WO1999062626A1 - Liquid breathing-gas exchanger - Google Patents
Liquid breathing-gas exchanger Download PDFInfo
- Publication number
- WO1999062626A1 WO1999062626A1 PCT/US1999/012132 US9912132W WO9962626A1 WO 1999062626 A1 WO1999062626 A1 WO 1999062626A1 US 9912132 W US9912132 W US 9912132W WO 9962626 A1 WO9962626 A1 WO 9962626A1
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- Prior art keywords
- liquid
- gas
- fluid
- feed tube
- dispersion
- Prior art date
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Classifications
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
- A61M16/00—Devices for influencing the respiratory system of patients by gas treatment, e.g. mouth-to-mouth respiration; Tracheal tubes
- A61M16/0054—Liquid ventilation
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
- A61M16/00—Devices for influencing the respiratory system of patients by gas treatment, e.g. mouth-to-mouth respiration; Tracheal tubes
- A61M16/10—Preparation of respiratory gases or vapours
- A61M16/14—Preparation of respiratory gases or vapours by mixing different fluids, one of them being in a liquid phase
-
- 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
- B01F23/234—Surface aerating
- B01F23/2342—Surface aerating with stirrers near to the liquid surface, e.g. partially immersed, for spraying the liquid in the gas or for sucking gas into the liquid, e.g. using stirrers rotating around a horizontal axis or using centrifugal force
- B01F23/23421—Surface aerating with stirrers near to the liquid surface, e.g. partially immersed, for spraying the liquid in the gas or for sucking gas into the liquid, e.g. using stirrers rotating around a horizontal axis or using centrifugal force the stirrers rotating about a vertical axis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
- B01F27/93—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with rotary discs
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
- A61M16/00—Devices for influencing the respiratory system of patients by gas treatment, e.g. mouth-to-mouth respiration; Tracheal tubes
- A61M16/22—Carbon dioxide-absorbing devices ; Other means for removing carbon dioxide
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
- A61M2202/00—Special media to be introduced, removed or treated
- A61M2202/04—Liquids
- A61M2202/0468—Liquids non-physiological
- A61M2202/0476—Oxygenated solutions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/05—Stirrers
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/19—Stirrers with two or more mixing elements mounted in sequence on the same axis
- B01F27/191—Stirrers with two or more mixing elements mounted in sequence on the same axis with similar elements
Definitions
- the invention relates to methods and apparatus for counter-current exchange of gases between liquid and gaseous phases. More particularly, the invention relates to an extracorporeal gas exchanger for concentrating dissolved O 2 in a total liquid ventilation medium while reducing the CO 2 metabolic byproduct generated during each respiratory cycle.
- Liquid breathing is a therapeutic methodology currently under development for the treatment of respiratory disorders.
- the therapeutic protocol is based on utilizing liquid media as a mobile phase carrier solvent to facilitate transport and exchange of dissolved oxygen and carbon dioxide when brought into proximal communication with lung alveoli.
- Perfluorocarbon C 8 F 17 Br, LIQUINENTTM
- Perflubron C 8 F 17 Br, LIQUINENTTM
- possesses low surface tension and in combination with favorable wettability and flow characteristics, permits ease of entry into the microstructures of the lung without instigating washout of lung surfactant or introducing other undesirable side effects.
- Perflubron's high CO 2 and O 2 dissolution capacity makes possible the delivery of these respiratory gases in concentrations sufficient to mediate exchange by way of favorable transport gradients with blood levels.
- Perflubron's vapor pressure is positioned optimally such that treatment-end evacuation and clearance of residual liquid occurs naturally (passively) through normal evaporation at physiologic temperatures .
- PFC Partial Liquid Ventilation
- Total Liquid Ventilation is a variant modality in which a predetermined inspiratory (tidal) volume of PFC, properly dosed with dissolved oxygen, is administered endotracheally into the lung. The liquid is then subsequently withdrawn during an expiratory stage, is cleansed of CO 2 , and re-oxygenated via extracorporeal gas exchangers, before being re-administered for the next inspiration cycle.
