Abstract:
Disclosed is an improved water treatment process that operates on a continuous flow of fluids that are subjected to hydrodynamic waves, acoustic ultrasonic waves in combination with injected ozone and electro chemical treatment. The treatment system provides a cost efficient and environmentally friendly process and apparatus for cleaning and recycling fluids as contaminated as frac water, used to stimulate gas production from shale formations, as well as other types of fluids having various levels of contaminants such as aerobic and anaerobic bacteria and suspended solids. The calcium carbonate scaling tendency is reduced to an acceptable level without the use of acids, ion exchange materials, or anti scaling chemicals which is of economical and environmental significance and benefit.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     This application is related to U.S. patent application Ser. No. 13/450,172, entitled “Apparatus for Treating Fluids”, filed on Apr. 18, 2012. In addition, this application is a continuation-in-part U.S. patent application Ser. No. 13/019,113, entitled “Transportable Reactor Tank”, filed Feb. 1, 2011, which is a continuation-in-part of U.S. patent application Ser. No. 12/765,971, entitled “Improved Reactor Tank”, filed Apr. 23, 2010, which is a continuation-in-part of U.S. patent application Ser. No. 12/399,481, entitled “Enhanced Water Treatment for Reclamation of Waste Fluids and Increased Efficiency Treatment of Portable Waters”, filed Mar. 6, 2009, now U.S. Pat. No. 7,699,988, issued Apr. 20, 2010, which is a continuation-in-part of U.S. patent application Ser. No. 12/184,716, entitled “Enhanced Water Treatment for Reclamation of Waste Fluids and Increased Efficiency Treatment of Portable Waters”, filed Aug. 1, 2008, now U.S. Pat. No. 7,699,994, issued Apr. 20, 2010, which in turn is a continuation-in-part of U.S. Provisional Patent Application No. 60/953,584, entitled “Enhanced Water Treatment for Reclamation of Waste Fluids and Increased Efficiency Treatment of Portable Water”, filed Aug. 2, 2007, the contents of which are hereby expressly incorporated by reference. 
     FIELD OF THE INVENTION 
     This invention related to the field of fluid treatment and, in particular, to an improved treatment apparatus for destroying aerobic and anaerobic bacteria in fluids used in oil and gas recovery and conditioning of said fluid for reuse. 
     BACKGROUND OF THE INVENTION 
     The Applicant has worked extensively with some of the foulest waters imaginable. In many such instances the treatment of such fluids can be extremely expensive. For example, the global direct costs to oil companies for treating water used in oil and gas recovery surpassed $20 billion in 2007, with expenses skyrocketing in the following years. 
     While the instant invention can be used on most any fluid that is contaminated, it is especially suited for water contaminated with aerobic or anaerobic bacteria, or waters that benefit from the reduction in dissolved or suspended solids or conditioning thereof. Aerobic bacteria, often called a slime forming bacteria, produces a polysaccharide bio-film that often adheres to the shale and inhibits the flow of gasses. Anaerobic bacteria can be include an acid producing bacteria such as APB that grows on metal and secretes acid producing corrosion, or SRB which is a sulfate reducing bacteria that produces hydrogen sulfide and has the potential to create a dangerous situation and literally shut down a well. 
     The produced water example will highlight a major problem with contaminated water, produced waters are the byproduct associated with oil and gas production and contain both natural and manmade contaminants. The US Department of Energy (DOE) has called produced water “by far the largest single volume byproduct or waste stream associated with oil and gas production.” The DOE further terms its treatment a serious environmental concern and a significantly growing expense to oil and gas producers. While the instant cavitation reactor has a beneficial use with most any water treatment problem, the produced water problem highlights the effectiveness of the system. 
     In 2007, the world&#39;s oil and gas fields produced 80 billion barrels of water needing processing. The average is now almost nine barrels of produced water for each barrel of oil extracted. And the ratio of water to hydrocarbons increases over time as wells become older. That means less oil or gas and more contaminated water as we attempt to meet rising global energy needs. 
     The discharge of produced water is unacceptable unless treated. Currently it is necessary to introduce chemical polymers to flocculate the slurry and further treat the volatile organic compounds (VOC&#39;s) that are emitted as gases from certain solids or liquids. The VOC&#39;s are known to include a variety of chemicals some of which may have short or long term adverse health effects and is considered an unacceptable environmental discharge contaminant. Unfortunately, the use of polymers and a settling time is so expensive that economically it becomes more conducive to treat the waste off-site that further adds to the cost of production by requiring off-site transport/treatment or shipped to a hazardous waste facility where no treatment is performed. 
     The applicants have developed an enhanced water treatment system that employs the use of a cavitation reactor. The instant invention advances the developed processes of oxidizing heavy metals, converting oil sheens to inert CO 2  and water, precipitating certain cations or conditioning thereof, and oxidizing organics at a well site. Further, the system may treat numerous other fluid related problems providing both an economic and environmental benefit. 
