OXYGENATING APPARATUS, METHOD FOR OXYGENATING WATER THEREWITH, AND APPLICATIONS THEREOF

Abstract: A process for enriching water with oxygen, wherein water is conducted through a water inlet (1) into a sealed enriching space and through one or more turbulent mixers (21, 23) in the enriching space, oxygen is introduced through an oxygen inlet (17) into the water in the enriching space before passing through the turbulent mixer, and the oxygen-enriched water is recovered. The invention further includes an aerobic process by carrying out a chemical or microbiological reaction in the oxygen-enriched water as the reaction medium, and a therapeutic process of carrying out a therapeutic treatment of a body with an agent containing the oxygen-enriched liquid as a vehicle. The invention also concerns an apparatus for enriching water with oxygen, having a water inlet, a sealed enriching space containing an oxygen inlet, and one or more turbulent mixers, and an outlet for oxygenated water (3).

Description: OXYGENATING APPARATUS, METHOD FOR OXYGENATING WATER THEREWITH, AND APPLICATIONS THEREOF Field of invention The present invention relates to improved apparatus for oxygenating water and other liquids and a method for oxygenation with that apparatus. Background of the invention The most effective method and apparatus for saturating water with oxygen on an industrial scale is described in international patent application WO 95/29130. (U.S. patent application Ser. No. 08/441,708). According to this known process, water is introduced into a sealed enriching vessel which is under oxygen pressure, the water is subdivided such as by running it over a series of trays and the water is inflowing contact with the oxygen before about up to 55-60 mg/£ oxygen is dissolved in the water. This known method and apparatus works very well, however, it was desired to develop a high capacity, smaller and less costly than more portable apparatus capable of producing on an industrial scale super oxygenated water containing even more oxygen and retaining the dissolved oxygen for longer periods than with the known method. Effective bioremediation requires a high rate of oxygen use, but replenishment of oxygen occurs very slowly in groundwater. As a result, oxygen levels in the contaminated systems are often quickly repleted, even when water has been thoroughly aerated before the onset of the bioremediat¬ ion process. Bioremediation processes would be much more effective if oxygen levels could be maintained in the groundwater for a longer period of time after they are aerated. This means both higher concentrations of dissolved oxygen, and a lessened degree of degassing of oxygen from the water. Groundwater pollution control efforts have generally focused on using various "pump and treat" methods which have met only with very limited success while being extremely costly and time consuming. A later develop¬ ment of bioremediation, also known as in-situ or passive remediation, has recently presented itself as a more cost-effective means of treatment, and is far the most rapidly expanding sector of groundwater treatment technology. Most bioremediation sites utilize aerobic microorganisms to degrade the contaminants. In some circumstances the contaminants themselves are the primary substrate, however, due to resistance of most synthetic organic chemicals to biodegradation, the microbes often require an additional food source, such a methane or methanol to utilize the contaminants. In any case, the organisms need a surplus of dissolved oxygen to maintain the aerobic conditions necessary for accelerated by biodegradation. Experience demonstrated to date that the maintenance of adequate dissolved oxygen levels is one of the larger challenges to bioremediation proj¬ ects. It was determined that the greater the dissolved oxygen content, the greater and more rapid the treatment. A study conducted by the U.S. Air Force in 1992 found that with about 35 mg/£ dissolved oxygen feed water, an 80% reduction in dichloroethane could be obtained within 150 hours. In a laboratory study in 1993 it was found that vinyl chloride could be reduced by 95% within two weeks by infusing the contaminated groundwater with about 25 mg £ dissolved oxygen. Low dissolved oxygen bioremediation operations have proven to be very slow at best, and completely unsuccessful at worse. For example, in another 1993 experiment it was determined that oxygen levels around 18 mg/£ produced little or no reduction in dichlorethane after twelve days. Four different methods have been employed in the past to introduce oxygen into aquifers: air sparging, electrolysis, hydrogen peroxide, and surface aeration. All of these have limitations. Air sparging in the case of aquifers involved sinking wells into the aquifer to provide contact between the ground- water and the atmosphere. This, however, produces very low oxygen levels comparable to those that occur naturally, of about 10-14 mg/£ in cold water. Electrolysis was not found to offer any practical, real word applications, because concentrations of only up to 16 mg/£ could be obtained but at the same time the organisms for the biodegradation became substantially depopu- lated. Hydrogen peroxide injection seemed promising only at first glance, because oxygen was produced only at ratio of 1:2, and twice as high a concentration of hydrogen peroxide was required to arrive at the relatively low obtainable dissolved oxygen level. Furthermore, hydrogen peroxide proved toxic to the biodegradation organisms and