WO1998046340A1 - Systeme et procede de delivrance de fluides sursatures en gaz - Google Patents

Systeme et procede de delivrance de fluides sursatures en gaz Download PDF

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Publication number
WO1998046340A1
WO1998046340A1 PCT/US1998/007671 US9807671W WO9846340A1 WO 1998046340 A1 WO1998046340 A1 WO 1998046340A1 US 9807671 W US9807671 W US 9807671W WO 9846340 A1 WO9846340 A1 WO 9846340A1
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WO
WIPO (PCT)
Prior art keywords
gas
fluid
exchanger
pressure
source
Prior art date
Application number
PCT/US1998/007671
Other languages
English (en)
Inventor
J. Richard Spears
Richard J. Crilly
Original Assignee
Wayne State University
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Wayne State University filed Critical Wayne State University
Priority to AU74670/98A priority Critical patent/AU7467098A/en
Priority to CA002286653A priority patent/CA2286653A1/fr
Priority to JP54429098A priority patent/JP2001520575A/ja
Priority to EP98922038A priority patent/EP1009518A1/fr
Publication of WO1998046340A1 publication Critical patent/WO1998046340A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/20—Measuring; Control or regulation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/20—Measuring; Control or regulation
    • B01F35/22—Control or regulation
    • B01F35/221—Control or regulation of operational parameters, e.g. level of material in the mixer, temperature or pressure
    • B01F35/2213—Pressure