     There are many gas fields, most notably in North America, that contain enormous amounts of natural gas. This gas is trapped in shale formations that require stimulating the well using a process known as fracturing or fracing. The fracing process uses large amounts of water and large amounts of particulate fracing material (frac sands) to enable extraction of the gas from the shale formations. After the well site has been stimulated, the water pumped into the well during the fracing process is removed, and is referred to as flowback fluid or frac water. 
     Water is an important natural resource that needs to be conserved wherever possible. One way to conserve water is to clean and recycle this flowback or frac water. The recycling of frac water has the added benefit of reducing waste product, namely the flowback fluid, which will need to be properly disposed. On site processing equipment, at the well, is the most cost effective and environmentally friendly way of recycling this natural resource. 
     It takes from 1 million to 4.5 million gallons of fresh water to fracture a horizontal well. This water may be untreated water available from local streams, ponds, and wells or may be treated water purchased from a municipal water utility. Water is typically trucked to the well site by tanker trucks, which carry roughly five thousand gallons per trip. For instance, if approximately 300 five thousand gallon tanker trucks are used to carry away more than one million gallons of flowback water per well the amount of fuel consumed in addition to the loss of water is unacceptable. For a 3 well frac site these numbers will increase by a factor of three. 
     The present invention provides a cost-effective onsite cavitation reactor that combines ozone, hydrodynamic cavitation, acoustic cavitation and electro-precipitation for enhanced water treatment. The treatment apparatus is sized and configured to optimize the amount of water to be processed. The treatment system is compact, transportable and self-contained, including both the processing equipment and the power supply to the run the system. It is also configured to be compact in overall size to facilitate its use a remote well sites. The treatment device is also readily transportable such that it can be moved from well site to well site. 
     SUMMARY OF THE INVENTION 
     The instant invention is directed to an improved treatment apparatus that introduces high intensity acoustic energy and ozone into a conditioning container to provide a mechanical separation of materials by addressing the non-covalent forces of particles or van der Waals force. The invention further discloses hydrodynamic cavitation of the ozone and effluent prior to entry into the treatment apparatus to improve to improve the mixture of effluent with ozone. The ultrasound transducers used to provide the acoustic energy strategically located within the treatment apparatus to accelerate mass transfer as well as electrodes to break down contaminants at a faster rate. 
     Thus an objective of the invention is to provide a high capacity compact and improved cavitation reactor to treat fluids, the fluids are subjected to ozone saturation and flash mixed with hydrodynamic cavitation and ultrasonic transducers or varying frequencies to initiate flotation of oils and suspended solids and the conversion of ozone to hydroxyl radicals. 
     Yet still another objective of the invention is to disclose the use of a cavitation reactor that can be used in treatment of most any type of fluid by providing an effective means to destroy aerobic and anaerobic bacteria “on the fly”, and provide a reduction in contaminants. 
     Still another objective of the invention is to provide an improved cavitation reactor that eliminates the need for biocide and anti-scalant chemical typically employed in frac waters. 
     Still another objective of the invention is to provide a process to reduce scaling tendencies without the aid of acid, ion exchange processes, or anti scaling chemicals. 
     Yet another objective of the invention is to a process for lowering scaling tendencies in frac, flowback water, as demonstrated by dynamic tube-blocking tests 
     Another objective of the invention is employ nano-cavitation imploding bubbles to provide the liquid gas interface that is instantaneously heated to approximately 900 degrees Fahrenheit which oxides all organic compounds through sonoluminescence. 
     Still another objective of the invention is to provide an improved cavitation reactor for an on-site process that will lower the cost of oil products by reducing the current and expensive processes used for off-site treatment of waste fluids. 
     Another objective of the invention is to provide an improved cavitation reactor for on-site process that will extend the life of fields and increase the extraction rate per well. 
     Still another objective of the instant invention is to teach the combination of ultrasonic and hydrodynamic agitation in conjunction with ozone introduction into a closed pressurized generally cylindrically shaped container whereby the cavitations cause disruption of the materials allowing the ozone to fully interact with the contaminated flow back water for enhancement of separation purposes. In addition, anodes in the outlet line provide DC current to the flowback water to drive the electro precipitation reaction for the hardness ions present with the flowback water. 
     Still another objective is to teach a process of enhanced ozone injection wherein ozone levels can be made more effective. 
     Another objective of the invention is to provide a cost effective and environmentally friendly process and apparatus for cleaning and recycling frac water at the well site using transportable equipment. 
