Abstract:
A method and apparatus for dissolving an gas into a fluid which may contain at least one dissolved gas. In one embodiment, the apparatus includes a first vertically oriented tube defining a first inner space therein and having open upper and bottom ends. The apparatus also includes a second vertically oriented tube of diameter larger than the first tube and concentrically oriented about the first tube. The space between the first and second tubes is referred to as the second inner space. For introduction of the gas, the apparatus includes an inlet into the second inner space. The appartus includes an acceleration device for accelerating the flow of fluid through the second inner space. The acceleration device is placed above the bubble swarm. Further, the apparatus includes a helix-shaped bubble harvester located below the bubble swarm. The harvester removes fugitive (undissolved) bubbles from the fluid flow and returns them to the bubble swarm to increase the probability that those bubbles will be dissolved into the fluid. During operation, fluid is accelerated downward through the second inner space to maintain two phase flow in the bubble swarm. The harvester removes fugitive bubbles from the fluid leaving the bubble swarm and returns them to the bubble swarm to enhance the absorption rate and efficiency. In another embodiment of the invention, at least one gas initially dissolved into the fluid and then stripped by the reduced partial pressure in the bubble swarm is allowed to leave the apparatus through a vent. The present invention operates with hydrostatic pressure applications and in applications using externally supplied oxygen. It is inexpensive to produce, install, operate and maintain, while being capable of producing a significant amount of dissolved gas with a high absorption efficiency and low energy consumption. The apparatus and method are also suitable for a multitude of applications.

Description:
FIELD OF THE INVENTION  
         [0001]    This invention relates to an apparatus and method for dissolving gas in a fluid, and, more particularly, to dissolving a gas into a fluid which may contain other dissolved gases.  
         BACKGROUND OF THE INVENTION  
         [0002]    There are many instances when it is desirable to dissolve a gas, whether soluable or insoluable, into a fluid which may already contain other dissolved gases. For example, the macro and microbial organisms in all rivers, lakes, oceans, and all aerobic wastewater treatment processes are based on the presence of sufficient dissolved oxygen to sustain their life processes. Normally, in undisturbed bodies of water there is a rather low density of macro and micro organisms in the surface water and the limited natural absorption of oxygen from the air into the water is sufficient to maintain sufficient concentrations of dissolved oxygen in the water to sustain the life processes of that body of water. However, with increased population density and industrial activity, the associated organic water pollution causes a high microbial oxygen demand that natural oxygen aeration processes cannot begin to provide sufficient oxygen resources. Thus, artificial aeration mechanisms are required to enhance oxygen absorption.  
           [0003]    Some specific examples of oxygenation applications are worthy of discussion. Odors at aerobic wastewater treatment facilities are associated with the inability to maintain sufficient levels of dissolved oxygen (“D.O.”). In the absence of sufficient D.O., nitrates are reduced to N 2  gas. In the absence of both D.O. and nitrates, strongly reducing conditions develop and sulfates are reduced to H 2 S, also known as “rotten egg gas”. This process can occur in any aquatic system where the oxygen demand exceeds the D.O. supply.  
           [0004]    The high organic pollution in municipal wastewater of sewer lift stations supports a corresponding high microbial population, which, in turn, requires a high rate of D.O. to meet the demand. If the demand is not met, H 2 S formation readily occurs. Consequently, sewer force mains are a common source of odor nuisance for municipal public works.  
           [0005]    Some industries (pharmaceutical, petroleum, and chemical, for example) create significant air pollution problems in the course of aerobically treating their wastewater by the use of conventional aeration systems. The wastewaters contain significant volatile organics/solvents which are readily biodegradable if they can be retained in the aqueous phase for a sufficient time. The use of conventional aeration systems has led to the requirement that the wastewater aeration basins must be covered to capture and incinerate the off gas in order to comply with air emission regulations. The need for a covered basin arises because conventional aeration systems readily strip the organics/solvents from the aqueous phase, not allowing for a sufficient time to biograde in the liquid.  
           [0006]    Aerobic activated sludge processes are dependent upon oxygen transfer and sludge settling and recycle in the secondary clarifiers. It is now possible to develop high concentrations of sludge concentrations within the reactors, such as with the use of aerobic fluidized beds and moving bed filters, to the point where oxygen transfer becomes the limiting factor. Specifically, high levels of D.O. are required without subjecting the sludge to high energy dissipation/turbulence conditions which could shear off the biofilms or hinder flocculent sedimentation in the secondary clarifiers.  
           [0007]    Fish farming and shrimp production commonly occurs in large ponds. To maximize production, the ponds are operated at the edge of D.O. availability. Since a still pond absorbs very little oxygen, there exists a need for artificial aeration to sustain high levels of fish/shellfish production.  
           [0008]    The desire to increase dissolved oxygen levels is also applicable to slow moving rivers (such as the Cuyahoga River flowing through Cleveland, Ohio, and the rivers in Bangkok and Taipei) and canals (such as the waterways of Chicago, Ill. and the canals of Amsterdam). Many industries must curtail production (to considerable economic detriment) due to insufficient D.O. in the rivers, streams, and canals to which they discharge their treated wastewaters. Odor and corrosion problems can also occur in the bottom layer of stratified lakes and reservoirs feeding hydroelectric power dams. The low D.O. levels also result in fish kills.  
