections wherein the outflow port  407  of the first step down membrane filter body  401  communicates with the inflow port  406  of the second step down membrane filter body  401 . The membrane filter cartridge  417  within the second step down membrane filter body  401  has a greater number of filter membrane  413  “wraps” around its inner membrane cage  412  such that the filter membrane  413  is less porous than the filter membrane  413  in the first step down membrane filter body  401 . Each body  401  communicates with a next body  401  in the series with the same fluid flow direction therethrough, namely the outflow port  407  of one body  401  communicating with the inflow port  406  of the next body  401 . Similarly, the membrane filter cartridges  417  of each successive body  401  in the series of filter bodies  401  has a greater number of “wraps” around the inner membrane cage  412  so that as the fluid passes successively through each body  401  and each membrane filter cartridge  417  the contaminates and particulates within the fluid are removed with the larger contaminants and particulates being removed first, and successively smaller contaminants and particulates being removed through the successive membrane filters cartridges  417 . Only a portion of the particulates and contaminants are removed from the fluid in each body  401 . 
     Through this configuration of a series “step down” the fluid may be continuously filtered, and the well-known drawback of membrane filters becoming quickly saturated is overcome because each membrane filter cartridge  417  in the series has a different porosity, and is only separating out a portion of the contaminants and particulates within the fluid. The series of membrane filters  417  configured, as described herein, has the ability to ultimately remove contaminants and particulates from the fluid down to approximately 6 microns in size. 
     This configuration of step-down membrane filters  400  also provides an effective means to recover finely graduated particulates from the fluid and such finely gradiated particulates may be commercialized as a useful product. For example, if the fluid passing through the instant system is fruit or vegetable juice, the fruit/vegetable pulp may be gradiated by particulate size. The step-down configuration of the instant step-down membrane filters  400  allows various sizes of pulp particulates to be separated for commercialization, as it is well recognized that particular sizes of pulp particulates are commercially desirable as food additives, while the sizes are waste products. Further particulates of minerals such as gold and silver which are canned in solution from each mining operation may likewise be separated from the fluid and sized. 
     The collection of gradiated particulates is accomplished by interconnecting the backwash outflow  409  of each body  401  separately to a collection body  435  so that the backwash outflow from each body  401  flows into the collection body  435 . Because each body  401  may be backwashed independently from the other bodies  401  in the sizes of the contaminants/particulates flowing into the collection body  435  from a particular step-down membrane filter body  401  will be only the size contaminants/particulates that one removed by the membrane filter cartridge  417  of that particular body  401 . 
     A variety of sensors (not shown) and gauges (not shown) that sample for and measure characteristics such as, but not limited to, PH, Cl, Fe, O 2 , Phosphates and silt density (SDI) such as those manufactured by Hawk® Measurements of Middleton, Mass., USA communicate with the volume  405  of each body  401  to monitor head pressure and flow rates within the volumes  405 . An increase in “head pressure” or decrease in flow rate is indicative of the membrane filter cartridges  417  becoming saturated or otherwise plugged with contaminants such that fluid passage therethrough is reduced. When saturation or “plugging” or flow rate reductions occur, selector valve  430  may be activated which directs the fluid to flow through known plumbing connections into the parallel second step down membrane filter  400 B to maintain continuous filtration operations. While the fluid is being filtered by the parallel second step down membrane filter  400 B, the first step down membrane filter  400 A may be backwashed  75  by forcing clean water through the membrane filter cartridges  417  in a reverse direction which causes the accumulated contaminants within the membrane filter cartridges  417  to flow outwardly through a backwash outflow ports  409  and into the collection body  435  by known means whereupon the contaminants, and particulates may be collected for use and/or directed to the waste tank  250  for collection, storage and ultimate disposal. During the backwash  75  process the polarity of the voltage applied to the membrane cages  411 ,  412  is be reversed to drive charged particulates and ionic molecules into the backwash flow for removal. 