Definitions

  • the present invention generally relates to a system and method for delivering gas-supersaturated fluids. More specifically, the present invention relates to a system and method for delivering gas-supersaturated fluids to a gas- depleted site without the premature formation of bubbles.
  • a gas-enriched fluid to a site of interest, and/or increase the gas concentration of a fluid without a significant increase in the fluid volume.
  • a fire may be extinguished by delivering an inflammable or an inert gas, such as carbon dioxide or nitrogen, rapidly to the fire via a fluid transporting medium.
  • Environmental problems presented by toxic site cleanups may be ameliorated by delivering a high concentration of a neutralizing or cleansing gaseous agent to the toxic site.
  • the oxygenation level of ponds used in fish farms, and the oxygenation level of waste streams may also be increased by delivery of oxygen-enriched fluids to the ponds or streams.
  • One method of obtaining an increase in the gas concentration level without significant increase in fluid volume is by directly pumping a desired gas into a fluid site of interest.
  • direct pumping is not always efficient and may thereby result in an insufficient increase in gas concentration.
  • a noxious gas is used, direct pumping also poses waste engineering problems and/or health hazard due to the presence of any unabsorbed noxious gas .
  • Another method of obtaining an increase in the gas concentration level without significant increase in fluid volume is by infusing a gas-enriched fluid, such as a gas- supersaturated fluid, into the site of interest.
  • a gas-enriched fluid such as a gas- supersaturated fluid
  • Prior art systems for producing gas-supersaturated fluids typically require the use of a high pressure vessel to provide dwell time for dissolving gas nuclei in the fluid outputted from the high pressure gas exchanger.
  • Two such prior art systems are U.S. Pat. No. 5,407,426, "Method and Apparatus For Delivering Oxygen Into Blood" to Spears and U.S. Pat. No. 5,569,180, "Method For Delivering A Gas-Supersaturated Fluid To A Gas- Depleted Site And Use Thereof" to Spears.
  • gas nuclei may be present in the fluid prior to supersaturating the fluid with gas.
  • gas nuclei may be dust particles suspended in the fluid or crevices in the container wall in which gas is trapped or absorbed.
  • the presence of gas nuclei facilitates cavitation inception (or, bubble formation) , resulting in release of gas from the liquid and thereby decreasing the gas concentration of the fluid.
  • cavitation inception may occur because ejection of the fluid into an atmospheric environment results in a decrease in the hydrostatic pressure of the fluid below the gas partial pressure. Disturbances at or near the exit ports may further facilitate cavitation inception.
  • gas is released from the fluid, decreasing its gas concentration.
  • the presence of bubbles in the fluid generates turbulence and impedes the flow of the fluid beyond the exit ports.
  • a system and method for delivering gas-enriched fluid to a site of interest includes a fluid reservoir, a fluid pump, a gas source, a high pressure gas exchanger, and one or more arrays of capillary channels for delivery of gas-supersaturated fluid.
  • Differential pressure gauges and other suitable controls may be provided to maintain a near constant hydrostatic pressure of the fluid throughout the delivery system that is approximately 1% to 20% higher than the gas pressure within the housing of the high pressure gas exchanger.
  • the delivery system may also include a fluid filter for filtering the fluid before it enters the fluid reservoir.
  • the system and method of the present invention requires relatively low hydrostatic pressures and eliminates the need for a high pressure vessel for providing a dwell time for dissolving gas nuclei in the fluid.
  • the system and method of the present invention also eliminates the need for a high pressure fluid pump for high output delivery of the gas-supersaturated fluid.
  • the system and method of the present invention reduces or eliminates gas nuclei on the inner surface of the exit ports through which the gas- supersaturated fluid exits, in part by providing exit ports with a relatively small diameter.
  • FIG. 1 shows a system for delivery of gas- supersaturated fluids according to a preferred embodiment.
  • FIG. 2 shows a system for delivery of gas- supersaturated fluids according to an alternative embodiment.
  • delivery system 10 includes fluid reservoir 12, fluid pump 14, gas source 16, high pressure gas exchanger 18, delivery tube 36, and one or more arrays of capillary channels 20.
  • High pressure gas exchanger 18 preferably includes an outer gas tight housing surrounding semi-permeable membrane gas-fluid interface 26, such as an oxygenator, which comprises a gas permeable and at least substantially fluid impervious container.
  • Differential pressure gauge 22 is provided to measure the difference between the gas pressure in interior 40 and the hydrostatic pressure within gas-fluid interface 26.
  • Differential pressure gauge 22 and other suitable controls are provided to maintain a near constant hydrostatic pressure within gas- fluid interface 26 approximately 1% to 20%, higher than the gas pressure in interior 40 within housing 34 of high pressure gas exchanger 18. The higher hydrostatic pressure within gas-fluid interface 26 facilitates the dissolution of gas in the fluid in interior 40.
  • Delivery system 10 may also include a fluid filter 24 to filter fluid before it enters fluid reservoir 12.
  • Fluid filter 24 is preferably a standard, commercially available filter such as porous sintered metal filters manufactured by Mott Metallurgical.
  • Fluid pump 14 pumps fluid from fluid reservoir 12 into gas-fluid interface 26 via input tube 28.
  • gas-fluid interface 26 is located within gas exchanger 18 surrounded by gas containing interior space 40.
  • Gas-fluid interface 26 preferably incorporates silicone, such as silicone membranes or silicone tubules, as the gas exchanging media. Hollow microporous polypropylene tubes may also be used as a gas exchanging media.
  • gas source 16 contains a corrosive gas such as ozone
  • gas- fluid interface 26 is made of corrosive resistant materials such as certain plastics, stainless steel, glass, Kevlar, silicone, silicone rubber or platinum, and gold plated soft metal seals may also be utilized.
  • Output 30 of gas-fluid interface 26 is coupled to output 32 of high pressure gas exchanger 18, which is in turn coupled to output tube 36. Fluid exits output tube 36 via capillary channels 20.
  • Capillary channels 20 are preferably cylindrical, and have a relatively small diameter which helps to stabilize the gas supersaturated fluid upon ejection.