     Other objectives and advantages of this invention will become apparent from the following description taken in conjunction with the accompanying drawings herein set forth, by way of illustration and example, certain embodiments of this invention. The drawings constitute a part of this specification and include exemplary embodiments of the present invention and illustrate various objects and features thereof. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1A  is a top view of the main reactor of the treatment system. 
         FIG. 1B  is a side view of the main reactor of the treatment system. 
         FIG. 2  is a sectional view of the main reactor taken along line A-A shown in  FIG. 1A . 
         FIG. 3  is an exploded view of the main reactor. 
         FIG. 4  is a pictorial view of the main reactor and a schematic view of the flow treatment downstream of the main reactor. 
         FIG. 5  is a perspective rear end view of the treatment system mounted on a skid. 
         FIG. 6  is a perspective front-end view of the treatment system mounted on a skid. 
         FIG. 7  is a left side view of the treatment system mounted on a skid. 
         FIG. 8  is a top view of the treatment system mounted on a skid. 
         FIG. 9A  is a perspective view of the skid mounted treatment system including the suction intake manifold and associated inlets. 
         FIG. 9B  is a perspective view of the suction intake manifold and associated inlets. 
         FIG. 9C  is a sectional view of the suction intake manifold and associated inlets. 
         FIG. 10A  is a perspective view of one of the ozone mixing arrangements including a fluid inlet pump, ozone injection device, a flash reactor, a static mixer and a discharge nozzle on the left side of the main reactor as viewed from the front. 
         FIG. 10B  is a perspective view of one of the ozone mixing arrangements including a fluid inlet pump, ozone injection device, a flash reactor, a static mixer and a discharge nozzle on the right side of the main reactor as viewed from the front. 
         FIG. 11A  is a side view of a one of the flash reactors. 
         FIG. 11B  is a perspective view of one of the flash reactors. 
         FIG. 11C  is a sectional view of one of the flash reactors taken along line A-A of  FIG. 11A . 
         FIG. 12A  is a perspective view of one of the inline static mixers. 
         FIG. 12B  is a cross sectional view of one of the static inline mixers. 
         FIG. 12C  is a detailed view of one of the holes in the inline static mixer shown in  FIG. 12A . 
         FIG. 13  is a side view of a trailer assembly including the treatment system, power generator, oxygen concentrator, ozone generator and control systems. 
         FIG. 14  is a top view of the trailer assembly shown in  FIG. 13 . 
         FIG. 15  is a rear view of the trailer assembly shown in  FIG. 13 . 
         FIG. 16  is a complete P&amp;ID (piping and instrument diagram) of the treatment system annotated with partition lines for FIGS.  17 A through  17 DD that are enlarged views for purpose of clarity. 
         FIGS. 17A ,  17 B,  17 C,  17 D,  17 E,  17 F  17 G,  17 H,  17 I,  17 J,  17 K,  17 L,  17 M,  17 N,  17 O,  17 P,  17 Q,  17 R,  17 S,  17 T,  17 U,  17 V,  17 W,  17 X,  17 Y,  17 Z,  17 AA,  17 BB,  17 CC,  17 BB,  17 CC and  17 DD are enlarged views of various sections of the treatment as partitioned in  FIG. 16 . 
     
    
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT 
       FIG. 1A  is a top view of the main reactor  1  of the treatment system and  FIG. 1B  is a side view of the main reactor  1 . The main reactor  1  includes a cylindrical housing  3  that is, by way of example, approximately 16.5 feet long and 2 feet in diameter. A circular end plate  5  is mounted on each end of the cylindrical housing  3 . Located along the length of the cylindrical housing are eighteen ultrasonic transducers  2 A, 2 B, 2 C, 2 D, 2 E, 2 F,  2 G,  2 H,  2 J, 2 K,  2 L,  2 M, 2 N,  2 P, 2 Q,  2 R and  2 S. Each of the ultrasonic transducers is rated at 500 W capacity and is also equipped with a heated plate that is rated at 1000 W. At given flow rates it maintains a ΔT of 40 degrees that enhances the precipitation within the main reactor. Each transducer can produce an acoustic output in the range of 16 to 20 KHz and can be individually adjusted to the desired output frequency. Each transducer includes a diaphragm that is balanced with the help of a pressure compensation system so that a maximum amount of ultrasonic energy is released into the fluid. The transducer assemblies are installed around the periphery of the cylindrical housing  3  creating a uniform ultrasonic environment that helps to increase the mass transfer efficiency of the ozone. The acoustic cavitations generated by the ultrasonic generators also greatly enhance the oxidation rate of organic material with ozone bubbles and ensure uniform mixing of the oxidant with the fluid. Each transducer assembly includes mounting flange that is sized to mate with a flange on the cylindrical housing  3 . A series of ten disc anodes  4 A, 4 B, 4 C, 4 D, 4 E, 4 F, 4 G, 4 H, 4 I and  4 J are positioned along the length of the cylindrical housing  3 . Each of the disc anodes located in the main reactor  1  has a surface area of approximately 50.26 square inches. The current density for these set of disc anodes are 1.5 Amps/square inch. Each circular end plate  5  supports a series of twelve insulated anode electrodes  10 A, and  10 B. The twenty four anode rods within the two sets of twelve,  10 A and  10 B, are approximately seven feet in length and each have a surface area of approximately 197.92 square inches with a current density of 0.6315 amps per square inch. The main reactor tank has eight inlets  6 A,  6 B,  6 C,  6 D,  6 E,  6 F,  6 G and  6 H positioned along the length of the cylindrical housing  3 . Also positioned at one end of the cylindrical housing  3  on the upper most side is a pair of outlets  8 A and  8 B. 