     As noted previously, the backwash function/operation is a conventional operation well known to those familiar in the art of fluid filtration systems. In  FIG. 1  the backwash system is identified with the numeral  75  and fluid input to operate the backwash system  75  is identified with the numeral  50 . 
     The continuous filtration of the fluid exiting the particulate filters  300  may continue in uninterrupted fashion by using the parallel second step down membrane filter  400 B while the first step down membrane filter  400 A is backwashed, flushed or otherwise cleaned. The process is repeated when the parallel second step down membrane filter  400 B becomes saturated, clogged, plugged or the sensors indicate the flow rate is diminished or the “head pressure” increases over a predetermined level. Although not shown in the accompanying Figures, it is expressly contemplated that additional parallel step down membrane filters  400  similar to the first step down membrane filter  400 A and the parallel second step down membrane filter  400 B may be plumbed in parallel into the contaminant removal system to provide additional redundancy and contaminant removal capability. The mobile truck mounted nature of the instant invention further allows the addition of additional filter units to be simple and efficient and customizable for site specific conditions. 
     Fluid exiting the outflow ports  407  of the step down membrane filters  400  communicates with a valve  530  which directs the out flowing fluid to either the mixing station  700  or to an optional ultra filtration system  500 . 
     The ultra filtration system  500  ( FIGS. 7, 8 ) has a first ultra filtration manifold  500 A and a parallel second ultra filtration manifold  500 B. Because the first ultra filtration manifold  500 A and the parallel second ultra filtration manifold  500 B are similar, only the first ultra filtration manifold  500 A will be described in detail herein. As shown in  FIG. 7 , the ultra filtration manifold  500 A is configured to threadably receive plural filter cartridge bodies  502 . Each of the plural filter cartridge bodies  502  carries within a medial chamber  504  defined therein, a replaceable filter cartridge  503  such as a paper filter cartridge manufactured by Mann+Hummel, Inc. of Bloomfield Hills, Mich., USA that is capable of filtering even smaller micron size particles out of fluids passing therethrough. Such filter cartridges  503  are generally not tolerant of backwash cleaning operations and are instead replaced when saturated/plugged with contaminants/particulates. 
     A valve  531  interconnected with outflow ports (not shown) of the ultra filtration manifolds  500 A,  500 B receives filtered fluid therefrom and thereafter directs the filtered fluid either to the metering station  700  or to an inflow port  603  of the optional reverse osmosis filter  600 . 
     The optional reverse osmosis filter  600  ( FIG. 9 ) is of a known configuration, such as a reverse osmosis filter system designed and built by General Electric® Inc. (GE®). As shown in  FIG. 9 , the reverse osmosis filter  600  has a body  601  that defines an interior volume  602 . An inflow port  603  and an outflow port  604  are defined in the body  601  and communicate with the volume  602 . In one preferred embodiment, the reverse osmosis filter  600  carries a plurality of membrane filters  606  within the volume  602  that are preferably formed from a material such as, but not limited to, Polyacryl Nitryl Pan Polymer (commonly known as Poly-Pan membranes) which is known for its capability to remove dissolved salts from fluids. The reverse osmosis filter  600  has a continuous filtering volume capacity of approximately 600 GPM. However, by adjusting valve  531  the amount of fluid flowing into the reverse osmosis filter  600  may be adjusted below the maximum filtering capacity with the remaining amount of fluid from the ultra filtration manifold  500  passing directly to the mixing station  700  by known plumbing means rather than to the reverse osmosis filter  600 . 
     The use of the plural filter systems  100 ,  200 ,  220 ,  300 ,  400 ,  500  upstream from the reverse osmosis filter  600  is essential to the maintenance and longevity of the reverse osmosis filter  600  which is susceptible to damage and destruction by even miniscule amounts of petroleum based contaminants, such as any hydrocarbons or oil remaining in the fluid. 