           [0009]    Systems for dissolving a gas into a fluid are not limited to dissolving oxygen in water. Other gas/fluid combinations include: hydrogenation of vegetable oils, coal liquification, yeast production, Vitamin C production, pharmaceutical and industrial aerobic bioprocesses, and other processes well known in the art.  
           [0010]    Therefore, it is desired to provide an apparatus and method of dissolving a gas into a fluid possibly containing other dissolved gases that has application in at least the following situations:  
           [0011]    Slow moving rivers and canals  
           [0012]    Reservoirs  
           [0013]    Fish, shrimp shellfish, and/or mussel ponds  
           [0014]    Aerobic wastewater treatment systems  
           [0015]    Sewer lift stations  
           [0016]    Wastewater industries such as the pharmaceutical, petroleum, and chemical industries  
           [0017]    Aerated lagoons  
           [0018]    Hydrogenation of vegetable oils  
           [0019]    Coal liquification  
           [0020]    Yeast Production  
           [0021]    Vitamin C product  
           [0022]    Pharmaceutical and industrial aerobic bioprocesses  
           [0023]    Ozonation of water or other fluids  
           [0024]    Dissolving xenon in fluids for injecting into the body  
           [0025]    Supersaturating eye-wash liquids with supersaturated D.O.  
           [0026]    Conventional aeration systems either bubble air through diffusers in the bottom of the aeration tank or splash the water in contact with the air. These systems typically absorb 1 to 2 lbs. of oxygen per kilowatt hour of energy consumed. Oxygen absorption efficiency is generally not an issue with these systems because air is free. These systems are most efficient when the D.O. in the water is near zero and are progressively inefficient as the water D.O. level approaches saturation, i.e., 9.2 ppm at 20° C. at sea level. Because the oxygen used in the aeration process is from the air and therefore at no cost, the costs of such systems emanates from capital costs and operating costs. The capital cost of a surface aerator capable of dissolving one ton per day of D.O. is about $40,000. The cost of power for the aerator is $70 to $140/ton of D.O. If the capital costs are amortized at 8% for a 10 year life, the total cost is approximately $87 to $157/ton of D.O.  
           [0027]    In addition to costs, there are other disadvantages or shortcomings of conventional aeration systems. These shortcomings include: (a) low achievable D.O. concentrations of only 1 to 3 ppm; (b) high off-gas production; (c) high air stripping of volatile organic contaminants; (d) high energy dissipation in the reactor; (e) floc shear; and (f) limited D.O. supply potential.  
           [0028]    As an alternative to conventional systems using “free” air to increase D.O. levels, systems now exist which generate or store oxygen on-site and dissolve this generated or stored oxygen into the water. Some of these systems are as economical as conventional aeration systems. Some of these systems address some of the shortcomings of conventional aeration systems. However, these systems have their own shortcomings.  
           [0029]    For example, when high purity oxygen is being transferred into water, issues arise as to handling of dissolved nitrogen (“D.N.”) already in the water. D.N. is not utilized in an aqueous environment. Air is primarily comprised of 21% oxygen and 79% nitrogen gas. When water is in contact with air for prolonged periods, the water is saturated with D.N. At 30° C., the saturation concentration of D.N. in water is 16 mg/L. With conventional aeration systems, D.N. levels remain in a steady state. However, when high purity oxygen is introduced into the water, it results in a reduced D.N. partial pressure which strips the D.N. from the dissolved phase into the gas phase where it, in turn, reduces the percentage oxygen composition. The reduction in percentage oxygen composition reduces the partial pressure of oxygen in the gas phase, and the saturation concentration of oxygen, and ultimately the rate of oxygen transfer.  
           [0030]    Thus, the presence of D.N. in the incoming water presents is a trade-off situation. If high oxygen absorption efficiency is to be achieved, the increased nitrogen gas composition in the gas phase has to be accepted. This reduces the D.O. concentration which can be achieved in the discharge. Conversely, if high D.O. levels are to be achieved in the discharge, then the stripped nitrogen in the gas phase has to be wasted to reduce its percentage composition carrying with it a commensurate ratio of oxygen gas and reducing the percentage oxygen absorption efficiency.  
           [0031]    Therefore, it is desirable to develop an oxygenation system which manages the level of D.N. already present in the water, and which reduces the concentration of D.N. to allow for higher potential D.O. saturation (total gas composition of N 2 +O 2 −100%). Further, effervescent loss of highly saturated D.O. in the discharge should be prevented if the D.N. is reduced. Of course, these principles are applicable to dissolving a gas into a fluid containing dissolved gases other than dissolving oxygen in water (containing dissolved nitrogen).  