- Implicit in the TLV protocol is the requirement for a specialized gas exchange device which can efficiently replenish the liquid media on time scales commensurate with the breathing cycle. Since each lung model mandates a different volumetric dosing prescription, based upon functional lung volume, lung compliance, and the type, extent and severity of the pathological condition, the operational integrity of the device should not be compromised by potentially wide ranging liquid delivery rates.
- the gas exchange device is a vital and essential element of TLV therapy, and its operational performance is intimately connected with successful treatment outcome.
- the extracorporeal gas exchange device used in TLV is responsible for concentrating dissolved O 2 in the PFC liquid media, while at the same time eliminating the CO 2 metabolic byproduct generated during each respiratory cycle.
- the gas exchange devices currently used in the art require a finite PFC priming volume and inordinately large O 2 gas flows to effect its current level of performance.
- Such a gas exchange process when scaled-up to handle larger PFC flow rates, would in-turn require correspondingly more priming volume and O 2 consumption, ultimately making treatment cost prohibitive. This would become an obstacle to future investigational use as well.
- a reduction in both priming volume and O 2 gas flow requirements would make treatments more economical.
- the current gas exchange device used in TLV, the spray-bubbler column is a relatively long vertical tube, in which gas and liquid make direct contact.
- PFC liquid is introduced at the top of the column through a nozzle and gas enters the bottom of the column through a porous septum.
- the interfacial area for gas exchange is generated by two mass-transfer subsystems, a nozzle, which creates a liquid dispersion, and a porous septum, which creates an air dispersion.
- the effectiveness of both subsystems are problematic in that their operational performance is strongly dependent on flow rate.
- Both the nozzle and septum perform best at a single characteristic flow rate or narrow range of flow rates.
- Neither subsystem is capable of dynamically responding to varying flow rates and, as such, consistent predictable levels of performance cannot be guaranteed. Accordingly they are not ideally suited to TLV therapy where PFC liquid flow rates can vary from one patient to another.
- nozzle The nature of a nozzle is such that its mass transfer effect is dependent on the fluid dynamics, the shape and other subtle characteristics of the spray. Small variations in either flow rate, orifice diameter or nozzle shape can have dramatic effects on the fluid dynamics of the spray thereby introducing sensitive mass transfer dependencies. Because of this, nozzles are notoriously difficult to characterize.
- the effectiveness of a porous septum may be even more dependent on gas rate.
- the gas flow rate through a septum generally dictates the size and number of bubbles created.
- the narrow operational range of effective gas flow rates permitted through a porous septum is limited on the lower end of the range by the requirement that for good performance the whole septum surface should bubble more or less uniformly, and on the high end of the range by the onset of serious coalescence at the surface of the septum, resulting in poor dispersion.
- the spray bubbler generally requires a finite PFC priming volume and inordinately large O 2 gas flows to effect its current level of performance. Because of the large gas flows required to remove CO 2 , the oxygen flow rate must be relatively high so as to maintain the desired partial pressure of oxygen at the gas inlet. The scrubbing gas requirements being tied to the oxygenation gas requirements force artificially high levels of O 2 to be used. Such a gas exchange process, when scaled-up to handle larger PFC flow rates, requires correspondingly more priming volume and oxygen consumption, ultimately making treatments cost prohibitive.
- Evaporative loss of fluid priming volume during the time-course of treatment is important from both a procedural and an economic point of view. Therefore, it is a further object of the present invention to provide a gas exchanger device that controls and minimizes such losses so as to make treatments more economical and eliminate the need for the clinician to constantly monitor fluid levels and periodically interrupt treatment to make necessary fluid additions. Cleansing gas 'exhaust' from the device is a potential loss point since it most likely contains PFC in the form of vapor. Therefore, it is a further object of the present invention to centralize exhaust gases to allow efficient vapor recovery techniques including condensation of vapor so that condensate can be recovered and returned directly to the system.
- the gas exchange devices and methods described herein are based on the principle of the generation or formation of a finely divided liquid dispersion throughout a gas phase.
- One manner for uniformly dispersing the liquid, such that the process can be predictably scaled and respond to varying liquid flow regimens is to cast the liquid dispersion in the form of a plurality of discrete thin planes, each being finely divided (i.e., into liquid droplets), the number of which can be increased, as required, with substantial functional independence from the effects of adjacent planes.