     After the fluid has passed through the optional reverse osmosis filter  600 , the fluid exits the outflow port  604  and passes through an outflow control valve  605  used to precisely control outflow. Known plumbing apparatus and fittings interconnect the outflow control valve  605  to the water mixing station  700  at which point the wastewater outflow from the reverse osmosis filter  600  may be mixed with fluid coming from the first particulate filter  300 A and/or the parallel second particulate filter  300 B. Fluid mixing at the mixing station  700  allows fluid filtration to continue at a maximum rate while generating an outflow that meets or exceeds specifications, standards and regulations set forth by various governing authorities and/or users, such as but not limited to, induced hydraulic fracturing operators. For example, if the fluid outflow exiting the first particulate filter  300 A and parallel second filter particulate filter  300 B has minimal amounts of dissolved salt, use of the reverse osmosis filter  600  may not be necessary and therefore a large percentage of the fluid outflow may pass directly from the first particulate filter  300 A and parallel second particulate filter  300 B to the mixing station  700 . Alternatively, if the outflow from the first particulate filter  300 A and parallel second particulate filter  300 B has high levels of dissolved salts, it may be necessary to direct nearly all of the fluid outflow through the ultra filtration system  500  and through the reverse osmosis filter  600  to remove the dissolved salts. If the outflow from the particulate filters  300 A,  300 B has high levels of dissolved solids but not dissolved salts, it may be desirable to direct the fluid outflow only to the ultra-filtration system  500  and not the optional reverse osmosis filter  600 . 
     The mixing station  700  defines an inflow port  701  and an outflow port  702  and is fluidically interconnected with the other components of the system by known plumbing apparatus and fittings so that fluid from the particulate filters  300 , from the step down membrane filters  400 , from the optional ultra filtration manifolds  500 A,  500 B and the optional reverse osmosis filter  600  passes into the inflow port  701 . The mixing station  700  has a sensor array (not shown) that allows the filtered fluid outflow from the system to be tested with various sensors, scanners, samplers and testing apparatus and, for example, allows the pH of the water to be determined and thereafter and adjusted by addition of various chemicals including buffers for controlled neutralization of acids and the like. Other characteristics that are determined and may be adjusted include, but are not limited to, Silt Density Index (SDI), Fe, Cl, O 2 , Mg, CO 2 , N 2 , NO and phosphates. The mixing station  700  allows volumes of clean fluid, which may be water, to be added to the filtered and treated fluid flow to dilute any contaminant concentrations in the fluid. 
     Fluid exiting the mixing station  700  passes through the outflow port  702  and thereafter through known plumbing apparatus to a totalizer and sensor array  900 . The totalizer and sensor array  900  defines an inflow port  905  and defines an outflow port  906 . Positioned between the inflow port  905  and the outflow port  906  are various sensors (not show) and meters (not shown) and samplers (not shown) to test and measure and sample the fluid passing therethrough for components and characteristics such as, but not limited to, temperature, pH, dissolved solids, dissolved salts, mineral content, bacteria, oxygen content, nitrogen content, silt density and the like. A sensor array such as those manufactured by Hawk Measurements, Inc. is anticipated for use and provides an automated means to continually test and monitor the fluid output of the system. Information and data provided by the totalizer and sensor array  900  will allow operators to determine when and if to backwash and/or change filters and or alter chemical additives/treatments to the fluid. The totalizer and sensor array  900  provides a means to measure the quality and quantity and volume of fluid passing through the system which provides a means by which an owner of the system may bill/invoice an operator/lessee of the system on a volume basis of filtered fluid (by gallon, barrel, liter or other volume measurement) or by gallon/barrel/liter per minute whichever calculation means is agreed upon. 
     A volume meter  99  measures the volume of fluid flowing into the oil-water separator  100  and provides a baseline measurement against which can be compared the outflow volume determined by the totalizer and sensor array  900 . 
     Having described the structure of the system for separating contaminants from fluid, its operation may be understood. 