           [0032]    Another problem associated with prior art systems is the ability of the systems to provide a protracted period of contact (generally preferred to be greater than  100  seconds) of the bubbles of oxygen (air) with the water. Prolonged contact of the bubbles helps to ensure a high oxygen absorption efficiency. Further, bubbles in the water should be controlled—the greater number of bubbles of oxygen, the greater the percentage oxygen absorption efficiency. Therefore, it is desired to provide an oxygenation system and method which fully utilizes the bubbles in the system and which prolongs the contact of those bubbles with the water to increase oxygen absorption efficiency of the apparatus.  
           [0033]    With regard to the systems using oxygen rather than air, it is well known that high purity oxygen can be transported to the site in the form of liquid oxygen which is subsequently converted to gaseous oxygen for delivery to the oxygenator apparatus. Alternatively, on-site generation using cryogenic separation is feasible for oxygen requirements of 40 tons or more per day. Costs of liquid oxygen transported to the site fluctuates with the vagarities of site-specific conditions and the number of regional suppliers in competition, among other factors. Thus, in some instances, the cost of transported liquid oxygen may be prohibitive.  
           [0034]    For oxygen generated using cryogenic systems, the oxygen can be produced in either the liquid or gaseous forms. If the oxygen is to be used at the same rate as it is produced, the gaseous state is preferred as it is less expensive to produce the gaseous form. However, if the generated oxygen is not used immediately, storage usually requires generation in the liquid state which significantly increases the costs associated with the generated oxygen, both as to production and due to the requirement for double-walled liquid oxygen storage tanks.  
           [0035]    Another on-site production system is known as the pulsed swing absorption (PSA) process which utilizes pressure vessels filled with molecular sieves. A standard air compressor is used to feed the PSA device, and it generates oxygen with a 90% to 95% purity. The outlet pressure is related to the pressure of the air compressor which thus is the major cost factor in operating a PSA system. Therefore, it is desired to use the lowest possible PSA outlet pressure. In view of the available oxygen sources not based on “free” air, it is desirable to use PSA systems.  
           [0036]    Oxygen dissolution into water is enhanced by increased pressure in the oxygen/water contactor (bubble swarm). However, the unit energy consumption is excessive if the water has to be pumped into the oxygen/water contactor, because there is no economical way to recover this energy when the water leaves the contactor. However, if the oxygen/water contactor is placed below the ground surface and pressurized by a static head of water, the water can be moved into and out of it with negligible energy—only frictional losses. Yet, the oxygen transfer is significantly enhanced without associated energy consumption for pumping to maintain the pressure.  
           [0037]    Overall, it is desirable to provide an apparatus and method for dissolving a gas into a fluid which: (a) has a low capital cost; (b) has a low operating cost (kwhr/ton of gas dissolved); (c) discharges high D.O. concentrations; and (d) has a high oxygen absorption efficiency. Ideally, the system should be capable of producing a discharge D.O. of at least 30 mg/L and have an oxygen absorption efficiency of at least 80%, all accomplished with reasonable capital costs and a low unit operating cost.  
         SUMMARY OF THE INVENTION  
         [0038]    The present invention is an apparatus and method for dissolving a gas (whether soluable or insoluable) into a fluid which may or may not contain other dissolved gases. For example, the present invention may be used as an oxygenation system, i.e., dissolving oxygen into water (water contains dissolved nitrogen).  
           [0039]    In one embodiment, the apparatus comprises an inlet, an outlet, a bubble contact chamber, an acceleration device, a helix-shaped bubble harvester, and a bubble return pipe. The inlet receives the fluid containing the extraneous dissolved gas and is located at the top of the apparatus. Near the inlet and at the top of the bubble contact chamber is located the acceleration device for acceleration of the fluid therethrough into the chamber. The acceleration design may comprise a horizontally oriented plate extending through the entire upper end of the chamber and having at least one aperture therein. The chamber is made of two portions. The upper portion has either a constant or a generally diverging inside surface. The lower portion is substantially cylindrical in shape with a closed bottom end having at least one aperture therethrough. An inlet for introduction of the gas to be dissolved is connected to the chamber. The outlet is operatively connected to at least one aperture of the bottom end of the chamber. Residing in the bottom portion of the chamber is a helix-shaped bubble harvester. The bubble return pipe of the apparatus is vertically oriented and cylindrical in shape. The bubble return pipe has an open bottom end in the lower portion of the chamber, an open top end in the upper portion of the chamber, and at least one aperture located in the lower portion of the chamber proximate to the harvester.  
           [0040]    During operation of this embodiment, fluid enters the inlet and flows through the acceleration device. The accelerated fluid provides turbulence to keep the bubble size small. Without this turbulence, the bubble swarm will coalesce and collapse, greatly reducing the oxygen absorption rate. The harvester translates the fluid flow into a horizontal component which allows the bubbles to rise and attach to the underside of the helix-shaped harvester. The bubbles then flow upward by gravity and inward due to centrifugal force in the helix. The bubbles flow into the bubble return pipe through at least one aperture in the tube and into the bubble chamber for recycling. Exiting out the outlet is a fluid containing a high concentration of dissolved gas and devoid of bubbles.  
           [0041]    In another embodiment of the apparatus of the present invention, first and second vertical cylindrical tubes are concentrically oriented, with the first tube inside the second tube. The space inside the first tube is the first inner space and is the space through which fluid containing dissolved gas exits upward out of the apparatus. The second inner space is the space between the first and second tubes and is the space through which fluid and the dissolved gas enter the apparatus.  