the resulting foam and dead organisms clogged the injection wells. The best remaining known option was above-ground aeration wherein a portion of the groundwater was pumped up, aerated with air or pure oxygen, and injected back in to the aquifer. When using pure oxygen, dissolved oxygen levels of about 35 mg/£ have been obtained in 1992, but these were diluted upon reentering the aquifer. A direct relationship between the biological activity and the high oxygen levels could be established, and the activity dropped sharply with lower the dissolved oxygen levels. The observations have clearly indicated the need for even higher levels of dissolved oxygen for accelerating the bioremed- iation for more optimum rates. Oxygenated water when exposed to ambient atmosphere will gradual¬ ly lose the dissolved oxygen content above the amount (about 10-12 mg/£) that can be maintained under atmospheric equilibrium dynamics. Description of the invention It is an object of the present invention to enable the production of the water highly enriched with oxygen with a higher concentration of dis¬ solved oxygen and with a longer retention of the dissolved oxygen in the water, then has been possible in the prior art, to provide smaller, less costly and more portable apparatus for the industrial skill production of such super oxygenated water, and to provide for the improved utilization of such super oxygenated water. Another object of the present invention to enable industrial scale, continuous production of heretofore unavailable air oxygen levels dissolved in water, with a good retention of the dissolved oxygen, and at substantially reduced cost. As used throughout the specification and the claims, "water" is also meant to include any other liquid that is capable of super oxygenation, including flavored water and other injusticeable beverages. The process of the present invention is an improvement in a process for enriching water with oxygen, wherein water is conducted through a water inlet into a sealed enriching space, oxygen is introduced through an oxygen inlet into the water in the enriching space, and the oxygen-enriched water is recovered thereafter, the improvement comprises the enriching space includ¬ ing a turbulent mixer, and the water is conducted with the oxygen through the turbulent mixer for incoφorating the oxygen into the water before recovering the oxygen-enriched water. The present invention further includes an improvement in an appara¬ tus for enriching water with oxygen, the apparatus having a water inlet, an oxygen inlet, a sealed enriching space, and an outlet for oxygenated water, the improvement comprising the sealed enriching space including the oxygen inlet and a turbulent mixer. The process of the present invention virtually eliminates any dissolved oxygen deficiencies for most bioremediation and other aerobic processes thereby substantially reducing the time and cost of effective site treatment. The apparatus and the process of the present invention rapidly infuses contaminated groundwater with dissolved oxygen levels in excess of 65 mg/£. Pure oxygen can be infused at about 40 psi, suitably at about 50 to about 55 psi pressure which is capable of treating over 50,000 gallons per day. The present invention can achieve even higher dissolved oxygen concentrations either at lower flow rates, and/or with apparatus designed for higher throughput. Such higher throughput can be obtained, for example, by increasing the oxygen pressure and/or by providing additional mixing capacity, such as by the use of larger mixers, or connecting a number in mixers in parallel. Further as used throughout the specification and the claims "turbu¬ lent mixer" means a device, usually an elongated tubular, cylindrical or any other cross-section member having a hollow interior containing vanes or other flow-directing elements for causing turbulent flow therein to create a mixing effect in liquid flowing within the device. A turbulent mixer can suitably be a static mixer in which the flow directing elements are in a stationary or fixed position, or a dynamic mixer in which some or all of the elements can either freely rotate, or be rotated by a drive to intensify the mixing effect. It was surprisingly found that application, whereas water prepared by the aforementioned U.S. patent application No. 08/441,708 could produce a dissolved oxygen level of about 60-65 mg/£ which will reach the atmospheric equilibrium level of about 10-12 mg/£ within about 24 hours, the water oxygenated by the use of a four simple series-connected static mixers in accordance with the present invention, when initially containing about 70 mg/£, will lose the amount of oxygen to the equilibrium levels in about 48 hours. The reason for this slower oxygen loss is not known, but the process and apparatus of the present invention produce not only higher oxygen concentrations, but even more importantly, the oxygen losses to the ambient atmosphere of waters prepared by the present inventions are slower, at about half the rate of water oxygenated in accordance with the prior art. It is believed that the thorough mixing which results in a greater amount of oxygen being more thoroughly dissolved in the water, might account for that slower oxygen degassing loss. It is believed that the present invention could be employed to obtain even substantially higher dissolved oxygen levels than 70 mg/£, such as by slower feed through flow rates and/or improving the entire mixing efficiency, such as employing filters connected in