Patent Publication Number: US-2013233809-A1

Title: Water treatment system and method

Description:
FIELD OF THE INVENTION 
     The present invention relates to the treatment of water and, more particularly, to a system and method for taking liquid from inside a wastewater treatment plant or other treatment process and supersaturating the liquid with oxygen or another gas, and then re-injecting that supersaturated liquid back into the portion of the plant or process where a specified Biochemical Oxygen Demand (“BOD”) or Chemical Oxygen Demand (“COD”) reduction is required or where Dissolved Oxygen (“DO”) levels need to meet certain operational, regulatory or permit limits. 
     BACKGROUND OF THE INVENTION 
     Wastewater treatment is the process of removing contaminants from wastewater and raw sewage, involving effluents from runoff, domestic, commercial or industrial waste. Treatment involves using physical, chemical and biological processes to remove physical, chemical and biological contaminants. The primary objective of any wastewater process is to produce an environmentally safe, fluid waste stream and a solid waste that is suitable for disposal or reuse or return to the natural environment in a benign form acceptable to applicable regulations. 
     Wastewater treatment and water system treatment are referred to collectively, where appropriate, as a “Water System.” 
     Water system treatment is the process of removing contaminants from natural and manmade sources of water, including streams, rivers, lakes, ponds, lagoons, wells and any other body or source of water that may or may not involve a dedicated plant and may be performed in situ or under existing conditions. 
     A typical wastewater treatment process involves two or three stages: primary, secondary and tertiary treatment. Primary treatment involves removing solids from the wastewater stream by using screens, bars and/or holding the sewage in a quiescent basin such as a grit chamber, where heavy solids can settle to the bottom while oil, grease and lighter solids float to the surface. The settled and floating material can be separated and removed and the remaining liquid may be discharged or subjected to further treatment. 
     Secondary treatment is typically performed by indigenous, water-borne micro-organisms in a managed habitat, such as an aeration basin followed by a settlement process, like that performed by a clarifier, to separate and remove solids. Secondary treatment usually involves a separation process to remove the micro-organisms from the treated water prior to discharge or tertiary treatment. The remaining treated wastewater can then be disinfected and discharged into the environment in streams, rivers, or used for groundwater recharge or agricultural irrigation. The solids are usually retained for further biological breakdown and then disposal, at this stage, unless the plant has tertiary treatment or is required to meet additional discharge limits that require supplemental treatment. 
     Tertiary treatment is an additional supplement treatment or combination of treatments and processes to allow plant effluent to meet more stringent discharge requirements. Tertiary treatment is usually site specific and typically focuses on removing additional specific constituents in the wastewater stream, such as nitrogen, phosphorus, etc. Similar to secondary treatment, the effluent is disinfected to substantially reduce the number or micro-organisms so the effluent can be used for drinking, bathing, irrigation and the like, which is typically done in a chlorine contact chamber. 
     One of most common types of secondary treatment processes called activated sludge, uses aerobic bacteria in the presence of oxygen, so that the bacteria can oxidize carbonaceous (biological) matter, nitrogenous matter, chemical matter, remove phosphate, drive off entrained gases, generate a biological floc that facilitates settlement of suspended solids and generate a liquor that is low in dissolved or suspended material (“Aerobic Processing”). Although this type of treatment can be very effective, it is relatively expensive because of the significant amount of power required to operate the blowers that supply air into the aeration basins, and associated pumps and motors, all of which are required to supply oxygen to the process. Air diffuser systems or jet aerators that inject air bubbles into the basin have been used on a limited basis to reduce costs. 
     In general there has been an industry focus on trying to find innovative ways to reduce the size of the bubbles of air to increase the effective area of the water-bubble interface and improve the effective rate that oxygen is made available to the process. Diffusers that diffuse the air or jet injection nozzles all focus on different ways to inject various size air bubbles into the process. Coarse bubble diffusers are less efficient than fine bubble diffusers, but they have fewer operational problems, such as clogging that frequently plague fine bubble diffusers due to their small holes inside the aeration basin. 