           [0042]    Two alternatives of this invention are disclosed. In one alternative, the combination of an acceleration device, an inlet, a helix-shaped bubble harvester, and a bubble return tube are placed near the bottom of the apparatus. This combination is referred to as the gas dissolver, and operates similarly to the previously described embodiment. Briefly, fluid flows through the acceleration device in the second inner space. The gas is introduced to the second inner space immediately below the acceleration device to result in bubbles and fluid flowing downward within the second inner space. At the harvester, bubbles are returned to the second inner space. The fluid having dissolved gas exits upward through the first inner space.  
           [0043]    In a second alternative, the combination of an acceleration device, a harvester, and a bubble return tube are placed near the top of the apparatus. This combination is referred to as the dissolved gas stripper. The apparatus also includes a means for receiving waste gas from the oxygen gas absorber in the bottom of the apparatus, including a first vent located near the gas dissolver, waste gas tube, and a second vent located above the second harvester. Waste gas (gas from a gas dissolved in the fluid initially but later displaced by the dissolved gas) exits from the gas dissolved through the first vent and the waste gas tube into the bubble tube of the dissolved gas stripper. At the dissolved gas stripper, waste gas exits the apparatus through the second vent.  
           [0044]    The dissolved gas stripper function is enhanced by the low pressure in the bubbles swarm at the top of the apparatus, while the oxygen absorber function is enhanced by the increased hydrostatic head at the bottom of the apparatus.  
           [0045]    In yet another embodiment of the apparatus of the present invention, the harvester and bubble return pipe are placed near the bottom of the inlet side of a U-tube oxygenator. The use of the harvester and return pipe results in more efficient transfer. Thus, this modified U-tube oxygenator need not be as deep as a conventional U-tube oxygenator.  
           [0046]    The apparatus and method of the present invention is inexpensive to produce, install, maintain, and operate when compared to many systems used for oxygenation, for example. The apparatus and method may be used to dissolve a gas into a fluid which may or may not contain other dissolved gases. It has application where oxygenation is required, such as in slow moving rivers and canals, reservoirs, fish/shellfish/mussel ponds, aerobic wastewater treatment systems, sewer lift stations, wastewater industrial applications, lagoons, and more. It is also not limited to oxygenation of water, but is applicable for other gas dissolving applications.  
           [0047]    The present invention is also highly efficient in absorption of the gas into the fluid. When the embodiment including a stripper is used, this efficiency is further increased. The apparatus may be used for fluid applications as well as when hydrostatic pressure is available, such as at the beginning of sewer force mains. 
       
    
    
     BRIEF DESCRIPTION OF THE DRAWINGS  
       [0048]    [0048]FIG. 1 shows a side view of one embodiment of the apparatus of the present invention in which the outer tube member is translucent to illustrate the components of the apparatus;  
         [0049]    [0049]FIG. 2 shows a cross-sectional view of the apparatus of FIG. 1 at line  2 - 2  of FIG. 1;  
         [0050]    [0050]FIG. 3 shows a cross-sectioned view of the apparatus of FIG. 1 at line  3 - 3  of FIG. 1;  
         [0051]    [0051]FIG. 4 shows a cross-sectioned view of the apparatus of FIG. 1 at line  4 - 4  of FIG. 1;  
         [0052]    [0052]FIG. 5 shows a side view of a second embodiment of the apparatus of the present invention wherein the exterior of the apparatus is translucent to illustrate the components of the apparatus;  
         [0053]    [0053]FIG. 6 shows a side view of a third embodiment of the apparatus of the present invention wherein the outer tube member is translucent to illustrate the components of the apparatus; and  
         [0054]    [0054]FIG. 7 shows a side view of a fourth embodiment of the apparatus of the present invention wherein the tube member is translucent to illustrate the components of the apparatus. 
     
    
     DETAILED DESCRIPTION OF THE INVENTION  
       [0055]    Referring now to FIG. 1, there is shown a side view of one embodiment of the apparatus of the present invention in which the outer tube member is translucent to illustrate the components of the apparatus. In this embodiment, apparatus  10  is used to oxygenate water. Because water contains dissolved nitrogen which is displaced by the dissolved oxygen, apparatus  10  also permits for outgassing (stripping) of nitrogen gas.  
         [0056]    Apparatus  10  includes first tube member  12 , second tube member  14 , third tube member  16 , gas feed inlet  18 , accelerator plate  20 , bubble harvester  22 , waste gas vent  24 , and waste gas tube  26 . Both the upper end  28  and the bottom end  30  of first tube  62  are open. The interior of first tube  12  between upper end  28  and bottom end  30  defines first inner space  32 . First tube member  12  is oriented in a substantially vertical orientation and is comprised of a material impervious to the passage of fluid therethrough. If the fluid comprises water, for example, first tube  12  may be comprised of plastic or metal. The material of first tube  12  should also be resistent to corrosion caused by the fluid.  