- Invention devices and methods provide means for gas exchange with very little priming volume requirement, as well as providing for efficient CO 2 removal in a one-pass operation which is scaleable to accommodate a variable patient population, and for which it is possible to dynamically respond with minimally varying operational efficiency to varying flow requirements within a treatment regimen.
- the presently preferred embodiments of the invention described herein comprise a series of vertically aligned rotating disks, upon which shear-thin PFC liquid flows before generating uniform discrete thin planar liquid dispersed layers with high interfacial contact area sufficient to promote efficient mass transfer of dissolved gases.
- Figure 1 is a schematic representation of a preferred embodiment of the present invention.
- Figure 2 is a schematic representation of a preferred embodiment of the diverter of the present invention.
- Figure 3 is a schematic representation of an alternative embodiment of the present invention.
- Figure 4 is a schematic representation of a preferred embodiment of the present invention as part of a closed-circuit ventilation device.
- a device for exposing a liquid to a gas for the purpose of effecting an exchange of gases between the liquid and gas phases comprising: a) a gas containment chamber having one or more ports for said gas to enter and exit said chamber, b) an inlet for said liquid, c) an outlet for said liquid, d) one or more dispersion units for forming discrete thin planar layers of said liquid, located within said gas containment chamber, and in fluid communication with said source of said liquid.
- Liquids contemplated for use in the practice of the present invention will typically be suitable for use in a fluid breathing treatment regimen. Such liquids include perfluorocarbons (PFC) such as Perflubron (sold under the name of LIQUIVENT), and the like.
- the device comprises a fluid feed tube in operative or fluid communication with the liquid inlet and the source of liquid.
- the fluid feed tube is centrally located along the interior of the gas containment chamber.
- the fluid feed tube is rotatable around its longitudinal axis and has at least one dispersion unit attached thereto.
- the dispersion unit may comprise one or more disks mounted on the fluid feed tube.
- dispersion means mounted along a vertical fluid feed tube, wherein the feed tube has one or more outlets (orifices) associated with each dispersion unit; in this manner the dispersion means can be controllably actuated (for example by turning on or off outlets from the fluid feed tube) in response to changing liquid flow rates.
- dispenser units or “fluid dispersion units” means any apparatus that can be employed to form discrete thin planar dispersion layers of liquid.
- the present invention is not limited to the specific use of rotating disks to form the discrete thin planar liquid dispersion layers.
- Other potential devices and methods for droplet formation, as described herein, can be equally as effective and are contemplated for use in the practice of the present invention. Examples of such devices and methods are described herein in greater detail.
- a plurality of disks are employed as the dispersion unit.
- the disks can be made of any suitably rigid and polished material provided that the surface does not substantially interrupt two dimensional flow of a liquid thereon.
- Presently preferred disks are mylar film, for example 8.5 cm diameter floppy disks, which are lightweight (to reduce vibration during high rpm rotation), thin (to reduce edge effects and allow for close stacking of disks), polished (to minimize interruption of two dimensional flow), disposable, and reproducible (because floppy discs are manufactured with consistency).
- mylar film for example 8.5 cm diameter floppy disks, which are lightweight (to reduce vibration during high rpm rotation), thin (to reduce edge effects and allow for close stacking of disks), polished (to minimize interruption of two dimensional flow), disposable, and reproducible (because floppy discs are manufactured with consistency).
- mylar film for example 8.5 cm diameter floppy disks, which are lightweight (to reduce vibration during high rpm rotation), thin (to reduce edge effects and allow for close stacking
- Mylar film from 3.5 inch floppy diskettes was chosen for use because of the exacting specifications and tolerances with which it is produced.
- the finely polished surface provides uniformity so that liquid flow fields are not perturbed by surface irregularities.
- droplets are generated in a thin 2-dimensional plane where cross contamination or interference of adjacent disk's flow fields are minimized.
- Successful predictable scaleup is best achieved with thin two-dimensional (independent) planes of droplets. Due to the thin nature of mylar film, edge effects on droplet formation are minimized and closer stacking arrangements are possible.
- the air stability and apparent rigidity of the disks as they are made to rotate aids in the formation of very thin 2-dimensional liquid dispersed layers. Perhaps the most important factor contributing to small uniform droplet formation is the manner in which the PFC liquid coats or adheres to the mylar surface.