       FIG. 2  is a cross sectional view of the main reactor  1  taken along line A-A as shown in  FIG. 1A . As shown therein, cylindrical mono polar cathode screens  12 A and  12 B are each affixed to one of the circular end plates  5 . These cylindrical cathode screens are approximately eight feet in length and promote efficient migration of electrons. The cylindrical screens  12 A and  12 B are negatively charged to facilitate the precipitation of crystals to adhere to the wall of the cylindrical screens  12 A and  12 B. Each series of anode rods  10 A and  10 B are supported within the main reactor  1  by a pair of supports  16  that are each attached to the inner cylindrical wall of the main reactor  1 . Likewise, each cylindrical cathode screen,  12 A and  12 B, is support by one of the two pairs of supports  16 . Cylindrical cathode screen  12 A is electrically connected via connector  14 A and cylindrical cathode screen  12 B is electrically connected via electrical connector  14 B. 
       FIG. 3  is an exploded view of the main reactor  1  and associated components as described above in  FIGS. 1A ,  1 B and  2 . 
       FIG. 4  is a pictorial view of the main reactor  1  and a schematic view of the flow treatment downstream of the main reactor. The output of main reactor  1  is directed via outlets  8 A and  8 B, via connecting flow conduits  9 A and  9 B, to first fluid treatment conduits  20 A and  20 B, respectively. Each first fluid treatment conduit  20 A and  20 B has an inner diameter of approximately ten inches and is approximately seventeen feet in length. Positioned within the first treatment conduits are a plurality of fixed static mixers that are positioned along the entire length of the conduits  20 A and  20 B. Static mixers  30  are a series of geometric mixing elements fixed within the conduit and create hydrodynamic cavitation within treatment conduits  20 A and  20 B. Each of the geometric mixing elements includes multiple orifices which uses the energy of the flow stream to create mixing between two or more fluids/gases. The optimized design of static mixers achieves the greatest amount of mixing with the lowest pressure loss possible. The static mixers  30  are described in more detailed in  FIGS. 12A through 12C  herein below. Each of the first fluid treatment conduits  20 A and  20 B includes four separate disc anodes  21 A and  21 B, respectively. The disc anodes  21 A and  21 B help to facilitate the production of hydroxyl radicals. The flow exiting first fluid treatment conduits  20 A and  20 B are then directed to second fluid treatment conduits  22 A and  22 B, respectively. Second fluid treatment conduits  22 A and  22 B have an internal diameter of approximately ten inches and are approximately seventeen feet in length. Similar to the first fluid treatment conduits, second fluid treatment conduits  22 A and  22 B each have static mixers  30 , creating hydrodynamic cavitation, and four disc anodes  23 A and  23 B, respectively. As in the first treatment conduits, the disc anodes  23 A and  23 B help to facilitate the production of hydroxyl radicals. The flow exiting second treatment conduits  22 A and  22 B are directed into third treatment conduits  24 A and  24 B, respectively. The third treatment conduits  24 A and  24 B have an internal diameter of approximately ten inches and are approximately seventeen feet in length. The third treatment conduits  24 A and  24 B each have static mixers  30  throughout their length, thereby creating hydrodynamic cavitations. The flow exiting the third treatment conduits  24 A and  24 B is directed to outlets  26 A and  26 B, respectively. 
       FIG. 5  is a perspective rear end view of the treatment system mounted on a skid  41 . By mounting the treatment system on a skid platform the equipment can be readily removed and repaired or replaced and then reinstalled into the mobile trailer unit as will be described later. As shown, the fluid treatment apparatus includes two inlets  40 A and  40 B. One side of the apparatus includes four suction pumps  42 A,  42 B,  42 C and  42 D. Each suction pump  42 A,  42 B,  42 C and  42 D fluidly connects the inlet pipe  40 B to an ozone injection apparatus which is described and illustrated in  FIGS. 10A and 10B . The treatment apparatus also includes two separate outlets  26 A and  26 B. As shown in this view, one end of the main reactor  1  has electrodes  10 A mounted on a circular end plate  5 . Connecting flow conduit  9 B fluidly connecting main reactor  1  outlet  8 B to first treatment conduit  20 B. First fluid treatment conduit  20 B is in turn fluidly connected to second fluid treatment conduit  22 B. Second fluid treatment conduit  22 B is fluidly connected via connecting flow conduit  25 B to third fluid treatment conduit  24 B. The fluid exits the third fluid treatment conduit  24 B via an outlet  40 B. 