         [0057]    Apparatus  10  also includes second tube member  14  oriented in a substantially vertical orientation. Second tube member is of a diameter greater than the diameter of first tube member  12  and is oriented in a substantial concentric orientation relative to the first tube member  12 . Second tube member  14  has open upper end  34  and closed bottom end  36 . The space between the outside of first tube member  12  and the inside of second tube member  14  is second inner space  40 . Second tube member  14  should also be impervious to the flow of the fluid therethrough and it is preferred that it be resistant to corrosion caused by the fluid. Second tube member  14  should also be made of a material impervious to the flow of any material on the outside of second tube member  14  and is preferred to be resistent to corrosion caused by such material. First and second tube members  12  and  14  may be comprised of a similar material, but this is not required.  
         [0058]    Third tube member  16  has open upper end  42  and open bottom end  44 , is cylindrical in shape, and also substantially vertically oriented within second inner space  40 . Bottom end  44  is on the place formed by bottom end  30  of first tube member  12 . Upper end  42  is within second inner space  40  above bubble harvester  22 , waste gas vent  24  and waste gas tube  26 , and below accelerator plate  20  and inlet  18 . Third tube member  16  also includes at least one aperture or slot  46  proximate harvester  22 . Third tube member  16  should be comprised of a material impervious to the flow of fluid or the waste gas therethrough. Thus, third tube member  16  may be comprised of the same material as first tube member  12  and/or second tube member  14 , but this is not required.  
         [0059]    In the embodiment of FIG. 1, third tube member  16  is shown to lie against first tube member  12  (see also FIGS. 3 and 4). It is required that third tube member reside within second inner space  40 , as explained in greater detail below. It is not required that third tube member  16  be in contact with first tube member  12  as shown; however, as will be explained hereinafter, it is advantageous to place third tube member  16  closer to the central longitudinal axis of first tube member  12  and of apparatus  10  and, more specifically, close to the central axis of helix-shaped harvester  22 .  
         [0060]    Returning now to FIG. 1, apparatus  10  also includes inlet  18 , serving as an inlet means for introduction of the gas (in this illustration oxygen) to be dissolved into the fluid housed in second inner space  40 . The gas may be pumped into inlet  18  by means well known in the art for introduction of the gas into second inner space  40  through second tube member  14 .  
         [0061]    Apparatus  10  further comprises accelerator plate  20 . Accelerator plate  20  serves as a means to accelerate the flow of fluid therethrough. As shown in FIG. 2, a cross-sectional view along line  2 - 2  of FIG. 1, in this embodiment, accelerator plate  20  comprises a donut-shaped plate substantially extending horizontally and substantially filling second inner space  40 . Accelerator plate  20  also includes at least one aperture  48  for the flow of fluid therethrough.  
         [0062]    Accelerator plate  20  is only one alternative that may be used in the present invention. Again, the primary object of accelerator plate  20  is to accelerate the flow of fluid beneath accelerator plate  20  when compared to the flow of fluid above accelerator plate  20 . Thus, the acceleration means used to accomplish this objective must reside within the second inner space  40 , need not extend across the entire second inner space  40 , and, overall, may be an accelerator of the type well known in the art. For example, a suitable acceleration means may be a small mixer which, like accelerator plate  20 , prevents or inhibits the bubbles from coalescing and collapsing.  
         [0063]    As shown in FIG. 1 and in FIG. 3 (a cross-sectional view along line  3 - 3  of FIG. 1), apparatus  10  also includes waste gas vent  24  and waste gas tube  26 . Both waste gas vent  24  and waste gas tube  26  are positioned below upper end  42  of third tube member  16  and above bubble harvester  22 . In this embodiment, waste gas vent  24  simply comprises a trap to trap rising waste gas. Waste gas tube  26  extends through second tube member  14  below the upper lip of waste gas vent  24  to capture waste gas and allow it to travel through waste gas tube  26 .  
         [0064]    Returning to FIG. 1, apparatus  10  further includes bubble harvester  22 . As shown in FIG. 4, a cross-sectional view of line  4 - 4  of FIG. 1, harvester  22  is positioned within second inner space  40  and substantially extends from the outside of first tube member  12  to the inside of second tube member  14  while accommodating third tube member  16  therethrough. Returning to FIG. 1, harvester  22  is helix-shaped and includes upper end  50  and bottom end  52 . Bottom end  52  of harvester  22  is positioned above bottom end  36  of second tube member  14  and below bottom end  30  of first tube member  12 . The upper end  50  of harvester  22  is below accelerator plane  20 , inlet  18 , waste gas vent  24 , and waste gas tube  26 .  
         [0065]    Based on the above description, the operation of the embodiment of FIG. 1 is now described. Fluid (in this example, water) is allowed to flow downward within second inner space  40  toward accelerator plate  20 . Gas (in this example, oxygen) is introduced into second inner space  40  at inlet  18 . Acceleration plate  22  causes an increase in velocity in the fluid and bubbles below accelerator plate  20  when compared to the flow of fluid above accelerator plate  20 . The faster flowing fluid is caused by the restriction of cross-sectional area in second inner space  40  and results in the creation of downward moving jets of fluid. The downward moving fluid jets assist in maintaining a dynamic swarm of bubbles of the gas within second inner space  40 . Without the jets, the bubble swarm would coalesce and/or collapse, drastically reducing the gas bubble surface area per unit volume of liquid within second inner space  40 .  