     The oil-water separator  100 , the optimizer  200 , the dwell tank  220 , the waste tank  250 , the particulate filter  300 , the step-down membrane filter  400 , the optional ultra filtration system  500 , the optional reverse osmosis filter  600 , the mixing station  700  and the totalizer and sensor array  900  are all mobile and preferably truck trailer mounted or skid mounted. The various components are moved to the desired location and positioned relative to one another so that fluid interconnections between the various components can be established with known plumbing apparatus. Electrical power to the system pumps, sensors, valves and the like may be provided by a generator (not shown) or by interconnecting the system components to the local electrical grid. After the various components are interconnected, a pump (not shown) is primed with the fluid to be filtered and treated and the fluid is pumped to the volume meter  99  which is the fluid entry point for the system. 
     As fluid is pumped into the system the fluid passes through the plumbing apparatus and connections and passes into the various volumes  102 ,  205 ,  224 ,  305 ,  405 ,  504 ,  602  defined by the various components. As the fluid flows through the interconnected components the fluid is treated and filtered and is exposed to various additives, chemicals, pressures, electric fields and filter membranes which remove the contaminants and/or particulates from the fluid. 
     A first contaminant and/or particulate removal occurs within the oil-water separator  100  which removes oils, hydrocarbons and sediment. Floating oil agglomerations and the like are skimmed from the fluid within the oil water separator  100  by the rotary skimmer  106 . Sediment sinks to the sludge basin  104 . Fluid passing out of the oil water separator  100  passes into the optimizer  200  where the fluid may be treated with heat, ozone, oxygen and chemicals to facilitate precipitation, flocculation and settling. Fluid flowing through the optimizer  200  may be optionally directed into the dwell tank  220  if additional time is needed for precipitation, flocculation and settling of particulates to occur. 
     Fluid from the optimizer  200 , and from the dwell tank  220  after further precipitation if further precipitation is needed, passes to and through valve  230  and is directed to either the first particulate filter  300 A or the parallel second particulate filter  300 B for filtration through the filter medias  310 ,  311 ,  312 ,  313  contained within the plural filter bodies  301 . If crushed glass filter media  310 ,  311 ,  312 ,  313  is used within the filter bodies  301  contaminants and/or particulates within the fluid having a size of approximately 8 microns are removed as the fluid passes through the filter medias  310 ,  311 ,  312 ,  313 . Sensors, samplers, monitors and the like monitoring and testing fluid pressures, fluid flow and head pressure within the particulate filter  300 A bodies  301  monitor for when the fluid pressures, head pressure and/or fluid flow reaches a predetermined level which is indicative of the filter medias  310 ,  311 ,  312 ,  313  becoming plugged, clogged and/or saturated with contaminants and/or particulates. Upon reaching such predetermined level, valve  230  is activated and the fluid flow from the optimizer  200  is directed into the parallel second particulate filter  300 B for filtration and treatment of the fluid to continue uninterrupted. While the fluid from the optimizer  200  is flowing into and through the parallel second particulate filter  300 B, valves  330  communicating with the first particulate filter  300 A are activated allowing clean fluid, which may be water, to flow through the first particulate filter  300 A in a reverse direction, known as backwashing  75 , which forces accumulated contaminants, particulates and the like out of the filter medias  310 ,  311 ,  312 ,  313  in a reverse direction where the accumulated contaminants and/or particulates may be directed to the waste tank  250 . It is anticipated the backwash  75  procedure will take approximately three minutes. When the sensors, samplers, monitors and the like detect the pressures, head pressure and volume flow in the parallel second particulate filter  300 B reach the predetermined levels, valve  230  is again activated which directs the fluid flow from the optimizer  200  back into the first particulate filter  300 A while the parallel second particulate filter  300 B is backwashed  75  to remove accumulated contaminants and particulates therein. 