  • Capillary channels 20 may also have slit-like, rectangular, square, triangular, and annular cross-sectional shapes. Where channels 20 have a circular cross-section, the inner diameter of each of capillary channels 20 is preferably within the approximate range of 25 to 300 ⁇ m. Using capillary channels with inner diameters of less than about 25 ⁇ m is possible, but may require a large number of such channels to be used to compensate for the higher flow resistance.
  • capillary channels with inner diameters of less than about 25 ⁇ m may also increase the likelihood that such channels will become blocked with particulates .
  • the use of capillary channels with inner diameters larger than about 300 ⁇ m may not effectively stabilize fluids supersaturated gases, such as oxygen, at high partial pressures.
  • Capillary channels 20 are preferably non- hydrophobic with a smooth inner surface.
  • plastic channels such as polyimide channels
  • metal channels such as stainless steel channels
  • glass or silica channels generally provide a smoother inner surface, are less expensive to obtain commercially, and large arrays of parallel glass or silica channels ⁇ can be easily fabricated. Moreover, large numbers of parallel channels within glass plates may also be easily obtained commercially.
  • Glass and silica provide the additional benefit of being chemically inert in many environments, and thus are less likely to react with the gas-supersaturated fluid. Glass and silica channels can also be cleaned with harsh solvents with little or no damage.
  • gas is delivered from gas source 16 to interior 40 of high pressure gas exchanger 18 via gas input tube 38.
  • gas within interior 40 of high pressure gas exchanger 18 is maintained at a pressure of approximately 8 to 50 bar.
  • Differential pressure gauge 22 and other suitable controls are provided to maintain a near constant hydrostatic pressure within gas-fluid interface 26 approximately 1% to 20% higher than gas pressure within interior 40 of high pressure gas exchanger 18. More preferably, the near constant hydrostatic pressure within gas-fluid interface 26 is approximately 9 to 51 bar, which is slightly higher than the gas pressure within interior 40 of high pressure gas exchanger 18.
  • One example of a suitable control is to adjust the rate of the fluid flow from fluid pump 14 into gas-fluid interface 26.
  • Pressure differential gauge 22 may provide electrical signals to fluid pump 14 and/or to gas source 16 via electrical signals carrier 48.
  • fluid flow rate from fluid pump 14 would be adjusted accordingly so as to achieve and maintain proper hydrostatic pressures within gas- fluid interface 26 and proper pressure differences between the hydrostatic pressure and the gas pressure within interior 40.
  • Another example of a suitable control is to adjust the rate of the fluid flow from gas exchanger 18 to the site of interest by adjusting fluid valve 23 so as to achieve and maintain proper hydrostatic pressures within gas-fluid interface 26 and proper pressure differences between the hydrostatic pressure and the gas pressure within interior 40.
  • differential pressure gauge 22 regulates the gas flow rate from gas source 16 and regulates a gas release valve (not shown) for selective release of gas from within gas exchanger 18 in order to vary the fluid flow rate from gas exchanger 18.
  • the peak hydrostatic pressure required for the fluid in delivery system 10 i.e. fluid in input tube 28, gas-fluid interface 26, and delivery tube 36
  • the peak hydrostatic pressure required for the fluid in delivery system 10 is approximately 1% to 20% higher than the gas partial pressure
  • overt gas pockets in the gas-supersaturated fluid do not create active, bubble generating gas nuclei at the tube- liquid interface.
  • the pressure differential prevents generation of active, bubble generating gas nuclei, the need for a dwell time for dissolving gas nuclei in the fluid and the corresponding need for a high pressure vessel to provide the dwell time are eliminated.
  • delivery system 10 may be configured such that gas-deficient fluid pumped by fluid pump 14 can bypass high pressure gas exchanger 18 via bypass tube 42 and be delivered to capillary channels 20 via output tube 36, for initial flushing of capillary channels 20.
  • Delivery system 10 may further provide valves 44, 46 which may be in an initial bypass position or an operational position. During the initial flushing, valves 44, 46 are in the initial bypass position which allow fluid to flow from input tube 28 directly to output tube 36 via bypass tube 42 and prevent fluid from entering high pressure gas exchanger 18. After the initial flushing procedure, valves 44, 46 are in the operational position which allow fluid to flow from input tube 28 to output tube 36 via high pressure gas exchanger 18 and prevent fluid from entering bypass tube 42.
  • This procedure of flushing capillary channels 20 facilitates elimination of surface nuclei within capillary channels 20 because the surface gas nuclei can be relatively easily absorbed by the gas-deficient fluid and because the velocity of the fluid flow through channels 20 may result in flushing out the surface gas nuclei from channels 20.
  • the initial flushing procedure may be used to facilitate high volume delivery of gas-supersaturated fluid to the site of interest without cavitation inception despite a relatively low hydrostatic pressure of approximately 9 to 51 bar. Delivery of gas-supersaturated fluid through capillary channels 20 at a high velocity provides an additional mechanism for reducing or eliminating gas nuclei at the interface between the inner surface of capillary channels 20 and the gas-supersaturated fluid.
  • high velocity flow may reduce or eliminate gas nuclei at the channel-fluid interface due to a possible Venturi effect at the channel-fluid interface.
  • the high velocity flow and possible associated Venturi effect acts to flush gas nuclei from the inner surface of capillary channels 20 before the gas nuclei can grow large enough to become active and cause trains of bubbles to form.
  • High velocity flow further inhibits bubble formation because there is insufficient time for nucleation and bubble growth in the fluid within capillary channels 20, before the fluid exits the capillary channels.
  • subcritical bubble nuclei i.e. a bubble nuclei of size insufficient for bubble formation, are reabsorbed into the fluid and relatively rapid mixing of the fluid with liquids in the external environment occurs under ambient atmospheric pressure .
  • the velocity of fluid exiting capillary channels 20 is preferably greater than 0.05 m/sec, and more preferably in the range of 0.5 m/sec to 10 m/sec.
  • a parallel array of 55 fused silica capillary channels 20 each having an inner diameter of about 150 ⁇ m and a length of about 10 cm can be used to deliver 800 ml/min of water containing oxygen dissolved at a partial pressure of 20.5 bar, at a hydrostatic pressure of 22.5 bar.