         [0066]    The bubbles continue to flow downward toward helix-shaped bubble harvester  22 . Harvester  22  acts similar to a parallel plate separator in that the fluid flow is converted into a horizontal component, which results in the bubbles rising to the underside of harvester  22  above. This process removes bubbles from the fluid flow and causes the bubbles to rise upward in the opposite direction of the fluid flow along the underside of harvester  22 . The centrifugal force impacted by helix-shaped harvester  22  also forces bubbles toward the center of second inner space  40 . Some bubbles may be, during this process, in sufficient contact with the fluid to become dissolved in the fluid. If bubbles are not so dissolved, they enter slots  46  of third tube member  16 . These fugitive bubbles of gas are thus collected in the zone of harvester  22  of apparatus  10  and conveyed by gravity up third tube member  16  and into the bubble swarm of second innerspace  40 .  
         [0067]    Because less than all of the bubbles are absorbed into the fluid, bubbles are continually wasted from apparatus  10 . Excess bubbles leave apparatus  10  by being trapped by waste gas vent  24  and exit apparatus  10  by waste gas tube  26 . The fluid containing dissolved gas exits apparatus  10  by flowing upward through first tube member  12 .  
         [0068]    It will be appreciated by those of skill in the art that the gas dissolving apparatus of the present invention is comprised of few parts and of no moving parts, other than might be recognized or desired to introduce gas through inlet  18  and/or fluid through second inner space  40  (see FIG. 6, for example). Thus, the apparatus is cost effective, both as to capital costs and costs of operation. The apparatus does not require significant maintenance. The apparatus allows large particles to freely pass through the system. Yet, it is quite capable of resulting in high nonsoluable gas absorption efficiency.  
         [0069]    Referring now to FIG. 5, there is shown a side view of a second embodiment of the apparatus wherein the exterior of the apparatus is translucent to illustrate the components of the apparatus. In this embodiment, apparatus  100  includes inlet  102 , dissolved gas feed  103 , accelerator plane  104 , bubble contact chamber  106 , bubble harvester  108 , bubble return tube member  110 , and outlet  112 . Inlet  102  serves as a means for receipt of the fluid with or without an gas therethrough. Dissolved gas feed  103  serves as a means for introduction of the gas to the fluid housed in chamber  106 . Accelerator plate  104 , similar to accelerator plate  20  of FIG. 1, serves to accelerate the flow of fluids and bubbles in chamber  106  when compared to the fluid flow in inlet  102 .  
         [0070]    Bubble chamber  106  is comprised of first portion  114  and second portion  116 . As illustrated, first portion  114  has a diverging interior surface. Second portion  116  is substantially cylindrical and includes a bottom surface  118  having at least one aperture  120  therethrough. Aperture  120  is operatively connected to outlet  112 .  
         [0071]    Within second portion  116  of chamber  106  is harvester  108 . Like harvester  22  of FIG. 1, harvester  108  is helical and, except for the accommodation of bubble return tube member  110 , substantially extends across the interior of second portion  116  of chamber  106 .  
         [0072]    Bubble return tube member  110  is substantially vertical and proximate to the center axis of chamber  106 . Tube member  110 , like third tube member  16  of FIG. 1, has open upper end  122 , open bottom end  124 , and at least one aperture  126 . Apertures  126  are located proximate harvester  108  and are below the upper end of harvester  108 .  
         [0073]    As will be appreciated by those of skill in the art, the embodiment of FIG. 5 will operate in the presence of hydrostatic pressure, such as in a pump discharge. In such a configuration, there also is no need to accommodate outgassing of initially dissolved gases displaced by the absorption of the gas. Therefore, the embodiment of FIG. 3 does not contain any special components for handling waste gas.  
         [0074]    Considering the operation of the apparatus of FIG. 5, fluid is introduced to apparatus via inlet  102  and gas is introduced via gas inlet  103 . Increased jet velocity of the fluid is achieved by passage of the fluid through accelerator plate  104  in the manner described in association with accelerator plate  20  of FIG. 1. The expanded cross-section of first portion  114  of chamber  106  reduces the downward velocity of the fluid to less than or equal to that of the buoyant velocity of the bubbles of gas in the bubble swarm in chamber  106 . This reduction in fluid velocity allows retention of a very high concentration of bubbles in the swarm housed in chamber  106 . The configuration of chamber  106  therefore enhances gas absorption. Maintenance of prolonged bubble residence times in the bubble swarm is helpful in this regard.  
         [0075]    As fluid and bubbles reach harvester  108  in second portion  116  of chamber  106 , harvester  108  translates the fluid flow into a horizontal component which permits the bubbles to rise and attach to the underside of harvester  108 , thereby removing them from the fluid flow. The bubbles then flow upward by gravity and inward due to centrifugal force in helix-shaped harvester  108 . The bubbles enter apertures  126  of bubble return tube member  110  and flow upward out upper end  122  of tube member  110  into chamber  106 . Thus, apparatus  100  returns fugitive bubbles to enhance efficiency by prolonging their residence times. Fluid having gas dissolved therein exits chamber  106  through aperture  120  of bottom surface  118  of chamber  106  into outlet  112 .  