     The key consideration for selecting a diffuser is to make sure it will produce the required oxygen transfer rate to achieve the desired level of dissolved oxygen (DO) in the fluid in the basin. Most of these applications also rely on using ambient air for the source of oxygen, which contains approximately 20.9% oxygen. The result is that a great of energy is wasted moving 79% of the volume of air that provides little or no benefit to the aerobic process. 
     Thus, there is a need for a more cost efficient way to introduce oxygen in the secondary treatment stage of a wastewater treatment system, and in other water treatment processes. There is also a need for a more effective way of achieving and maintaining an optimum level of dissolved oxygen in the treatment fluid for removing organic matter from wastewater. 
     The owner of the inventions described herein is the assignee of U.S. Pat. Nos. 7,048,786; 7,270,314; 7,491,340 and 7,544,323, the entire content of which are incorporated herein by reference as though fully described. These patents disclose an apparatus and method for treating a fluid to produce a high nano-sized oxygen particle concentration and a low surface tension stream. The device in the patents flows a fluid into a surface tension modification generator (STMG) at a first pressure. An energy wave or an electromagnetic wave is applied to the fluid, and the wave travels along the fluid for a defined distance to modify a physical characteristic of the fluid, forming an altered fluid. The use of an STMG or the like to super-oxygenate a liquid is referred to below as the “Process.” 
     After the altered fluid is formed, the Process includes flowing oxygen or ozone or another gas into the altered fluid forming an altered fluid mixture. Then, the altered mixture is flowed into the inner chamber of a multi-chamber device at a second pressure, which is lower than the first pressure. The altered fluid mixture is then passed from the inner chamber through a plurality of funnels forming a turbid fluid condition at a focus point in an outside chamber to dissolve nano-sized oxygen particles into the fluid at an increased concentration, thereby forming supersaturated oxygenated water. 
     The above-mentioned patents describe a two-chamber atomizing carburetor for blending the gas and liquid to perform the Process. Then, in a multi-chamber device with an inner chamber with funneled openings (diffuser), the gas and liquid are fed into an outer chamber to create extreme turbulence between an inner and outer chamber to assist in creating very tiny (sub-micron) oxygen molecules, that when combined with the first two technologies further boost the mixing of the gas into the liquid. When these components create a liquid supersaturated with the gas, a relatively high volume of liquid is required relative to the gas volume (90%-10% liquid/gas ratio or greater). 
     The integrated Process for creating a supersaturated liquid described above, is not generally suitable for use in a system for wastewater treatment such as wastewater treatment plants or other types of systems such as lagoons (“Water System”) where the source water has suspended material present, without substantial adaptation to mitigate the negative effect of suspended solids and materials in the water source stream. Field testing of the technology in potential wastewater applications identified a variety of materials that impair the process including but not limited to: organic or biological material, hair, floss, rags, egg shells, grit, silt, paper, metals, small pebbles, plastic, etc. The level (volume, size, composition, etc.) of this type of material depends upon the source of the water supply within the Water System, such as the collection system that supplies wastewater to wastewater treatment plant. 
     For use in a Water System, a suitable source for the super oxygenated liquid is difficult to find because it is not economically feasible to use clean or potable water from an external source. In a wastewater treatment plant this demand could typically require up to Y2 of the plant throughput capacity. Additionally, because the liquid must have a relatively low level of suspended solids and materials in order for the Process to be effective, there is a technological and economic challenge for using the technology disclosed in the above-identified patents in Water Systems because of the high amount of total suspended solids (TSS) in the source liquid at most locations from where water can practically be drawn. 
     SUMMARY OF THE INVENTION 
     These problems have been solved in the present invention where a Water System liquid that is taken from one or more of the component parts through a device that can treat the liquid to form a supersaturated oxygenated fluid. The oxygenated fluid can then be introduced into an aeration basin or other part of a Water System where organic solids are treated with the supersaturated oxygen content liquid, that is sufficient to raise the DO in the application to a sufficient level needed or required. 