  • the mean flow velocity of the oxygen-supersaturated water through each channel 20 would be approximately 13 m/sec.
  • Apps for preferred embodiments include many different gas-liquid combinations, which may be a mixture of a plurality of gases and/or liquids.
  • system 10 may be used for relatively quick and inexpensive large scale delivery of oxygen- supersaturated water into fluid requiring aeration, such as potable water, municipal water, wastewater, water in bioreactors, fisheries, ponds, lakes, streams, wells, swimming pools, baths and hot tubs.
  • aeration such as potable water, municipal water, wastewater, water in bioreactors, fisheries, ponds, lakes, streams, wells, swimming pools, baths and hot tubs.
  • relatively high oxygen concentrations for example, 10 mg/L or greater
  • the preferred embodiments provide a gas transfer efficiency of nearly 100%; thus, 5 almost all of the dissolved gas delivered is absorbed by the oxygen-deficient body of water.
  • a relatively smaller volume of oxygen-supersaturated water is required to adequately aerate an oxygen-deficient body of water.
  • the fluid source 15 after filtration can be used as the fluid source for preparation of the gas-supersaturated fluid to be recycled back into the large body of fluid.
  • the volume of body of fluid is not increased.
  • Hyperbaric gas concentration levels are achievable in the external body of fluid to be aerated. If the mean velocity of the effluent is relatively low, for example less than 5 m/sec, and the volume of fluid in the external body of fluid is small relative to the effluent volume flow rate per
  • a hyperbaric gas level can be achieved and maintained in the external body of fluid.
  • an oxygen bath is thereby provided where the p0 2 in the external body of fluid is in the range of at least approximately 5-10 bar.
  • Such an oxygen bath may be utilized for neonates and infants with respiratory insufficiency to
  • both the higher permeability of human neonatal skin relative to that of adults and the relatively high ratio of the neonatal body surface area to the neonatal body volume facilitate the transport of oxygen from the oxygen bath across the skin into the general circulation.
  • the high oxygen level in an oxygen bath may also be utilized to enhance healing of superficial wounds, such as burns, and to enhance collagen synthesis of otherwise normal, but relatively oxygen-poor skin.
  • Ozone-supersaturated fluid infusion can be used for disinfection, flocculation, oxidation of dissolved metals, odor control, and oxidation of organic material.
  • system 10 when system 10 is used for the delivery of an effluent supersaturated with a non-toxic gas into, for example, wastewater, microorganisms and other organic matters may grow and accumulate on gas-fluid interface 26 over time, thereby reducing its gas transfer efficiency.
  • system 10 may also be used for the periodic and temporary delivery of ozone-enriched or ozone-supersaturated fluid. The ozone would kill the microorganisms and oxidize the organic materials, which would then be more easily flushed from gas-fluid interface 26.
  • a suitable solvent such as alcohol, acetone, or a strong acid or base may be flushed through gas exchanger 18 to clean gas-fluid interface 26 of microorganisms and organic matter.
  • a suitable solvent such as alcohol, acetone, or a strong acid or base
  • the periodic and temporary delivery of effluent containing ozone and/or a suitable solvent would sterilize and disinfect system 10 of organic elements as well as to flush out any accumulated debris.
  • a high ozone concentration can be achieved at partial pressures of only approximately 3 to 10 bar.
  • a concern with infusing ozone-supersaturated fluid into a site of interest is that the half-life of ozone in ordinary tapwater is generally in the range of 10 to 20 minutes.
  • ozone-supersaturated water from high pressure gas exchanger 18 can be delivered at high velocities via capillary channels 20 within a few seconds, resulting in very little loss of activity of the dissolved ozone. And because the ozone delivered remains dissolved (that is, it does not bubble out of fluid) there is less concern that ozone will enter the atmosphere.
  • the ozone- supersaturated water can be used to treat open bodies of water, such as reservoirs, lakes, ponds, streams, rivers, swimming pools, as well as groundwater, well water, and water within closed chambers.
  • Bioreactors often use carbon monoxide as a carbon source for synthesis of organic compounds by anaerobic bacteria. Because carbon monoxide has a low solubility in water and consumption of the gas by the anaerobic bacteria can be relatively high, it may be difficult to maintain a sufficient carbon monoxide supply in a bioreactor. An infusion of carbon monoxide-supersaturated water generated by system 10 could be used to provide an efficient and controlled means for increasing the level of carbon monoxide in a bioreactor. Other gases, such as nitrogen sources, may be useful for the growth of other types of organisms.
  • a fluid supersaturated with an inert gas such as nitrogen or carbon dioxide
  • an inert gas such as nitrogen or carbon dioxide
  • a fire can be extinguished with greater efficiency than with the use of water alone because of the displacement of oxygen in the air with the inert gas, cooling of the fluid during gas expansion, and the dispersion of the fluid upon gas expansion.
  • Liquids other than water may also be used in system 10 to deliver a high concentration of a gas or a mixture gases to a site of interest.
  • System 10 may be utilized to eject the fluid into a combustion chamber, such as the cylinders of an engine.
  • a combustion chamber such as the cylinders of an engine.
  • the high solubility of oxygen in most fuels, such as gasoline and diesel fuel results in a high oxygen concentration at relatively low partial pressures.
  • the improved oxidation of the fuel could reduce some toxic gaseous byproducts associated with incomplete combustion.
  • Another application of the system of the present invention is snow making by ejecting water supersaturated with air into air having an ambient temperature slightly higher than 0°C.
  • the prior art snowmaking equipment does not achieve as great a maximum distance as the system of the present invention.
  • the air-supersaturated water fluid can remain as an intact stream for sufficiently long periods because of the high flow velocity of the fluid. Due to gas bubbles nucleating from the fluid and normal hydrodynamic forces, such as Rayleigh instability, the fluid fragments in the air and form water droplets, fragments, and/or bubbles. The associated drop in temperature from expansion of the dissolved gas then freezes the water to produce artificial snow.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)