parallel and/or using dynamic mixers in which the mixer elements are rotated to intensify the mixing effect. Since it is expected that the loss of dissolved oxygen under ambient atmospheric conditions increases as far as the added amounts of dissolved oxygen are concerned, it is very likely to find a dissolved oxygen concentra- 7/27146 -7- tion (break-even level) above which under atmospheric conditions the loss of the increased amount of oxygen would be so fast that the cost and the effort may not match the benefit of incoφorating such higher amounts of oxygen on an industrial scale. This does not necessarily apply to sealed bottles of highly oxygenated water or other beverages, because that can maintain its oxygen content under pressure practically indefinitely. This break-even level, however, is expected to be considerably above the about 70 mg/£ concentra¬ tion that has been so far routinely obtained on an industrial scale with relatively little effort in accordance with the present invention. In the case of the treatment of groundwaters the highly oxygenated water is reinjected into an injection well immediately up-gradient of the contaminated plume. As the injection is made several feet below the water level in the injection well, any turbulence at the atmosphere-water interface can be kept to a minimum. Typically the oxygenated water penetrates into the surrounding porous media over several hours after injection, with a substantial minimum of turbulence due to the slow flow rate. Once the highly oxygenated water penetrates the contaminated aquifer, very little oxygen degassing is expected due to the combination of hydrostatic pressure, the low velocity nonturbulent flow conditions, and the rapid microbe utiliza- tion of the dissolved oxygen. Therefore, most of the oxygen is used for microbial respiration rather than is lost due to pore degassing. It is expected that, depending on the operational parameters, from about 35 to about 110 mg/£ oxygen can be incoφorated into water in accordance with the present invention. Typically, the use of a four static mixer tube apparatus of the present invention, each with a 2" ID could conveniently produce up to 100,000 gallons of water per day. The oxygen in water input can be adjusted over a very wide range, such as to obtain a dissolved oxygen concentration of between about 65 and about 70 mg/£. The present invention is suitable for treating all waste waters which create a high demand for oxygen. However, the process and apparatus of the present invention are also suitable for use in aerobic processes and other processes such as therapeutic processes advantageously employing oxygen containing liquids. As used throughout the specification and the claims, reference to an "aerobic" process generally includes all chemical and microbiological pro- cesses in which such a process is carried out or is promoted in a liquid medium in the presence of oxygen. As used throughout the specification and the claims "therapeutic" processes involve the oxygenation of the body or its parts by treatment with an agent in a liquid vehicle containing dissolved oxygen. Suitably aerobic processes in which water oxygenated in accordance with the present invention can be employed include for example processes in which heretofore water has been aerated such as by bubbling air thereinto, and also in situ or ex situ bioremediation of contaminated (e.g. with petro¬ leum products) surface and ground waters; wastewater, sludge, and animal waste treatment, both by fixed film and by suspended growth methods; rehabilitation of atrophying lakes; biochemical oxygen demand (BOD) measurement techniques; fresh water aquaculture (e.g. fish farming); odor suppression barriers for anaerobic processes; and insolubilization of dissolved contaminants (e.g. Fe., and Mn ions) for removal by filtration or sedimenta- tion. In view of the particularly good oxygen retention of liquids oxygen¬ ated by the present invention kept in containers, a particularly advantageous new aerobic use of those liquids was discovered. In accordance with a further feature of the present invention such oxygenated liquids can be advantageously employed as the fermentation liquor of all kinds of fermenta¬ tion processes, such as drug production or food processing by microorganisms. Microorganisms such a bacteria consume massive quantities of oxygen in the process of a assimilating or breaking down waste. The rate at which oxygen can be introduced into the biomass, is a substantial limiting factor on how quickly a breakdown by oxygenation can be achieved. The problem with the known process technologies is that oxygen introduction by aeration is highly inefficient because air contains only 21% percent oxygen and thus 79% percent of the energy used by aerators is wasted in pumping useless nitrogen. Therefore, the use of highly oxygenated water in accordance with the present invention in such aerobic processes is expected to be about 5 times more efficient, also to obtain thereby a like extent of energy efficiency improve¬ ment. Thus the infusion of water with 40-50 mg/£ of oxygen allowed a considerably more efficient and much more rapid aerobic treatment, com¬ pared to 7-10 mg/£ for the normal oxygen content of water, and just slightly more when a conventional bubbling aerator is used with 20% oxygen contain¬ ing air. Furthermore, as the equilibrium oxygen content of water is used up, its dissolved oxygen content rapidly decreases. Suitable therapeutic processes in which liquids made in accordance