     In natural and manmade sources of water supply from the Water System, the source of the water source can vary by specific circumstances, but will usually entail the potential inclusion of matter that negatively impacts the Process unless the matter is removed before the fluid is subjected to the Process. 
     In a wastewater treatment plant, one source of the liquid could be from the grit chamber, provided that suitable screens and filters are used to reduce the TSS of the liquid before it is circulated through the Process. The preferred source for the liquid is from the aeration chamber even though filters and screens must be used to reduce the TSS because the liquid can be re-circulated in a closed loop, which reduces negative impacts on overall plant hydraulics. Alternatively, the liquid can be drawn from the clarifier or disinfectant contact chamber, which has the advantage of using liquid having a relatively low TSS even though it could negatively impact plant hydraulics and operations because of the relatively high capacity demands and degrade plant economics since this source of water has already been treated. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       Various embodiments of the invention will be explained in greater detail with reference to the appended Figures, in which: 
         FIG. 1  is a schematic diagram of the components of a representative sewage treatment plant in the prior art. 
         FIG. 2  is a schematic diagram of the components of the representative sewage treatment plant in  FIG. 1 , which includes the Process connected to receive liquid from the grit chamber to super-oxygenate the effluent, and showing the super-oxygenated liquid being introduced into the aeration basin. 
         FIG. 3  is a schematic diagram of the components of the representative sewage treatment plant in  FIG. 1 , which includes the Process connected to receive liquid from the aeration basin to super-oxygenate the liquid, and showing the super-oxygenated liquid being reintroduced into the aeration basin on a closed loop basis. 
         FIG. 4  is a schematic diagram of the components of the representative sewage treatment plant in  FIG. 1 , which includes the Process connected to receive liquid from the clarifier to super-oxygenate the liquid, and showing the super-oxygenated liquid being reintroduced into the aeration basin. 
         FIG. 5  is a schematic diagram of the components of the representative sewage treatment plant in  FIG. 1 , which includes the Process connected to receive liquid discharged from the last stage of the system, to super-oxygenate the liquid, and showing the super-oxygenated water being introduced into the aeration basin. 
         FIG. 6  is a schematic diagram of the components of a representative natural or manmade Water System, which includes the Process connected to receive liquid from one or more water sources, to super-oxygenate the liquid, and showing the super oxygenated liquid being reintroduced into the Water System. 
     
    
    
     DETAILED DESCRIPTION OF EMBODIMENTS 
     Before reviewing embodiments of the invention in detail, it is to be understood that the invention is not limited to the particular embodiments herein and it can be practiced or carried out in various ways. 
     The invention relates to Water Systems, processes and plants, in which super-oxygenated liquid is introduced for treating organic and chemical material in the system process or plant. One application for the invention is in a wastewater treatment plant of the type shown in  FIG. 1 . In such a wastewater treatment plan, where sewage (domestic, commercial or industrial) to be treated is introduced, as represented by arrow  5 , into the primary stage  10  after initial screening for removing large objects in a well known way. The primary stage  10  typically includes a quiescent basin such as a grit chamber  12  for holding raw sewage so that heavier solids can settle to the bottom while oil, grease and lighter solids can float to the surface. After the settled and floating material is removed, the remaining liquid may be discharged as shown by arrow  14 . 
     A secondary treatment stage  16 , which for the present invention is performed by removing indigenous, water-borne organic material in the form micro-organisms in a managed habitat, such as an aeration basin  18 . The secondary treatment for the present invention involves a separation process to remove the micro-organisms from the treated water prior to settlement in a clarifier and then discharge for either disinfection and discharge to the local environment or subsequent tertiary treatment, illustrated by the arrow  20 . 
     The tertiary treatment stage  22  performs additional treatment so the effluent is clean enough to meet higher quality discharge requirements. Tertiary treatment can be performed using a variety of techniques depending upon the treatment objectives. The effluent is also disinfected to substantially reduce the number of micro-organisms so that the effluent can be used for drinking, bathing, irrigation and the like. The disinfecting step can be performed in a chlorine contact chamber  26 , from which effluent is discharged as shown by arrow  28 . 