Abstract

L'invention concerne un système et un procédé permettant de délivrer un fluide sursaturé en gaz. Ce système comprend un réservoir (12) de fluide, une pompe à fluide (14), une source de gaz (16), un échangeur (18) de gaz haute pression, et un ou plusieurs réseaux de canaux (20) capillaires. Des commandes appropriées, par exemple un manomètre (22) différentiel ou des soupapes à pression différentielle, permettent de maintenir une pression hydrostatique presque constante du fluide à l'intérieur de l'interface (26) gaz-fluide à membrane semi-perméable dudit échangeur de gaz, cette pression étant environ 1 à 20 % supérieure à la pression partielle gazeuse du fluide situé à l'intérieur de l'échangeur de gaz. Le fluide sursaturé en gaz s'écoule depuis l'échangeur de gaz par l'intermédiaire des canaux capillaires, à une vitesse d'écoulement supérieure à 0,05 m/sec, ce qui facilite la délivrance de débits élevés de fluides sursaturés en gaz, sans effet de cavitation.
PCT/US1998/007671 1997-04-16 1998-04-16 Systeme et procede de delivrance de fluides sursatures en gaz WO1998046340A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
AU74670/98A AU7467098A (en) 1997-04-16 1998-04-16 System and method for delivery of gas-supersaturated fluids
CA002286653A CA2286653A1 (fr) 1997-04-16 1998-04-16 Systeme et procede de delivrance de fluides sursatures en gaz
JP54429098A JP2001520575A (ja) 1997-04-16 1998-04-16 ガス過飽和流体の送出用の系及び装置
EP98922038A EP1009518A1 (fr) 1997-04-16 1998-04-16 Systeme et procede de delivrance de fluides sursatures en gaz