with the present invention can be advanteously employed include, for exam- pie, increasing the oxygen content of blood and tissues; oxygenation of wounds to increase the rate of healing and to reduce infections; oxygenated organ transplant storage media; tumor oxygenation for radiation therapy and chemotherapy; lung bypass by oxygenated liquids in case of pulmonary deficiencies; carbon monoxide poisoning; mouthwashes, dentrifices; topical, including cosmetic, treatment media; contact lens treating solutions; and cell level therapeutic applications. Eight test subjects of various ages and of differing sex, had their blood oxygen contents and their pulse rates determined. Each subject drank between Vi and 3 λ liters of highly oxygenated water. Evidence of a pulmo¬ nary function bypass was observed a short period after ingestion, by an average blood oxygen increase of about 30%, and the effect of a concomitant cardiac relief was observed through an average of about 10% pulse rate reduction. In view of the especially good oxygen retention of liquids oxygenated by the present invention kept in containers, a particularly advantageous new therapeutic product of those liquids was discovered. In accordance with a further feature of the present invention such oxygenated liquids can be employed as solvents for physiological saline isotonic solutions, especially when kept in sealed, sterile containers. If desired, the water treated in accordance with the present invention can also be made effervescent by the addition of a gas such as carbon dioxide. If the carbon dioxide is added after the dissolution of the oxygen in the water, then it will displace a portion of the dissolved oxygen. It has been found, however, that the effervescent liquid can be further enriched with oxygen to a substantial degree after the addition of the carbon dioxide. Even more oxygen can be dissolved in the water, if the water being enriched with the oxygen is chilled at the time of the oxygen enrichment. However, some of the chilling or the entire lack of chilling can be substituted by the employ¬ ment of higher oxygen pressures such as around 50 psi or higher. An apparatus in accordance with the present invention oxygenating water at an experimental fish farm, where the fish did not require the maintenance of elevated oxygen levels, but only the maintenance of dissolved oxygen concentration of about 9-12 mg/£, the cost of the required power was about 8 cents per hour, and the overall cost per kilogram of dissolved oxygen produced was about 79 cents per kilogram dissolved oxygen. In another experiment highly concentrated formate/acetate industrial effluent waste streams were treated, having an approximate biological oxygen demand (BOD =10,000 mg £), were successfully treated so that the aerobic biodegradation of the waste stream, even before process optimization, was able to achieve an 80% reduction in total organic carbon levels in less than three hours of intense treatment. Thus the use of the apparatus in accor- dance with the process of the present invention results in a very inexpensive and very efficient technique. Therefore, the evidence is present that the present invention is more suitable for oxygenating and super oxygenating liquids, than the techniques air sparging, electrolysis, hydrogen peroxide, pumping and other methods known from the prior art. Oxygen concentrations in the oxygenated water prepared in accor¬ dance with the present invention were measured with a Model 830 and a Model 840 dissolved oxygen meters sold by ATI Orion Analytical Technology, Inc. When the two meters were at the same location, they were used to compare the measurements which have been found to correlate satisfactorily. Brief description of the drawing The invention is described in greater detail with reference being had to the enclosed drawing, wherein Fig. 1 is a plan view of the apparatus of the present invention; Fig. 2 shows four ganged turbulent mixer elements; Fig. 3 is a plan view of an oxygen mixing venturi; Fig. 4 is a schematic showing of a dynamic mixer; Fig. 5 is a schematic showing of turbulent mixers connected in series; and Fig. 6 is a schematic showing of turbulent mixers connected in parallel and the parallel mixers are connected in series. Detailed description of the invention Fig. 1 shows the oxygen - saturating apparatus of the present inven¬ tion. Water is introduced through a water inlet 1 which is suitably a 1.5 inch OD pipe. Oxygenated water exits from the system through a water outlet 3, suitably a 1" OD pipe. The water can be lead to the apparatus through the inlet 1 from the water mains, or a water supply tank (not shown), and the like. Suitably the water is passed through a basket strainer 5 to remove any solid contaminants, particularly if the starting water is a wastewater or a recirculated water. From the basket strainer 5 the water passes through a pump 7 which further feeds the input water at a uniform pressure into the apparatus. When the oxygenated water removed at the water outlet 3 is re¬ moved periodically, such as when the oxygenated is bottled, upon the cessa- tion of flow at the outlet 3, a backflow pressure regulator 9 opens and recirculates the input water along the path indicated by the broken line to the water inlet 1, or to the optional water supply tank from where the input water may be drawn. When the water pressure at the water outlet 3 is above a certain value, the back-flow pressure regulator 9 is closed and the pump passes the water into the oxygenation