       FIG. 6  is a perspective front-end view of the treatment system mounted on a skid. This view is a side view opposite to that shown in  FIG. 5 . As illustrated, this side of the treatment apparatus shows three suction pumps  44 A,  44 B, and  44 C. It should be understood that it is possible to install a fourth pump (not shown) on this side as well as was shown in  FIG. 5 . Typically the reactor is configured with seven inlets and associated pumps and ozone injectors and operated with six of the inlets with one inlet held in reserve for use as needed. It should be noted that the system can be configured with up to eight inlets wherein all eight can be simultaneously operated. Each pump, either three or four in number, fluidly communicates with intake pipe  40 A on the intake side of each pump and an ozone injection apparatus on the outlet side of the pump. The flow leaving main reactor  1  passes through connecting flow conduit  9 B and into first treatment flow conduit  20 A that in turn is communicated to second fluid treatment conduit  22 A. The flow leaving second fluid treatment conduit  22 A then passes through connecting flow conduit  25 B and into third fluid treatment conduit  24 B. The fluid exits the third fluid treatment conduit  24 A via an outlet  26 A. 
       FIG. 7  is a left side view of the treatment system mounted on a skid  41 . This view shows suction pumps  42 A,  42 B,  42 C and  42 D each drawing fluid from intake conduit  40 B and outputting the flow to an ozone injection apparatus which in turn conveys the fluid to the main reactor housing  1 . Also shown in this view is connecting flow conduit  9 B that connects outlet  8 B with first fluid treatment conduit  20 B. Also shown in this view is second fluid treatment conduit  22 B that is fluidly connected to the third fluid treatment conduit  24 B via connecting flow conduit  25 B. The third fluid treatment conduit is connected to outlet  26 B. 
       FIG. 8  is a top view of the treatment system mounted on the skid  41 . As seen in the figure the first treatment conduit  20 A contains four disc anodes  21 A and first treatment conduit  20 B also contains four disc anodes  21 B. In a similar fashion the second treatment conduit  22 A contains four disc anodes  23 A and the other second treatment conduit  22 B contains four disc anodes  23 B. Connecting flow conduit  25 A fluidly connects second treatment conduit  22 A to the third treatment conduit  24 A and the other connecting flow conduit  25 B connects the second treatment conduit  22 B to the third treatment conduit. 
       FIG. 9A  is a perspective view of the skid mounted treatment system including the suction intake manifold and associated inlets. The suction intake manifold in mounted below the skid  41 . As shown in  FIG. 9B  the suction manifold  50  includes four inlets  52 ,  54 ,  56 , and  58 . At the end of the suction manifold  50  is a suction box  60 . As shown in  FIG. 9C  the suction box  60  includes a mesh screen  62  with 0.5-inch apertures to arrest debris and particulates greater than 0.5 inches in size. The suction box  60  and mesh screen  62  can be accessed from the rear end of the box  60 . The suction manifold  50  is constructed with hydrodynamic static mixer vanes  64  positioned within the manifold between the inlets  52  and  56  and the suction box  60 . The construction of these static-mixing devices is described in  FIGS. 12A through 12C  to follow. Static mixer vanes encourage the homogeneous mixing of the fluid before entering the main reactor  1 . As will be described, the holes formed within the mixing vanes acts as orifices and allow varying pressure at multiple locations. The local pressure drops in flow through the manifold produces cavitations bubbles. These cavitation bubbles collapse as the pressure is again raised. The collapse of the cavitation bubbles produces oxidation of organic substances in the fluid. The suction manifold  50  has two outlets  66 A and  66 B. Outlets  66 A and  66 B are sized and configured to mate up with inlet conduits  40 A and  40 B, respectively. 