     Fluid outflow from the particulate filter  300  passes to valve  320 . If the fluid flow from the particulate filters  300  has been treated and filtered sufficiently to meet determined standards for purity and quality control, the fluid may pass through valve  320  and into the mixing station  700 . If the fluid needs additional treatment and/or filtration, valve  320  will direct some portion of the fluid or perhaps all of the fluid from the particulate filter  300  to valve  430  and to the step-down membrane filter  400 . Valve  430  directs the fluid flow to either the first step-down membrane filter  400 A or to the parallel second step-down membrane filter  400 B for filtration of the fluid through the membrane filter cartridges  417  carried in each of the bodies  401 . Because each of the of the step-down membrane filter bodies  401  carry a membrane filter cartridge  417  within the volume  405  defined thereby, and because each of the membrane filter cartridges  417  in the series of step-down membrane filter bodies  401  have an increasing number of “wraps” of low pressure Poly-Pan filter membrane  413  between the metallic inner membrane cage  412  and outer metallic membrane cage  411 , the porosity of the membrane filter cartridges  417  decreases as the fluid flows through each of the step-down membrane filter cartridges  417  in series. Each of the step-down membrane filter bodies  401  in the series separates only a portion of the contaminants and/or particulates from the fluid passing therethrough because each membrane filter cartridge  417  has a specific porosity that is determined by the number of “wraps” of filter membrane  413  within the membrane filter cartridge  417 . Application of electrical current to the membrane cages  411 ,  412  also creates a magnetic field between the membrane cages  411 ,  412  that passes through the membrane filter  413  to exert ionic forces on charged molecules and/or charged particles/contaminants within the fluid. The magnetic fields tend to “drive” the charged particles/contaminants and/or molecules toward or away from one of the membrane cages  411 ,  412 . Because each step-down membrane filter body  401  only separates/removes specific size contaminants and/or particulates from the fluid, the separated contaminants and/or particulates are finely gradiated by size and may be commercialized. Sensors, samplers and monitors continuously monitor, sample and test fluid pressures, fluid flow and head pressure within each step-down membrane filter body  401  for when the fluid pressures, head pressure and/or fluid flow reaches a predetermined level which is indicative of the membrane filter canisters  417  becoming plugged, clogged and/or saturated with contaminants and/or particulates. Upon such determination, valve  430  is activated and the fluid flow from the particulate filter  300  is directed into the parallel second step-down membrane filter  400 B for filtration and treatment of the fluid to continue uninterrupted. While the fluid from the particulate filter  300  is flowing into and through the parallel second step-down membrane filter  400 B, valves communicating with each of the first step-down membrane filter  400 A bodies  401  are activated allowing clean fluid, which may be water, to flow into and through each of the first step-down membrane filter  400 A bodies  401  in a reverse direction, known as backwashing  75 , which forces accumulated contaminants, particulates and the like out of the membrane filter canisters  417  in a reverse direction where the accumulated contaminants and particulates are directed into the collection body  435 . Concurrently with the backwash  75 , the polarity of the electrical current applied to the membrane filter cages  411 ,  412  is reversed to exert ionic forces on the charged particles and/or contaminants which will assist in cleaning the membrane filter cartridges  417 . Each of the step-down membrane filter bodies  401  fluidically communicates separately with the collection body  435  which receives the backwash fluids and backwashed contaminants and/or particulates during the backwash  75  operation. It is anticipated the backwash operation  75  will take approximately three minutes and such process is not harmful or damaging to the membrane filters  413 . Gradiated and/or sized contaminants and/or particulates collected within the collection body  435  may be collected, removed and sold if desired. Non-useful contaminants and/or particulates may be passed to the waste tank  250  or otherwise removed for proper disposal. When the sensors, samplers and monitors detect that the second parallel step-down membrane filter  400 B is becoming plugged, clogged and/or saturated valve  430  is activated and fluid flow is directed back through the first step-down membrane filter  400 A while the parallel second step-down membrane filter  400 B is backwashed  75  providing uninterrupted operation and filtration of the fluid and collection of the finely gradiated contaminants and/or particulates in the collection body  435 . 