apparatus through an apparatus input 11 and a unidirectional flow-assuring check valve 13. The operation of the pump 7 is regulated by a pump control panel 15, and its associated conventional circuity. Oxygen input to the apparatus occurs at 17 through a venturi mixer 19. The oxygen flow can be obtained from many convenient sources, suitably from an oxygen generator manufactured by Airsep Coφ. The simple Airsep oxygen generator produces about 45 ft 3 /hr 0 2 at about 50-55 psi. This requires at water pressure the output of the pump 7 of about 70 psi. In the case of a higher oxygen input pressure to the venturi mixer 19 the output water pressure of the pump 7 may not need to be as high. If a higher O 2 production rate is desired, a more productive 0 2 generator, or more 0 2 generators connected in parallel can be used. The venturi mixer 19 distributes the oxygen input in the water flow as bubbles and also as some amount of oxygen dissolved in the water flowing through the venturi mixer from where the water is passed to four turbulent mixers connected in series. In Fig. 1 the first two turbulent mixers are static mixers 21, and the last two mixers in the series connection are dynamic mixers 23. The static mixers 21 are suitably 2" ID tubular units sold under the trademark Komax by Ryan Harco Co. The dynamic mixers 23, in contrast with the static mixers 21, have rotary mixing vanes that are rotated inside the mixers by an exterior driving motor M (see Fig. 4). The design of the rotating mixer elements, and their speed of rotation determines the intensity of the mixing that takes place within the dynamic mixer. The 7/27146 PC17US96/00037 -14- intensity of mixing taking place in the static filters 21 depends on the resul¬ tants of the introduced water pressure and oxygen pressure and the design features of the interior mixing vanes. The mechanical agitation which takes place to varying degrees within the various types of turbulent mixers 21 and 23 forces the thorough incoφoration of the oxygen in the water. The water exiting the last mixer 23 passes through a bubble remover 25 in which a pipe (not shown) ranges below the water level of the water flowing through the remover, and any free, undissolved oxygen bubbles rise through the pipe and are recirculated along the broken line to the oxygen input 17. The amount oxygen entering through the oxygen input 17, includ¬ ing the oxygen recirculated from the bubble remover, can be monitored by an oxygen flow meter 27. After the bubble remover 25, the oxygen-saturated water passes through a pressure gauge 29 to an output backflow regulator 31. The output back flow regulator 31 has only a limited throughput of about 25 gallons per minute. Therefore, a regulator bypass valve 33 passes the smaller amount of throughput through the bypass that is in excess of the regulator throughput. The provision of such a bypass is a simpler and less expensive solution, than the use of a higher throughput backflow regulator which is disportionately expensive. The output of the regulator 31 and the water passing through the bypass valve 33, exit from the apparatus through the water outlet 3. The role of the regulator 31 is to close and bar most or all of the outflow of oxygenated water through the outlet 3. This takes place when the pressure in the sealed enriching space falls below a preset value, suitably about 40 psi. Such pressure loss can occur in the turbulent mixers for example, when too much oxygenated water has passed through the outflow 3. In that case, the output backflow regulator 31 closes to prevent most of all of the outflow of 97/27146 -15- oxygenated water from the system. The pressure within the sealed enriching space thereupon rapidly increases and this results in the input backflow pres¬ sure regulator 9 shutting down, and the input water begins to recirculate to the water inlet 1. If any valves on the output side of the apparatus are closed, then no oxygenated water will leave the system while the outlet backflow regulator 31 is closed. If, on the other hand, any valves on the output side are open, except for the outlet backflow regulator 31, only a relatively minor proportion of the oxygenated water passes through the regulator bypass valve 33, and the required pressure buildup within the sealed enriching space remains assured. Fig. 2 shows the design of a suitable turbulent mixer 35, in which static mixers 21 are connected alternately in series with dynamic mixers 23. The mixer 35 contains a plurality mixers, each containing twisted elements. The mixers are arranged axially and alternatingly within the cyhndrical body. Some elements are twisted for example clockwise, and some of the other elements can be twisted counterclockwise, or vice versa, when they are viewed from the inlet side of the mixer 35. The venturi mixer 19 is shown in greater detail in Fig. 3 with the oxygen entering through the oxygen input 17 with an optional extra oxygen outlet 37 for optional extra introduction of oxygen at some other desired point into the system, a water input 39, and a water with oxygen output 41. The operating principle of a dynamic mixer is schematically shown in Fig. 4, where a dynamic mixer element 23 is adapted to rotate inside the dynamic filter, as driven by a motor M. Suitably the speed of the motor M is variable to permit an adjustment of the mixing intensity of the dynamic mixer 23. Figs. 5 and 6 are schematic showings of turbulent filter elements connected in parallel and connected in parallel and in series, respectively.