       FIG. 10A  is a perspective view of one of the ozone mixing arrangements on the left side of the main reactor as viewed from the front and  FIG. 10B  is a perspective view of one of the ozone mixing arrangements on the right side of the main reactor as viewed from the front.  FIG. 10A  shows one of the pumps  42 A,  42 B,  42 C or  42 D mechanically connected to an electric motor  70 . The pump has an inlet  71  that draws in fluid from the inlet conduit  40 B.  FIG. 10B  shows one of the pumps  44 A,  44 B or  44 C mechanically connected to an electric motor  70 . Downstream of the pump is a venturi type-mixing device  72  to inject ozone into the fluid flow. By way of example this can be a Mazzie® injector. The venturi type injector has an ozone inlet  73 . An air compressor feeds an oxygen generator that in turn feeds an ozone generator. The output of the ozone generator is then automatically metered into each of the venturi type mixing devices as is shown in FIGS.  17 A through  17 DD. The pressure drop across the venturi is controlled by an automated bypass valve  74  using a PID control loop. Downstream of the venturi type injector is a flash reactor  76 . The flash reactor  76  uses pressure velocity to create turbulence. Higher cavitation energy dissipation is observed in the flash reactor  76 . The turbulence in the reactor  76  creates high shear making the ozone gas bubbles smaller thereby creating a higher mass transfer efficiency. The flash reactor is described in  FIGS. 11A-11C  described below. Downstream of the flash reactor  76  is an inline static mixer  78  formed from a series of static blades with apertures, as will be described in  FIGS. 12A through 12C , positioned within a 4-inch conduit. The static mixer  78  creates hydrodynamic cavitation and produces cavitation bubbles locally at the orifices of the vanes. As these cavitation bubbles implode within the high-pressure area, energy is released in the fluid in the form of heat, light, and mechanical vibration thereby destroying/degrading the organic contaminants. Located downstream of the in line static mixer  78  is a converging discharge nozzle  80 . The conduit supporting the discharge nozzle  80  is fluidly sealed to the main reactor  1  and the nozzle itself is positioned within the main reactor. By way of example only, the converging discharge nozzle can be a Mazzie® nozzle N 45 . The discharge nozzle is used to increase the velocity of the fluid entering the main reactor that means a higher Reynolds Number and hence higher turbulence energy dissipation. The converging nozzle  80  enhances the systems performance with the venturi type injector  72 . The converging discharge nozzle  80  provides a desired backpressure on the venturi type injector  72  and, the dynamic mixing under pressure results in greater mass transfer of the ozone into the fluid and permits a larger dosage of ozone to enter the fluid. 
       FIG. 11A  is a side view of a one of the flash reactors,  FIG. 11B  is a perspective view of one of the flash reactors and  FIG. 11C  is a sectional view of one of the flash reactors taken along line A-A of  FIG. 11A . Flash reactor  76  is formed as a generally cylindrical housing and has in inlet conduit  82  that is smaller in diameter than outlet conduit  88 . Within the flash reactor housing  76  the inlet conduit  82  is fluidly connected to a slightly curved section of conduit  83  having a reduced portion  84 . Also within the flash reactor  76  is a curved section of conduit  86  that is fluidly connected to outlet conduit  88 . The direction of curvature of conduit section  83  is opposite to that of curved conduit  86 . As the flow of fluid that has been mixed with ozone is passed through the flash reactor  76  the sizes of gas bubbles are reduced to nano size by high shear. The uni-directional and shearing design of the gas/liquid water mixture allows for a rapid dissolution and attainment of gas/liquid equilibrium that results in high mass transfer efficiency with a minimal time. Due to the configuration of the flow paths within the flash reactor  76  there are different areas within the flash reactor where severe velocity and pressure changes take place. These drastic velocity and pressure changes create high shear that reduces the size of the ozone/oxygen bubbles to nano size and also dissolving more gas into the fluid that is under pressure. 
       FIG. 12A  is a perspective view and  FIG. 12B  is a cross sectional view of one of the static inline mixers.  FIG. 12C  is a detailed view of one of the holes in the inline static mixer shown in  FIG. 12A . The inline static mixers  30  in  FIG. 4  are approximately 10 inches in diameter and are positioned adjacent to one another within the fluid treatment conduits  20 A,  22 A,  24 A,  20 B,  22 B and  24 B. The inline static mixers  64  are positioned adjacent one another within intake manifold  50 , as shown in  FIG. 9C , and are approximately 16 inches in diameter. The incline static mixers  78  are positioned adjacent one another as shown in  FIGS. 10A and 10B  and are approximately 4 inches in diameter. The views shown in  FIGS. 12A through 12C  are illustrative of the inline mixers  30 , being approximately ten inches diameter. The inline static mixers  64  and  78  are of similar construction to mixer  30  except that the four-inch mixer  78  has fewer holes per baffle  96  than mixer  30  and the 16-inch inline mixer  78  has more holes per baffle  96  than the mixer  30 . The holes  90  formed on each of the baffles  96  of the inline static mixers  30 ,  64  and  78  are formed as diverging nozzles having an inlet aperture  92  on the upstream side having a diameter that is smaller than the diameter of the outlet aperture  94  on the downstream side of the blade. The inlet aperture and outlet aperture are connected by a conically shaped bore  94 , as shown in  FIG. 12C . Static mixers  30 ,  64  and  78  are each formed as a series of geometric elements fixed within a conduit wherein each of the baffles  96  of the static mixing elements contains a plurality of holes  90  are formed as diverging nozzles. The static mixers use the energy of the flow stream to create mixing between two or more fluids. The static mixers are designed to achieve the greatest amount of mixing with the lowest possible pressure loss. 