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US84090897A 1997-04-16 1997-04-16
US08/840,908 1997-04-16

Publications (1)

Publication Number Publication Date
WO1998046340A1 true WO1998046340A1 (fr) 1998-10-22

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PCT/US1998/007671 WO1998046340A1 (fr) 1997-04-16 1998-04-16 Systeme et procede de delivrance de fluides sursatures en gaz

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EP (1) EP1009518A1 (fr)
JP (1) JP2001520575A (fr)
AU (1) AU7467098A (fr)
CA (1) CA2286653A1 (fr)
WO (1) WO1998046340A1 (fr)

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WO1999021798A1 (fr) * 1997-10-29 1999-05-06 Fsi International, Inc. Procede et systeme permettant d'accroitre la quantite de gaz dissous dans un liquide et de maintenir cette quantite accrue jusqu'a l'utilisation dudit liquide
US6235641B1 (en) 1998-10-30 2001-05-22 Fsi International Inc. Method and system to control the concentration of dissolved gas in a liquid
US6248087B1 (en) 1997-08-15 2001-06-19 Therox, Inc. Apparatus for generalized extracorporeal support
US6274506B1 (en) 1999-05-14 2001-08-14 Fsi International, Inc. Apparatus and method for dispensing processing fluid toward a substrate surface
US6406551B1 (en) 1999-05-14 2002-06-18 Fsi International, Inc. Method for treating a substrate with heat sensitive agents
US6565807B1 (en) 1999-09-30 2003-05-20 Therox, Inc. Method of blood oxygenation
US6602467B1 (en) 1998-07-24 2003-08-05 Therox, Inc. Apparatus and method for blood oxygenation
US6613280B2 (en) 2001-03-20 2003-09-02 Therox, Inc. Disposable cartridge for producing gas-enriched fluids
US6890482B2 (en) 1999-09-30 2005-05-10 Therox, Inc. Apparatus for blood oxygenation
US8192384B2 (en) 2008-12-04 2012-06-05 Therox, Inc. System for enriching a bodily fluid with a gas having a dual-function power switch mechanism
RU2454271C1 (ru) * 2010-12-27 2012-06-27 Владимир Антонович Шутиков Способ изготовления газовой смеси
US8246564B2 (en) 2008-12-04 2012-08-21 Therox, Inc. System for enriching a bodily fluid with a gas having automated priming capabilities
US8636952B2 (en) 2008-12-04 2014-01-28 Therox, Inc. System for enriching a bodily fluid with a gas having a removable gas-enrichment device with an information recording element

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JP3814719B2 (ja) * 2001-12-18 2006-08-30 株式会社ササクラ オゾン溶解水の製造方法及び製造装置

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US4442843A (en) * 1980-11-17 1984-04-17 Schering, Ag Microbubble precursors and methods for their production and use
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US6607698B1 (en) 1997-08-15 2003-08-19 Therox, Inc. Method for generalized extracorporeal support
US6248087B1 (en) 1997-08-15 2001-06-19 Therox, Inc. Apparatus for generalized extracorporeal support
US6454997B1 (en) 1997-08-15 2002-09-24 Therox, Inc. Apparatus for the preparation and delivery of gas-enriched fluids
US5971368A (en) * 1997-10-29 1999-10-26 Fsi International, Inc. System to increase the quantity of dissolved gas in a liquid and to maintain the increased quantity of dissolved gas in the liquid until utilized
WO1999021798A1 (fr) * 1997-10-29 1999-05-06 Fsi International, Inc. Procede et systeme permettant d'accroitre la quantite de gaz dissous dans un liquide et de maintenir cette quantite accrue jusqu'a l'utilisation dudit liquide
US6488271B1 (en) 1997-10-29 2002-12-03 Fsi International, Inc. Method to increase the quantity of dissolved gas in a liquid and to maintain the increased quantity of dissolved gas in the liquid until utilized
US6648307B2 (en) 1997-10-29 2003-11-18 Fsi International, Inc. Method to increase the quantity of dissolved gas in a liquid and to maintain the increased quantity of dissolved gas in the liquid until utilized
US6936221B1 (en) 1998-07-24 2005-08-30 Therox, Inc. Method of forming gas-enriched fluid
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JP2001520575A (ja) 2001-10-30
AU7467098A (en) 1998-11-11
CA2286653A1 (fr) 1998-10-22

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