- the light weight mylar material also reduces the load on the motor and less vibration is encountered at high rotational velocities.
- Flow paths may not distribute in such an idealized discrete cutoff fashion but rather are shared in accordance with continuous paths of least resistance (Hydrostatic partitioning).
- Hydrostatic partitioning There is, indeed, a practical upper-limit flow rate which can be achieved through any given pin-hole orifice and, at these maximal flows, the additional hydrostatic contribution (due to gravity effects), to the total pressure is negligible in comparison to the pressures involved at each pin-hole orifice due to high pumping pressure.
- the dispersion units e.g., disks
- the dispersion unit comprises a shaped element such as a small solid half-sphere, or the like, disposed axially about the fluid feed tube and attached thereto.
- the shaped element is partially immersed within the liquid.
- a film forms which climbs up to the equator of the half-sphere before departing in the form of droplets.
- optimal dispersion and droplet formation can be achieved.
- cone shaped and funnel shaped objects may also be semi- immersed and rotated in this manner with great effect.
- Funnel shaped or gravity-well shaped objects permit both sides of the surface to be utilized to first form a thin film and then launch droplets of the liquid.
- an outlet in the fluid feed tube is provided in close proximity to the dispersion means (e.g., near the upper surface of the disk). It may also be preferred for some dispersion units (e.g., a disk) to provide a diverter mounted on the dispersion means or on the fluid feed tube. The diverter in the invention device controls the access of fluid exiting the outlet(s) of the fluid feed tube to the upper surface of the dispersion means.
- the fluid feed tube rotates, thereby passing fluid through the fluid feed tube and out one or more outlets (orifices), resulting in the dispersion of the liquid along the upper surface of the dispersion means, from which the liquid is ejected by means of centrifugal force into the gas surrounding disk, so as to form a two-dimensional liquid dispersion in the gas.
- the liquid ejected in the form of discrete planar layers proceed towards the sidewalls of the gas containment chamber, ultimately colliding therewith.
- feed tube outlet sizes can be employed depending on the particular fluid chosen, the velocity of rotation and the disk material employed.
- the orifice size be about 0.041 inches in diameter.
- the rotational motion of the disk assembly was found to enhance and induce air circulation to a level where effective removal of CO 2 from the fluid was accomplished passively using room air without the need for an active cleansing gas-feed.
- propellers of varying pitch may be placed at several selected vertical positions on the central feed tube.
- the increased air circulation effect is significant in that CO 2 removal from the PFC liquid media is increased. It is evident that maintaining the CO 2 levels within the chamber to very low levels is desirable to take full advantage of the interfacial exposure developed by the liquid dispersion. This observation leads to the conclusion that, once the liquid is sufficiently dispersed in the form of small uniform liquid droplets, the air-space CO 2 concentration becomes the rate limiting step governing the overall performance of the process. As such, further efforts to more finely disperse the liquid or efforts aimed at increasing contact time are expected to be fruitless in such an air-space environment. Because of the importance of this finding, in accordance with additional embodiments of the present invention, there are provided means for improving air circulation.
- One of the objects of the present invention is to not only remove dissolved gases (e.g., CO 2 ) but to exchange them for other gas or gases (e.g., O 2 ).
- substantially pure oxygen gas is supplied by a flat plate bubbler directly to the bulk liquid that has temporarily pooled and collected at the bottom of the contacting chamber before exiting. This method proves adequate and O 2 gas requirements following such treatments were found to be minimal. Indeed, the O 2 gas requirements were found to be reduced from those demanded by current spray-bubbler columns since extra oxygen need not be supplied to compete with the much higher gas turn-over required for CO 2 removal.
- the bulk liquid pool is directed into a separate compartment from that of the upper air space, as shown in Figure 1 (which is specialized for CO 2 removal) thereby resulting in more efficient oxygenation. While only certain embodiments of oxygenation devices and methods are shown and/or described herein, many alternatives may be conceived by those of skill in the art, and are properly contemplated as within the scope of the present invention. Further examples of such techniques and devices are provided below.