     The multiple holes in each of the baffles of the static mixers act as localized orifices, dropping the pressure of the fluid locally allowing the formation of cavitation bubbles. As these cavitation bubbles are carried away with the flow, these bubbles collapse or implode in the zone of higher pressure. The collapse of the cavitation bubbles at multiple locations within the treatment system produces localized high-energy conditions such as shear, high pressure, heat light, mechanical vibration, etc. These localized high-energy conditions facilitate the breakdown of organic substances. The baffles are arranged so that when the fluid is discharged from one baffle, it discharges with a swirling action and then strikes the downstream baffle. The baffles provide a local contraction of the flow as the fluid flow confronts the baffle element thus increasing the fluid flow pressure. As the fluid flow passes the baffle, the fluid flow enters a zone of decreased pressure downstream of the baffle element thereby creating a hydrodynamic cavitation field. Hydrodynamic cavitation typically takes place by the flow of a liquid under controlled conditions through various geometries. The phenomenon consists in the formation of hollow spaces which are filled with a vapor gas mixture in the interior of a fast flowing liquid or at peripheral regions of a fixed body which is difficult for the fluid to flow around and the result is a local pressure drop caused by the liquid movement. At a particular velocity the pressure may fall below the vapor pressure of the liquid being pumped, thus causing partial vaporization of the cavitating fluid. With the reduction of pressure there is liberation of the gases that are dissolved in the cavitating liquid. These gas bubbles also oscillate and then give rise to the pressure and temperature pulses. The mixing action is based on a large number of forces originating from the collapsing or implosions of cavitation bubbles. If during the process of movement of the fluid the pressure at some point decreases to a magnitude under which the fluid reaches a boiling point for this pressure, then a great number of vapor filled cavities and bubbles are formed. Insofar as the vapor filled bubbles and cavities move together with the fluid flow, these bubbles move into an elevated pressure zone. Where these bubbles and cavities enter a zone having increased pressure, vapor condensation takes place within the cavities and bubbles, almost instantaneously, causing the cavities and bubbles to collapse, creating very large pressure impulses. The magnitude of the pressure impulses with the collapsing cavities and bubbles may reach ultra high pressure implosions leading to the formation of shock waves that emanate form the point of each collapsed bubble. 
       FIG. 13  is a side view of a trailer assembly  100  containing the treatment system. The complete system is packaged in a mobile trailer that is approximately 53 feet in length. At the forward end of the trailer assembly  100  is a 600 KW generator set  102  powered by a diesel engine. The system is capable of a flexible flow rate of 20-70 barrels per minute. It is capable of producing 2520 gal/minute flow rate with a supply water pressure within the range of 10-40 psi. It is also capable of handling a fluid input having a salinity range of 50-200,000 PPM. A plurality of oxygen concentrators  104  are mounted on a vertical wall within the trailer assembly  100 . Also shown in  FIG. 13  are an ozone panel  106  and a cooling water chiller  108 . Visible from this side view are inlets  58 ,  56  and inlet conduit  40 A. Also shown in  FIG. 13  is main reactor  1 , one of the first treatment conduits  20 A, as well as connecting flow conduits  9 A,  25 A and one of the third fluid treatment conduits  24 A. The fluid treatment system is mounted on a skid  41  for ease of removal, repair or replacement, and subsequent reinstallation through rear access of the trailer. The ability to swap out system component modules substantially minimizes system down time and improves the ability to repair the processing equipment in a quick and efficient manner. The main reactor  1  is approximately 16 feet in length. 
       FIG. 14  is a top view of the trailer assembly shown in  FIG. 13 . This view of the trailer assembly  100  show the 600 KW generator set  102 , the oxygen concentrators  104 , the ozone panel  106  and the cooling water chiller  108 . In addition, this view also shows air pumps  110 , main panel  112 , a DC power supply (e.g. 252 KW) to power the treatment system and power distribution panel  116 . The trailer assembly  100  also includes two side access doors  118  and  120 . 
       FIG. 15  is a rear view of the trailer assembly  100  with the rear access open. As shown the treatment apparatus is supported on skid  41 . Side doors  118  and  120  are shown in an open position. 