     An important aspect of the invention is to reduce or preferably, to eliminate air diffusers or jet aerators (not shown), and their associated blowers and power equipment, which have typically been used in the aeration basin  18  for raising dissolved oxygen (DO) to the desired level for aerobic processing. In accordance with the invention, instead of adding oxygen in conventional ways to the aeration basin, supersaturated oxygen is added to elevate the dissolved oxygen (DO) in the aeration basin to the desired level for effective conversion of the organic matter. 
     A preferred source for the supersaturated oxygen is through the Process, which includes a device called a surface tension modification generator (STMG). An example of such a device is described in U.S. Pat. Nos. 7,048,786; 7,270,314; 7,491,340 and 7,544,323, the entire content of which are incorporated herein by reference as though fully described. The STMG described in those patents physically changes the characteristics of the fluid and creates an altered fluid. An energy wave or an electromagnetic wave is applied to the fluid, and the wave travels along the fluid for a defined distance to modify a physical characteristic of the fluid, forming an altered fluid. 
     After the altered fluid is formed, oxygen, ozone or another gas is flowed into the altered fluid forming an altered fluid mixture. Then, the altered mixture is flowed into the inner chamber of a multi-chamber device at a second pressure, which is lower than the first pressure. The altered fluid mixture is then passed from the inner chamber through a plurality of funnels forming a violent turbid fluid condition at a focus point in an outside chamber to dissolve nano-sized oxygen particles into the fluid at an increased concentration, thereby forming supersaturated oxygenated fluid. 
     Alternative methods can be used for forming a supersaturated oxygenated fluid in the Process for introduction into oxygenating aeration basins. These methods include, but are not limited to, (1) air injection, including through course and fine bubble diffusers, (2) side stream injection using a venturi or other method for mixing water and air, oxygen or other gases, (3) known pressurized oxygen delivery systems, such as Speece cones, downflow bubble contactors or sparging methods, (4) U-Tube contactor delivery and mixing systems, (5) liquid oxygen delivery and mixing systems, (6) high purity oxygen and pressure swing adsorption oxygen delivery and mixing systems, (7) cryogenic air separation delivery and mixing systems, (8) jet aerators, (9) commercial oxygen delivery and mixing systems. Any such method must be able to form supersaturated oxygenated fluid with an oxygen concentration sufficient to elevate the dissolved oxygen (DO) in the desired location in the Water System, to a level for effective conversion of the organic matter. 
     In order to adapt the Process for use in a Water System, substantial modification has been required to mitigate the effect of suspended solids and materials in the water source stream. Field testing of the technology in a potential Water System such as a wastewater treatment plant identified a variety of materials that impair the process including but not limited to: organic or biological material, hair, floss, rags, egg shells, grit, silt, small pebbles, plastic, metals, etc. The level (volume, size, composition, etc.) of this type of material depends upon the source of the water supply within the Water System. 
     Because water demands for the super oxygenating liquid in the Process are high, and can require as much as 50% of the wastewater treatment plant throughput, it is advantageous to use liquid from anywhere in the Water System or from one of the stages of the wastewater treatment system, and then introduce the supersaturated oxygenated liquid into the aeration basin or other part of the wastewater treatment plant or Water System where the supersaturated liquid is useful for converting organic matter in the Water System. Because liquid taken from different parts of the Water System have different levels of total suspended solids (TSS), and plant hydraulics are different for liquid taken from each location within a treatment plant, the design considerations vary for each water source. Exemplary embodiments of the invention showing the fluid being taken from different stages of a wastewater treatment system are illustrated in  FIGS. 2-5 . An embodiment of the invention showing fluid being taken from one or more sources in a water treatment system is illustrated in  FIG. 6 . 
       FIG. 2  shows liquid being taken from the grit chamber  12  for introduction into the aeration basin  18 . When liquid is taken from this source, care must be taken to manage flow in order to maintain a continuous process because the liquid supply tends to be uneven and may make this source unsuitable for a continuous process when flow rates are not predictable or have a wide variance. 