- the invention device described herein in all its embodiments, is particularly suited to efficient mass transfer between a liquid and a gas
- methods for promoting efficient mass transfer between a liquid and a gas comprising: creating a plurality of finely divided uniform liquid dispersions containing a first dissolved gas, wherein the uniform liquid dispersions are each in the form of a discrete thin planar layer, and sequentially contacting a continuous gaseous counter-current flow containing a second gas with the plurality of finely divided uniform liquid dispersions.
- the number of discrete thin planar layers is increased proportionally with increase in the flow rate of the incoming gas, thereby rendering the efficiency of mass transfer of the first and second gases into the opposite phase substantially independent of the flow rate of the incoming gas flow.
- the first gas is carbon dioxide and the second gas is oxygen.
- the liquid is a perfluorocarbon and the gas is air.
- each discrete planar layer functions substantially independently from adjacent layers.
- the partial pressure of carbon dioxide in the gas contacting the droplets making up the dispersions in the first of the plurality of thin planar layers contacted is near zero.
- baffles or thin blade affixed to the gas containment chamber wall either vertically positioned, or in other suitable orientations, promotes mixing of the gas phase (e.g., air), within the chamber.
- Static baffles or blades affixed to the inner chamber wall induce whirlpool-like mixing as air moves in the annular space between disks and chamber wall.
- the baffles may be solid continuous, perforated, or sectioned to protrude at selected locations with the chamber.
- the baffles do not necessarily have to be attached to the chamber's inner surface but may alternately be freely suspended or supported by appropriate means.
- the vents are slanted or otherwise oriented to prevent the liquid from exiting the gas containment chamber other than through the intended liquid outlet(s).
- Other distributed gas inlets, one-way valves, or the like may be employed to accomplish the same effect.
- positive pressure sources can be used to force gas into the chamber.
- sub- atmospheric pressure devices, or the like can be used to draw gas out of the chamber.
- air circulation may be further enhanced by placing a cage or grid-like structure fitted internally within the gas containment chamber for strategic placement of air flow ports for either positive or negative pressure flows.
- a cage or grid-like structure fitted internally within the gas containment chamber for strategic placement of air flow ports for either positive or negative pressure flows.
- the gas containment chamber may be fashioned to act like a bellows.
- a bellows, flexible bag, pumping diaphragm, or the like may be synchronized appropriately to collapse and expand with frequency, thereby drawing air into this gas-liquid contacting volume.
- Use of one-way flap valves or other suitable valves permits this bellows action to preferentially draw air into the chamber.
- an oscillating top plate and or accordion-like chamber walls can also be used to provide freedom of movement for the bellows-like chamber to expand and contract, also drawing air into the chamber.
- the up and down motion of a piston or syringe-like plunger, either internal or external to the chamber, combined with one-way valves could be used to rapidly flush the air-space.
- the gas containment chamber can be made of a simple bag-like, balloon-like, or otherwise flexible or elastic bladder with a thin collapsible surface, optionally contained within a rigid support structure. The bag can be kept inflated with a mild positive air pressure.
- the rotation of the dispersion unit assembly can be stopped, and the bag can collapse partially or entirely, to flush air out before being rapidly inflated for the next liquid feed cycle. This action primes the air space before each liquid feed.
- the dispersion unit assembly rotation can be halted between inspiration and expiration cycles when the liquid is not being fed.
- Flexible or elastic materials used as the contacting chamber provide the benefits of being disposable and easily permit variable volume operation. Accordingly, while not in use, the chamber occupies little space.
- the contact chamber can be made to telescope (e.g., a cylinder within a cylinder) so as to expand or contract either to promote air flow or to allow the adjustment of the height of the chamber and hence its volume.
- telescope e.g., a cylinder within a cylinder
- Such a telescoping chamber is easy to size to accommodate the needs of various patients.
- the gas containment chamber can be connected to a mechanical ventilator to precisely regulate air flows into and out of the chamber during a treatment.
- a mechanical ventilator to precisely regulate air flows into and out of the chamber during a treatment.
- Such a scheme can be used to deliver the precise volume and concentration of gas mixtures into the chamber. This scheme may be used alone or in combination with any other embodiments described herein.
- the gas phase environment is maintained with near zero partial pressures of CO 2 .