       FIG. 16  is a complete P&amp;ID (piping and instrument diagram) of the treatment system annotated with partition lines for FIGS.  17 A through  17 DD which are enlarged views to provide clarity.  FIGS. 17A ,  17 B,  17 C,  17 D,  17 E,  17 F  17 G,  17 H,  17 I,  17 J,  17 K,  17 L,  17 M,  17 N,  17 O,  17 P,  17 Q,  17 R,  17 S,  17 T,  17 U,  17 V,  17 W,  17 X,  17 Y,  17 Z,  17 AA,  17 BB,  17 CC,  17 BB,  17 CC and  17 DD are enlarged views of various sections of the treatment as partitioned in  FIG. 16 . 
     The theory of operation behind the main treatment is as follows. The mass transfer of ozone in the water is achieved by hydrodynamic and acoustic cavitations. In the pressurized reactor tank  1 , water that has been ozonated is introduced into through seven separate discharge nozzles  80 . Initially the water to be treated is pressurized by six of the seven pumps each of which in turn feeds an ozone injector  72 . The ozonated fluid is then introduced into a flash reactor  76  that is used to reduce the size of the ozone bubbles to enhance the gas mass transfer efficiency. The ozonated fluid is then introduced into a hydrodynamic mixing manifold  78 . The discharge nozzles  80  direct the flow against the inner wall of cylindrical housing  3  of the main reactor  1 . The phenomenon of hydrodynamic cavitations is created as the pressurized water leaves the small orifices within the hydrodynamic mixing manifold  78 . The dissolved ozone forms into millions of micro bubbles that are mixed and reacted with the incoming water. As the water flows through the main reactor  1  the ultrasonic transducers located around the periphery of the main reactor emit ultrasonic waves in the range of 16 KHz and 20 KHz into the flow of water. The main reactor  1  also includes a plurality of disc anodes, 10 in number by way of example, located about the circumference of the main reactor  1 . In addition, there are two groups of anode electrodes  10 A and  10 B that extend longitudinally into the main reactor  1  from the end plates  5  of the main reactor. Each group of the anode electrodes  10 A and  10 B consists of twelve rods approximately seven feet in length. The main reactor  1  also includes a pair of cylindrical cathode screens  12 A and  12 B that likewise extend longitudinally into the main reactor  1  from the end plates  5  to electro chemically treat the fluid with the main reactor. 
     A sonoluminescence effect is observed due to acoustic cavitation as these ultrasonic waves propagate in the water and catch the micro bubbles in the valley of the wave. Sonoluminescence occurs whenever a sound wave of sufficient intensity induces a gaseous cavity within a liquid to quickly collapse. This cavity may take the form of a pre-existing bubble, or may be generated through hydrodynamic and acoustic cavitation. Sonoluminescence can be made to be stable, so that a single bubble will expand and collapse over and over again in a periodic fashion, emitting a burst of light each time it collapses. The frequencies of resonance depend on the shape and size of the container in which the bubble is contained. The light flashes from the bubbles are extremely short, between 35 and few hundred picoseconds long, with peak intensities of the order of 1-10 mW. The bubbles are very small when they emit light, about 1 micrometer in diameter depending on the ambient fluid, such as water, and the gas content of the bubble. Single bubble sonoluminescence pulses can have very stable periods and positions. In fact, the frequency of light flashes can be more stable than the rated frequency stability of the oscillator making the sound waves driving them. However, the stability analysis of the bubble shows that the bubble itself undergoes significant geometric instabilities, due to, for example, the Bjerknes forces and the Rayleigh-Taylor instabilities. The wavelength of emitted light is very short; the spectrum can reach into the ultraviolet. Light of shorter wavelength has higher energy, and the measured spectrum of emitted light seems to indicate a temperature in the bubble of at least 20,000 Kelvin, up to a possible temperature in excess of one mega Kelvin. The veracity of these estimates is hindered by the fact that water, for example, absorbs nearly all wavelengths below 200 nm. This has led to differing estimates on the temperature in the bubble, since they are extrapolated from the emission spectra taken during collapse, or estimated using a modified Rayleigh-Plesset equation. During bubble collapse, the inertia of the surrounding water causes high speed and high pressure, reaching around 10,000 K in the interior of the bubble, causing ionization of a small fraction of the noble gas present. The amount ionized is small enough fir the bubble to remain transparent, allowing volume emission; surface emission would produce more intense light of longer duration, dependent on wavelength, contradicting experimental results. Electrons from ionized atoms interact mainly with neutral atoms causing thermal bremsstrahlung radiation. As the ultrasonic waves hit a low energy trough, the pressure drops, allowing electrons to recombine with atoms, and light emission to cease due to this lack of free electrons. This makes for a 160 picosecond light pulse for argon, as even a small drop in temperature causes a large drop in ionization, due to the large ionization energy relative to the photon energy. 
     It is to be understood that while certain forms of the invention is illustrated, it is not to be limited to the specific form or process herein described and shown. It will be apparent to those skilled in the art that various changes may be made without departing from the scope of the invention and the invention is not to be considered limited to what is shown and described in the specification and drawings.