Claims: We claim: 1. In a process for enriching water with oxygen, which comprises conducting water through a water inlet into a sealed enriching space, introducing oxygen through an oxygen inlet into the water in the enriching space, and recovering the oxygen-enriched water, the improvement which comprises said enriching space includes a turbulent mixer, and conduct- ing the water with oxygen through said turbulent mixer for incoφorating the oxygen into the water, before recovering the oxygen-enriched water. 2. The process of claim 1 wherein a plurality of turbulent mixers are employed. 3. The process of claim 2, wherein said plurality of turbulent mixers comprises a plurality of static mixers, a plurality of dynamic mixers, or a combination of one or more static mixers with one or more dynamic mixers. 4. The process of claim 2, wherein said plurality of turbulent mixers are connected in series with each other. 5. The process of claim 1, wherein said plurality of turbulent mixers are connected in parallel with each other. 6. The process of claim 2, wherein said turbulent mixer is a first turbulent mixer or mixers connected in series with one or more second turbulent mixers, said second turbulent mixers being a plurality of parallel- connected turbulent mixers. 7. The process of claim 2, wherein each of said turbulent mixers has an inside diameter between about 0.5" and about 5". 8. The process of claim 6, wherein four turbulent mixers are connected in series each having an inside diameter between about 0.75" and about 2". 9. The process of claim 1, wherein said enriching space has a venturi for the introduction of the oxygen into the water before substantially dissolving the introduced oxygen in the water in said turbulent mixer. 10. The process of claim 9, further comprising after said substantially dissolving, removing undissolved oxygen before the recovering the oxygen enriched water. 11. The process of claim 9, wherein said removing comprises after said turbulent mixer conducting the oxygen enriched water through a bubble remover where bubbles of undissolved oxygen are removed, and returning the so removed oxygen to the oxygen inlet. 12. A liquid enriched with oxygen by the apparatus of claim 25. 13. An aerobic process which comprises carrying out a chemi- cal or microbiological reaction in an oxygen enriched liquid as the reaction medium, the liquid having been prepared by the process of claim 1. 14. A therapeutic process which comprises carrying out a therapeutic treatment of a body with an agent comprising an oxygen enriched liquid as a vehicle, the liquid having been prepared by the process of claim 1. 15. An aerobic process which comprises carrying out a chemi- cal or microbiological reaction in an oxygen enriched liquid as the reaction medium, the liquid having been prepared with the apparatus of claim 25. 16. A therapeutic process which comprises carrying out a therapeutic treatment of a body with an agent comprising an oxygen enriched liquid as a vehicle, the liquid having been prepared with the apparatus of claim 25. 17. An aerobic process which comprises carrying out a chemi- cal or microbiological reaction in the oxygen enriched liquid of claim 12 as the reaction medium. 18. A therapeutic process which comprises carrying out a therapeutic treatment of a body with the oxygen enriched liquid of claim 12 as a vehicle. 19. An aerobic process which comprises carrying out a chemi- cal or microbiological reaction in the oxygen enriched liquid of claim 12 as the reaction medium. 20. A therapeutic process which comprises carrying out a therapeutic treatment of a body with an agent comprising the oxygen en- riched liquid of claim 12 as a vehicle. 21. A fermentation process which comprises using as the fermentation liquor the oxygen enriched liquid of claim 12. 7/27146 PC17US96/00037 -20- 22. A physiological saline solution which comprises as the solvent the oxygen enriched liquid of claim 12. 23. A fermentation process which comprises using as the fermentation liquor the oxygen enriched liquid of claim 12. 24. A physiological saline solution which comprises as the solvent the oxygen enriched liquid of claim 12. 25. In an apparatus for enriching water with oxygen, which comprises a water inlet, an oxygen inlet, a sealed enriching space, and an outlet for oxygenated water, the improvement which comprises said sealed enriching space including said oxygen inlet and a turbulent mixer. 26. The apparatus of claim 25, wherein said turbulent mixer comprises a plurality of turbulent mixers. 27. The apparatus of claim 26, wherein said plurality of turbulent mixers comprises static mixers, or dynamic mixers, or a combination of static mixers and dynamic mixers. 28. The apparatus of claim 27, wherein said mixers are connected in parallel, in series, or in parallel and in series. 29. The apparatus of claim 26, wherein said plurality of turbulent mixers are connected in parallel with each other. 