     A screen  30  is provided at the outlet of the grit chamber for restricting particle size to &lt;¼″ size or less before the liquid is circulated through the conduit  32  and into the STMG  34  for performing the Process. The STMG  34  includes a filter  36  for filtering suspended material down to 400-1500 microns, or less. After the liquid is supersaturated with oxygen sufficient to raise the DO in the aeration basin to the desired level, supersaturated liquid is introduced into the aeration basin  18  through a conduit  36 . 
     Pumps (not shown) are used to circulate liquid from the grit chamber, or other source of liquid in the embodiments described below, are of the type well known in the art of water treatment systems. These pumps are capable of handling a fluid with high TSS and organic or biological material, hair, floss, rags, egg shells, grit, silt, small pebbles, plastic, metals, etc. before it is filtered in advance of the Process. These types of pumps are typically referred to in the industry as trash pumps, solids pumps or sewage pumps and must be reliable and low maintenance and avoid clogging, felting and plugging. There are a variety of commercially available pumps, such as those made by the Patterson Pump Company, Division of Gorman Rupp Company, Toccoa, Ga., series 10, U, V and T pumps, among others, that can meet these conditions and be optimally sized for the desired flow and pressure desired in the specific application. 
     Liquid from the grit chamber is of a very poor quality and typically has medium TSS (+/−500 Mg/L), and a relatively high solids count. The screen  30  can be a passive suction screen of the type used in well water applications for screening out sand and rocks from water wells. Such a screen can be designed in a way that will provide initial coarse screening of the suspended solids and material and limit the potential negative impact on existing processes. 
     Design considerations include utilizing designs commonly applied to down hole, water well sand screens to restrict sand from entering water wells, which are sold by a number of vendors and fabricators of equipment for the water well industry. The longitudinal screen openings must be designed with a certain minimum square area relative to fluid flow rate to minimize the pressure differential across the screen which in turn minimizes plugging resulting from the adhesion of solids on the screen surface; screen openings of a sufficiently restrictive size to limit the flow of suspended material that would otherwise impair or degrade the process. Such screens can be designed and specified by one with ordinary skill in the art in order to maintain flow across the screen face to velocities of 0.1 feet per second or less to prevent caking or plugging of the screens. 
     The inlet screen must be designed to be sufficiently diffused across the basin to minimize local hydraulic imbalances, and fabricated to fit within the logistical and operational constraints of the specific plant design or Water System where the water supply is sourced. 
     The screen should also be designed in such a configuration to prevent air from entering the system and breaking the primary seal on the suction side of the water supply, and to avoid negatively impacting the operations of the plant itself or the water supply on a material basis. 
     The screen can be fabricated from a variety of known materials, from PVC to steel, stainless steel, ceramic, glass, fiberglass, metal, elastomeric materials, carbon fiber, etc. depending upon the particular water environment. Such screens are available from known sources such as Johnson Screens, 11939 Aldine Westfield Rd., Houston Tex. 77093. 
     The filter  36  is self-cleaning with low energy requirements and low water demand during rinse cycles in a continuous flow operation required by the process, and have the following characteristics:
         To efficiently be able to handle the secondary cleaning, the filter had to work with the screening solution to minimize continuous interruptions due to the rinse cycle;   The self-cleaning filter can be installed downstream of the screen and before fluid is processed in the Process; and       

     Rinse cycle waste can be re-injected into the aeration basin or digester. 
     A filter suitable for this purpose is a the ORB Series brush screen filter, Model ORB-04-PE, which is a self-cleaning, continuous flow filter manufactured by Orival, 40 N. Van Brunt St., Englewood, N.J. 07631. There are a number of similar self-cleaning, low-pressure filters that could be substituted for this part of the application. 
       FIG. 3  shows another embodiment of the invention where liquid is taken from the aeration basin  18 , circulated through the Process, and then re-introduced into the aeration basin  18 . This is the optimal source for liquid to be treated because it has no negative impact on plant hydraulics and allows for a closed loop application of the process. 