     If the fluid outflow from the step-down membrane filter  400  meets or exceeds desired standards and/or quality and/or purity measurements, the fluid outflow may be directed to the mixing station  700  by valve  530 . If the desired standards and/or quality and/or purity of the fluid outflow does not meet or exceed desired standards, for example contaminants and/or particulates having a diameter down to approximately 6 microns still need to be removed, valve  530  may direct the fluid outflow to the ultra filtration system  500 . 
     Fluid entering the first ultra filtration manifold  500 A passes into and through a series of filter cartridges  503  carried within screw on filter canisters  502  that fluidically communicate with the ultra filtration manifold  500 A. Because the ultra filtration cartridges  503  are preferably formed of paper, the ultra filtration cartridges  503  are not amenable to backwashing  75  which has the tendency to damage the paper filter cartridges  503 . Instead, when the sensors, samplers and monitors determine and indicate the pressures, head pressures and/or fluid flow through the ultra filtration manifold  500 A reaches a predetermined level, valve  530  is activated to direct the fluid flow through the parallel second ultra filtration manifold  500 B while the paper ultra filtration cartridges  503  of the first ultra filtration manifold  500 A are removed and replaced. Similarly, when the sensors, samplers and monitors determine and indicate the pressures, head pressures and/or fluid flow through the ultra filtration manifold  500 B reaches a predetermined level, valve  530  is activated to direct the fluid flow back through the first ultra filtration manifold  500 A for continuous operation. 
     If the fluid outflow from the ultra filtration manifolds  500 A,  500 B meets or exceeds desired standards and/or quality and/or purity measurements, the fluid outflow may be directed to the mixing station  700  by valve  531 . If the desired standards and/or quality and/or purity of the outflow does not meet or exceed desired standards, for example dissolved salts still need to be removed from the fluid, valve  531  may direct the fluid outflow to the reverse osmosis system  600  where the fluid is forced under high pressures, generated by fluid pumps (not shown), though a plurality of Poly-Pan filter membranes  606  where dissolved salts are removed from the fluid. Fluid exiting the reverse osmosis filter  600  passes to the mixing station  700 . 
     Fluid entering the mixing station  700  is tested, monitored, sampled and analyzed, preferably automatically by automatic testing, sampling, analysis and measuring systems and apparatus to sample, determine and measure contaminant levels and the like to determine whether the fluid meets and/or exceeds the desired necessary standards for quality, safety, purity, and the like. If additional chemical treatment is required additional chemical additives such as pH buffers and the like may be added, automatically or manually at the mixing station  700 . Fluid exiting the mixing station  700  passes to the totalizer and sensor array  900  for final analysis, sampling, testing and measuring to determine the volume of fluid exiting the system. The volume of fluid passing through the system, as determined by the totalizer  900  may be compared against the volume of fluid entering the system as measured by the volume meter  99  to determine system efficiency and pricing for fluid treatment which may be invoiced/billed to a user/operator. Treated and clean fluid exiting the system may be stored for future use or plumbed to a destination for immediate use. 
     The above description has set out various features, functions, methods and other aspects of my invention. This has been done with regard to the currently preferred embodiments thereof. Time and further development may change the manner in which the various aspects are implemented. 
     The scope of protection accorded the inventions as defined by the claims is not intended to be limited to the specific sizes, shapes, features or other aspects of the currently preferred embodiments shown and described. The claimed inventions may be implemented or embodied in other forms while still being within the concepts shown, described and claimed herein. Also included are equivalents of the inventions which can be made without departing from the scope of concepts properly protected hereby. 
     Having thusly described and disclosed a SYSTEM FOR SEPARATING CONTAMINATES FROM WATER, I file this INTERNATIONAL PATENT APPLICATION UNDER THE PATENT COOPERATION TREATY.