30. The apparatus of claim 26, wherein said turbulent mixer is a first turbulent mixer or mixers connected in series with one or more second turbulent mixers, said second turbulent mixers being a plurality of parallel- connected turbulent mixers. 31. The apparatus of claim 26, wherein each of said turbu- lent mixers has an inside diameter between about 0.5" and about 5". 32. The apparatus of claim 28, wherein four turbulent mixers are connected in series each having an inside diameter between about 0.75" and about 2". 33. The apparatus of claim 26, wherein said enriching space has a venturi for the introduction of the oxygen into the water before substantially dissolving the introduced oxygen in the water in said turbulent mixer. 34. The apparatus of claim 33, further comprising a water in- put pump between said water inlet and said venturi. 35. The apparatus of claim 34, further comprising a water ba- ckpressure regulator between said pump and said venturi, and a bypass for unoxygenated water for recirculating the unoxygenated water to said water inlet, when the pressure within said sealed enriching space rises above a predetermined level. 36. The apparatus of claim 33, further comprising a bubble remover in said sealed enriching space, between said turbulent mixer and said outlet for removing oxygen bubbles from the oxygenated water, and an oxygen bypass for recirculating said oxygen bubbles to said venturi. 37. The apparatus of claim 26, further comprising an oxygen- ated water backpressure regulator having a throughput capacity, and an oxygenated water bypass for bypassing said oxygenated backpressure regulator when the outflow of oxygenated water from said sealed enriching space exceeds said throughput capacity. 38. The apparatus of claim 37, wherein said oxygenated water backpressure regulator is adapted to close to the outflow of oxygenated water when the pressure in said sealed enriching space falls below a preselected value. AMENDED CLAIMS [received by the International Bureau on 26 May 1996 (26.05.96); original claims 1, 25 and 36 amended; remaining claims unchanged (4 pages)] 1. In a process for enriching water with oxygen, which comprises conducting water through a water inlet into a sealed enriching space, introducing oxygen through an oxygen inlet into the water in the enriching space, and recovering the oxygen-enriched water, the improvement which comprises said enriching space being under an oxygen pressure of at least 40 psi, and said enriching space including a turbulent mixer and a bubble remover, conducting the water with oxygen through said turbulent mixer for incorporating the oxygen into the water, and removing oxygen bubbles from the oxygen containing water before recovering the oxygen- enriched water containing at least 40 mg/£ oxygen. 2. The process of claim 1 wherein a plurality of turbulent mixers are employed. 3. The process of claim 2, wherein said plurality of turbulent mixers comprises a plurality of static mixers, a plurality of dynamic mixers, or a combination of one or more static mixers with one or more dynamic mixers. 4. The process of claim 2, wherein said plurality of turbulent mixers are connected in series with each other. 5. The process of claim 1, wherein said plurality of turbulent mixers are connected in parallel with each other. 6. The process of claim 2, wherein said turbulent mixer is a first turbulent mixer or mixers connected in series with one or more second turbulent mixers, said second turbulent mixers being a plurality of parallel- connected turbulent mixers. 22. A physiological saline solution which comprises as the solvent the oxygen enriched liquid of claim 12. 23. A fermentation process which comprises using as the fermentation liquor the oxygen enriched liquid of claim 12. 24. A physiological saline solution which comprises as the solvent the oxygen enriched liquid of claim 12. 25. In an apparatus for enriching water with oxygen to an oxygen concentration of at least 40 mg/£ under an oxygen pressure of at least 40 psi, which comprises a water inlet, an oxygen inlet, a sealed enriching space, and an outlet for oxygenated water, the improvement which comprises said sealed enriching space including said oxygen inlet, a turbulent mixer, and a bubble remover for removing oxygen bubbles from the oxygenated water. 26. The apparatus of claim 25, wherein said turbulent mixer comprises a plurality of turbulent mixers. 27. The apparatus of claim 26, wherein said plurality of turbulent mixers comprises static mixers, or dynamic mixers, or a combination of static mixers and dynamic mixers. 28. The apparatus of claim 27, wherein said mixers are connected in parallel, in series, or in parallel and in series. 29. The apparatus of claim 26, wherein said plurality of turbulent mixers are connected in parallel with each other. 