     A screen  40  is provided at the outlet of the aeration basin for restricting particle size to &lt;¼″ size or less before the liquid is circulated through the conduit  42  and into the STMG  34 . The STMG  34  includes a filter  36  for filtering suspended material down to 400-1500 microns, or less. After the liquid is supersaturated with oxygen sufficient to raise the DO in the aeration basin or Water Source to the desired level, the liquid is re-introduced into the aeration basin  18  through a conduit  44 . 
     Liquid from the aeration basin is the most difficult to treat because it has very high TSS (+/−5000 Mg/L), and suspended material including fibrous material mixed with solids. The screen  30  can be a passive suction screen of the type used in drinking and irrigation water wells, with the characteristics described above in conjunction with  FIG. 2 . 
     The pumps (not shown) and filter  36  can also have the same characteristics as the ones described above in conjunction with  FIG. 2 . 
       FIG. 4  shows liquid being taken from the clarifier  24 , circulated through the STMG, and then introduced into the aeration basin  18 . A screen  46  is provided at the outlet of the clarifier  24  for restricting particle size to &lt;¼″ size or less before the liquid is circulated through the conduit  48  and into the Process  34 . The STMG  34  includes a filter  36  for filtering suspended material down to 400-1500 microns, or less. After the liquid is supersaturated with oxygen to raise the DO in the aeration basin to the desired level, it is introduced into the aeration basin  18  through a conduit  50 . 
     The screen  46  can be a passive suction screen having the characteristics described above in conjunction with  FIG. 2 . 
     The pumps (not shown) and filter  36  can also have the same characteristics as the ones described above in conjunction with  FIG. 2 . 
       FIG. 5  shows liquid being taken from effluent steam  28  after treatment in the tertiary stage  22 , circulated through a conduit  52  into the STMG  34 , and then introduced into the aeration basin  18  through a conduit  54 . Because the liquid has been completely treated there is no need for a screen or filter. 
     The effectiveness of the invention was demonstrated in a series of tests at four different wastewater treatment plants. 
     Test #1 took place at a permanent in ground wastewater treatment plant with a capacity of 250,000 gallons per day (GPD) with secondary treatment that had two mirrored trains of flow with centralized clarifiers. The test focused on ½ of the plant and the Process was supplied from the clarifier. The test results confirmed that the Process could completely eliminate all of the blowers used for aeration, while maintaining acceptable DO levels of &gt;2.0 ppm or mg/L, reducing net solids and creating net power savings of 50-70% over prior operating conditions. The flow rates averaged 80-120 GPM with the water sourced from the clarifier using no screen and screens similar to the detail on the attached schematic design. The DO of the output water from the Process was sufficient to raise the overall DO levels of the basin to the test result levels and were approximately 200-250% saturation. 
     Test #2 took place at a package wastewater treatment plant with a capacity of 300,000 gallons per day (GPD) with secondary treatment that had a single train of flow with centralized clarifiers. The liquid was taken from the clarifier, with typical TSS of &lt;500 mg/L and circulated through the Process and then introduced into the aeration basin. The flow rates averaged 80-120 GPM with the water sourced from the clarifier using no screen and screens similar to the detail on the attached schematic design. The DO of the output water from the Process was sufficient to raise the overall DO levels of the basin to the test result levels and were approximately 200-250% saturation. The test results confirmed that the Process could completely was able to improve the DO levels in the aeration basins by &gt;250%, reduce solids and improve the overall health of the plant while achieving electric power savings of 51%. 
     Test #3 took place at a larger package wastewater treatment plant with a capacity of 900,000 GPD that was split into two trains, one side which operated normally and the other side with an liquid taken from the clarifier, circulated through the Process, and then introduced into the aeration basin. This test site was on one side of a two-train plant (two independent wastewater treatment systems) with a total of 7 aeration basins and 2 clarifiers. The liquid was taken from the clarifier, circulated through the Process and then introduced into the aeration basin. During the test of this site, the Process was able to improve the DO levels of the aeration basin by over 400% while reducing overall power demand on the entire plant by 35%, reducing solids and improving the overall health of the plant by restoring DO levels to appropriate levels. In this test the flow rates varied between 100-120 GPM and was sourced from the clarifier with TSS &lt;500 mg/l and a variety of screen configurations were utilized. The DO of the output water from the Process was sufficient to raise the overall DO levels of the basin to the test result levels and were approximately 200-250% saturation. Plugging from organic and inorganic debris suspended in the clarifier impaired the process, by reducing flow and requiring physical clearing of the Process until the proper screening solution was discovered and designed to fit the specific local circumstances while not impairing the routine operation of the plant. 