         [0076]    It will be appreciated by those of skill in the art that several mechanisms contribute to the gas absorption efficiency of the apparatus of FIG. 5. The shape of chamber  106  assists in keeping bubbles in contact with the fluid for an extended period of time to enhance absorption. To dissolve oxygen in water, for example, it is desired to force contact of the bubbles with the water for as much as  100  seconds to ensure absorption. Also, the continuation of harvester  108  and bubble return tube member  110  recycle fugitive (unabsorbed) bubbles back into chamber  106 . This also increases absorption efficiency.  
         [0077]    It will also be appreciated that the exact shapes of chamber  106  need not be as illustrated in FIG. 5. For example, various angles and lengths of first portion  114  of chamber are possible. Also, second portion  116  need not be cylindrical in shape. Also, the chamber could be of unitary conical shape, unitary cylindrical shape, or any other shape reasonably able to promote the flow of fluid and the bubble swarm as described herein.  
         [0078]    Referring now to FIG. 6, there is shown a side view of a third embodiment of the apparatus of the present invention wherein the outer tube member is translucent to illustrate the components of the apparatus. In this embodiment, apparatus  150 , like apparatus  10  of FIG. 1, includes first tube member  12 , second tube member  14 , third tube member  16 , inlet means  18 , accelerator plane  20 , first helix-shaped bubble harvester  22 , first waste gas vent  24 , and first waste gas outlet  26 . This embodiment further includes second accelerator plate  152 , second helix-shaped bubble harvester  154 , fourth tube member  156 , second waste gas vent  158 , and second waste gas outlet  160 . The apparatus further includes fifth tube member  162  connecting first gas tube outlet  26  to the open bottom end of fourth tube member  156 .  
         [0079]    As will become apparent with the description of apparatus  150  below, the lower portion of apparatus  150  is primarily responsible for absorption of the gas, and the upper portion is primarily responsible for stripping an initially dissolved gas which is replaced with the absorbed gas. If used to oxygenate water, the lower portion is the oxygen absorption and the upper portion is the nitrogen stripper.  
         [0080]    In the embodiment of FIG. 6, apparatus  150  is buried in an excavated shaft, bottom end  36  of second tube member  14  is approximately  10  feet or more below the surface of the earth. First tube member  12  is about  12  inches in diameter and second tube member  14  is about  36  inches in diameter. These dimensions are illustrative, not a necessity, and not to be limiting in any respect.  
         [0081]    Also nearby is tank  164  having the fluid therein. Tank outlet means  166  extends into the fluid residing in tank  164  and is operatively connected to upper end  34  of second tube member  14 . Tank inlet means  168  extends into the fluid residing in tank  164  and is operatively connected to upper end  28  of first tube member  12 . To initiate and/or maintain flow of fluid from tank  164  through tank outlet means  166  into apparatus  150 , pump means  170  is shown.  
         [0082]    Now, turning to the operation of apparatus  150 , fluid is pumped from tank  164  through tank outlet means  166  into upper end  34  of second tube member  14 . In one embodiment, the velocity of fluid entering upper end  34  of tube member  14  is approximately 0.5 ft/sec to 2.0 ft/sec. The fluid passes through second accelerator plate  152 . Second accelerator plate  152  restricts the cross-sectional area for fluid flow and includes apertures (see FIG. 2) to cause the fluid to accelerate into downward jets. In one embodiment, the downward jets of fluid move at approximately 6 ft/sec to 12 ft/sec. The increased velocity jets maintain a dynamic bubble swarm in the upper portion of apparatus  150 . The rise velocity of the bubbles in this upper portion (only about 0.5 ft/sec to 1 ft/sec in one embodiment) is low enough so that most of the bubbles accumulate and remain in the dynamic bubble swarm. The gas fed into the upper portion originates from first waste gas vent through first waste gas tube  26  as described below. As the gas bubbles accumulate in second inner space  40  in this upper portion of apparatus  150 , they are crowded downward and are eventually lost as the bubble swarm is pushed below second waste gas vent  158  to enter second waste gas tube  160 .  
         [0083]    At the upper portion of apparatus  150 , as fluid flows downward through the bubble swarm the gas (introduced at inlet means  18  originally) is dissolved into the fluid and a gas already dissolved in the fluid is stripped out of the fluid into the gas phase. Fugitive bubbles which get inadvertently dragged out of the bubble swarm must be efficiently captured and returned to the bubble swarm. This is accomplished with second helix-shaped bubble harvester  154  and fourth tube member  156  in a manner as previously described in association with comparable components shown in FIGS. 1 and 5.  