30. The apparatus of claim 26, wherein said turbulent mixer is a first turbulent mixer or mixers connected in series with one or more second turbulent mixers, said second turbulent mixers being a plurality of parallel- connected turbulent mixers. 31. The apparatus of claim 26, wherein each of said turbu- lent mixers has an inside diameter between about 0.5" and about 5". 32. The apparatus of claim 28, wherein four turbulent mixers are connected in series each having an inside diameter between about 0.75" and about 2". 33. The apparatus of claim 26, wherein said enriching space has a venturi for the introduction of the oxygen into the water before substantially dissolving the introduced oxygen in the water in said turbulent mixer. 34. The apparatus of claim 33, further comprising a water in- put pump between said water inlet and said venturi. 35. The apparatus of claim 34, further comprising a water ba- ckpressure regulator between said pump and said venturi, and a bypass for unoxygenated water for recirculating the unoxygenated water to said water inlet, when the pressure within said sealed enriching space rises above a predetermined level. 36. The apparatus of claim 33, wherein said bubble remover is disposed in said sealed enriching space between said turbulent mixer and said outlet, and an oxygen bypass for recirculating said oxygen bubbles to said venturi. 37. The apparatus of claim 26, further comprising an oxygen- ated water backpressure regulator having a throughput capacity, and an oxygenated water bypass for bypassing said oxygenated backpressure regulator when the outflow of oxygenated water from said sealed enriching space exceeds said throughput capacity. 38. The apparatus of claim 37, wherein said oxygenated water backpressure regulator is adapted to close to the outflow of oxygenated water when the pressure in said sealed enriching space falls below a preselected value. STATRMENT UNDER ARTICLE 19 Static or motionless cocurrent mixers are conventional devices for promoting the inline gassing of liquids in small diameter columns, such as with oxygen, for wastewater treatment. However, none of the references singly, or combined teach or suggest the incoφoration and maintenance of high levels of at least 40 mg/£ oxygen in water by incoφorating oxygen into the water under a pressure of at least 40 psi with a static or dynamic mixer and removing the large, undissolved bubbles of oxygen from the water. U.S. patent No. 5.200.080 discloses liquid waste biotreatment by recirculating the waste through an oxygenator to a lagoon or tank. The two-phase gas/liquid mixture passes through turbulence-creating reduced diameter portion to provide for equal distribution of the components of the mixture in the following branch point of the pipe. Part of the two-phase mixture continues and another part branches off to V enturis. In each branch the oxygen water mixture is further intermixed with V enturis installed far from the shoreline in the lagoon and submerged at least 10 feet below the lagoon surface. The outflow from each branch is diluted in an approximately 3:1 ratio with unoxygenated wastewater from the lagoon in a liquid/li¬ quid venturi, whereby the oxygenated water is mixed with a greater amount of unoxygenated water thus diluting the oxygen content with the greater volume of unoxygenated water to produce a lower oxygen concentration than the saturation oxygen concentration under atmospheric pressure, and thus maintaining a constant, only low level of dissolved oxygen. U.S. Patent Nn. 5.167.806 describes bubble-forming flotation clarification of a contaminated liquid wastewater by dissolving gases in a high speed rotating swirling liquid in an enclosed pressure vessel, from where the mixture is released to form fine bubbles for flotation. Any gas, including air, oxygen, nitrogen, CO 2 , ozone and other gases or several gases at the same time, can be used for foam formation. U.S. Patent Nn- 5.013.429 separates sludge by settling or flotation after a flocculent was added, then water is removed to pre-thicken the solids content, then is acidified in a second mixer to remove heavy metals, and is introduced in a sludge stabilizing tank with a rotating mixer of full tank size to stir up the sludge in the tank and to intensify mixing of the sludge with gas bubbles sparged in at the bottom to stabilize the sludge that is then withdrawn. U.S. Patent Nn 4,695.378 employs an aerating venturi and a static mixer to neutralize and replenish by aeration the depleted oxygen level in the acid mine drainage to a normal level and to oxidize the metal content to higher oxidation state prior to the removal of the metal contaminant.

Inventors: ABRAMOFF FRANK, TAYLOR DARRELL L, ABRAMOFF, FRANK, TAYLOR, DARRELL, L.
Applicants: ABRAMOFF FRANK, LIFE INT PRODUCTS INC, TAYLOR DARRELL L, ABRAMOFF, FRANK, LIFE INTERNATIONAL PRODUCTS, INC., TAYLOR, DARRELL, L.
Application year: 1996
Main classification: C02F1
IPC codes: A01N59, A23L2, A61K33, B01F3, B01F5, C02F1, C02F3, C12M1