     Test #4 took place at a larger package wastewater treatment plant with a capacity of 1,200,000 GPD that was split into four trains of 2-3 aeration basins per train (9 total) and 4 clarifiers of approximately equal size. Average daily flow at the plant was approximately 90-100% or more of design capacity. Two separate Process boxes were installed at the site that and the site was plumbed to allow sourcing of the water from a variety of sources within the plant including the effluent of the plant, the clarifier or from the aeration basin. Specific local logistics prevented the sourcing of water from the equalization chamber or from another non-potable or potable water source. Each box served 2 of the process trains or approximately 50% of the plant capacity. Each box flowed Process water in a range of flows from 90-190 GPM depending upon the source and discharge requirements of the configuration. When both boxes were configured to maximum flow rates, the daily equivalent flow was approximately 550,000 GPD (190 GPM×1440 minutes/day×2 boxes) or the equivalent of 45.6% of the plant capacity. Various configurations of screens were installed until the above discovered design criteria was found and various flow configurations were experimented with to discover the best approach for various different installation configurations that would limit the introduction of solids, prevent the introduction of air to the system and minimize the impact on existing plant operations. 
     The characteristics of how the plant operated near its design capacity and the volume of water used in this test required that the water supply for the process be sourced from the aeration basin where TSS was routinely 4-5000 mg/l to minimize hydraulic overloading within the plant. The aeration basin also contained a variety of fibrous and solid material that impaired the process and required commercially infeasible shutdowns and maintenance to restore the process. In addition, due to the heavy loading of the plant, the amount of suspended material present when water was sourced from the clarifier with TSS &lt;500 mg/l also impaired the process to an extent that required screening and filtering. 
     In addition, there were a number of occasions when the poor quality of even the effluent source of water supply required screening and filtering to not impair the Process and the TSS was estimated to be &lt;500 mg/l due to a combination of heavy loading and rain events. Once the hydraulics were stabilized through the proper screening and filtering of the supply water test results confirmed that the DO of the output water from the Process was sufficient to raise the overall DO levels of the aeration basin to the test result levels and were approximately 200-1000% and above with supersaturated oxygenated water with DO levels of 250-700% mg/l from the Process. In addition the DO levels also improved in the clarifiers by 250-500% during the test period. 
       FIG. 6  shows the components of a representative natural or manmade Water System, which includes the STMG  34  connected to receive liquid from a water source, which can be one or more of a river or stream  60 , a pond or lake  62 , a man-made water treatment lagoon  64 , a water source such as a holding tank  66  and/or an underground well  68 , shown by the arrows  60   a ,  62   a ,  64   a ,  66   a  and  68   a , respectively. The liquid is introduced into the STMG  34  from a header  70 , as shown by the arrow  72 , through the filter  36 , which are similar to the STMG and filter described above for previous embodiments. Appropriate screens (not shown) are used for screening liquid from each of these sources, which have the same characteristics described above for previous embodiments. 
     After the fluid is supersaturated with oxygen sufficient to raise the DO in the lagoon  64  and other portions of the Water Source in which the liquid is reintroduced, the supersaturated liquid is reintroduced into one or more of the river or stream  60 , the pond or lake  62 , the water treatment lagoon  64 , the water source such as a holding tank  66  and/or the underground well  68 , as shown by the arrows  60   b ,  62   b ,  64   b ,  66   b  and  68   b , respectively. In this way, organic material being treated in the lagoon  64  can be separated effectively without the need for oxygenating he water from other sources. 
     The embodiments described are intended to be exemplary and not all-inconclusive, and those with ordinary skill in the art will be able to make improvements and modifications within the spirit and scope of the invention.