         [0084]    Fluid, devoid of fugitive bubbles, continues downward from the bottom of second harvester  154  toward first accelerator plate  20 . In one embodiment, the velocity of the fluid in this area is about 0.5 ft/sec to 2.0 ft/sec. The operation of the device is, at this point, as described in association with apparatus  10  of FIG. 1  
         [0085]    Because less than all of the gas is absorbed in the lower portion of apparatus  150 , some bubbles are continually wasted from the system through waste gas vent  24  into first waste gas tube  26 , through fifth tube member  162  into fourth tube member  156 . These bubbles are then processed as described above for eventual exit from the system via second waste gas vent  158  and second waste gas tube  160 . Of course, fluid containing dissolved gas and devoid of bubbles exits the bottom of first harvester  22  and flows upward through first tube member  12 , through tank inlet means  168 , into tank  164 .  
         [0086]    It will be appreciated by those of skill in the art that the embodiment of FIG. 6 reduces the extraneous gas (gas initially dissolved in the fluid) in the system to enhance absorption of the gas. The extraneous gas is reduced before the gas dissolver. It will also be appreciated that, although shown as installed in an excavation, the apparatus of FIG. 6 need not be so installed. Instead, apparatus  150  may be placed in a tube or directly into the fluid.  
         [0087]    Referring now to FIG. 7, there is shown a fourth embodiment of the present invention wherein the U-tube member of the apparatus is translucent to illustrate the components of the apparatus. In this embodiment, apparatus  180  comprises a conventional U-tube oxygenator  182  and helical bubble harvester  184  and bubble return pipe (tube member)  186 . Harvester  184  is similar to the bubble harvesters of FIGS. 1, 5, and  6  and bubble return pipe  186  is similar to those of FIGS. 1, 5, and  6 .  
         [0088]    U-tube oxygenator  182  includes inlet  188  for introduction of the gas (such as oxygen) to be dissolved into the fluid (such as water) housed in U-shaped tube member  190 . In this embodiment, harvester  184  is placed proximate the bottom of the inlet side of the U-tube member  190 .  
         [0089]    During operation of apparatus  180 , harvester  184  and bubble return pipe  186  serve the same functionality as described in association with the embodiments of FIGS. 1, 5, and  6 . Specifically, as bubble move down the inlet side of the U-tube number  190 , undissolved (fugitive) bubbles flow upward against the underside of harvester  184 . The captured bubbles then flow into the apertures of bubble return pipe  186  to be returned to the bubble swarm above harvester  184 . Exiting out the outlet side of U-shaped tube member  190  is the fluid containing a high concentration of dissolved gas and devoid of bubbles.  
         [0090]    With regard to the embodiment of FIG. 7, it will be appreciated by those of skill in the art that use of harvester  184  to capture bubbles results in a more efficient transfer of gas into the fluid. As a result, the U-tube apparatus does not have to be as deep as a conventional U-tube apparatus to achieve the same absorption levels.  
         [0091]    It will be appreciated by those of skill in the art that the present invention solves several shortcomings of the prior art and can be used to dissolve soluable and insoluable gases. The apparatus manages the dissolved gases initially present in the fluid and displaced by the dissolved gas. The apparatus provides a high bubble area per volume of fluid to result in a high reduction in dissolved gas deficit. Fugitive bubbles are effectively separated to increase the percentage absorption efficiency of the gas. Hydrostatic pressurization rather than mechanical pressurization is used for dissolving the gas, thereby reducing operational costs. Also, gas is fed into a pressurized fluid chamber without the necessity of equal pressure from a PSA generator.  
         [0092]    It will also be appreciated that the harvester and bubble return pipe of the present invention may be used in any container containing fluid, and need not be vertically oriented as illustrated in FIGS. 1, 5,  6 , and  7 . Instead, the harvester/bubble return pipe may be used to capture bubbles from any fluid flowing in a pipe or conduit (or other container). Further, the harvester/bubble return pipe combination is useful whether or not any gas is to be dissolved into the fluid.  
         [0093]    It will be further appreciated that the use of the harvester/bubble return pipe combination can reduce the cross-section and/or depth of bubble contactor of any apparatus in which it is used. Such reductions result in a lower cost of the apparatus and any cost of excavation of the apparatus, if applicable.  
         [0094]    It will be still further appreciated that the apparatus of the present invention has use in a myriad of applications. In oxygenation of water for example, the present invention may be used for slowly moving rivers and canals, lagoons, reservoirs, fish/shellfish/mussel ponds, wastewater treatment systems, sewer lift stations, and wastewater processing for various industries; including but not limited to the pharmaceutical, petroleum, and chemical industries. The present invention is also useful for dissolving hydrogen into vegetable oil, hydrogen into coal liquifaction fluids, or for pharmaceutical and industry aerobic bioprocesses, such as yeast production and Vitamin C production. The present invention also has application for ozonation of water or other fluids, dissolving xenon into fluids for injecting into the body, and supersaturating eye-wash liquids with D.O.  
         [0095]    The foregoing is offered primarily for purposes of illustrating the apparatus and method of the present invention. It will be readily apparent to those of skill in the art that the materials, dimensions, operating procedures and conditions, and other parameters of the gas dissolving apparatus and method may be further modified or substantiated in various ways without departing from the spirit and scope of the invention.