- the individual fluid droplets e.g., PFC droplets
- favorable gradients for diffusion persist until equilibrium is reached, at which time liquid phase CO 2 concentrations can be made to approach the desired low levels.
- gas phase partial pressures of O 2 are appropriately adjusted, the liquid phase should become oxygenated to near equilibrium partial pressures of O 2 with those in the gas phase.
- each dispersion unit i.e., disk, in the embodiment illustrated in Fig. 1
- the bottom surface remains available for the inclusion of adornments in relief, fins, vanes, or other such protrusions of various angles, pitches, and placements.
- the rotational motion of dispersion units equipped with such adornments will induce air flow and reduce points of stagnation between dispersion units.
- the fins could be attached to the periphery of all or some of the dispersion units in the assembly. Either etched or pitted surfaces could also be used to drag air along with rotational motion.
- the adornments to the underside or periphery of the dispersion units should not be made in such a way so as to cause the dispersion units to flutter as they rotate as fluttering might cause the liquid to be dispersed in a chaotic fashion and/or not be restricted into planes or zones that are isolated from interference with droplets for adjacent planes or zones.
- objects that augment gas flow with properties similar to, but not limited to, propellers, impellers, paddle agitators, fans, turbines, or blades of various pitch are placed in one or more positions below, above, or interspersed at selected vertical positions within the dispersion unit assembly and affixed to the rotating shaft of the feed tube to increase air circulation (see, e.g., Fig. 3, where an exhaust fan 124 is attached to the feed tube).
- These objects may be rigid or flexible to accommodate the airflow generated by specific embodiments of the dispersion unit.
- the rotation of such objects may be engaged by attachment to the feed tube shaft or rotation may be caused independently by attachment to externally supplied forces (e.g., motors, hydraulic impellers, and the like).
- Placement of such objects for movement of gases within a concentric draft tube may be employed to create an artificial chamber for top to bottom mixing of gas flow within the gas containment chamber.
- Fan blades, or the like can also be placed below the top plate of the gas containment chamber or gas containment outside the chamber above the top plate to augment gas flow.
- the advantages of counter-current flow in mass transfer are well recognized. While true counter-current flow is generally difficult to achieve in liquid-in-gas dispersions, the unique geometric uniformity of the dispersion of the liquid phase in devices and methods according to the present invention provide opportunities to achieve such counter-current flow wherein the gas is encouraged to move in directions opposite to that of the liquid droplets which comprise the thin planar units of dispersed liquid. Accordingly, in one embodiment of the present invention, the central axis of rotation acts as a sink for the gas phase. In this embodiment, at each level where a dispersion unit resides a gas port or orifice is positioned to draw gas out of the chamber, thereby inducing air to flow horizontally across each dispersion unit in the dispersion unit assembly.
- the fluid feed tube can have a region, inter-lumenal, multi-lumenal, or otherwise, devoted to gas flow.
- two or more tubes, which orbit around the same axis, one which delivers liquid and one which draws air out, can also be utilized for this purpose.
- the disks serve to compartmentalize each discrete, thin planar layer, of liquid dispersion. As long as the droplet flight path is not interfered with, the thin cross-sectional air-spaces created by the disk assembly within the chamber provide for improved air flow management by eliminating vertical cross flows. True counter-current flow can be achieved with the appropriate negative pressure sink at the axis of rotation.
- fluid distribution from the feed tube to any particular disk is achieved by way of specially constructed flow diverters (i.e., inter-disks) positioned above each dispersion unit in the dispersion unit assembly.
- flow diverters i.e., inter-disks
- Other methods or materials can be used to achieve a similar effect.
- fibrous, foam-like, swab-like, spongelike, or other similar materials can be used to dissipate the velocity of the liquid jets emanating from the central feed tube, thereby functioning to gradually leak fluid onto each associated dispersion unit in a controlled fashion and at the appropriate initial contact position.
- Wire mesh, screen-like, cloth-like, or other similar material can also be used to accomplish this purpose.
- a small circular semi-flexible flap for example made of mylar, can be positioned near the center shaft to dissipate the velocities of jets entering the chamber, either due to its compliance or by surface tension sealing/leaking.
- fluid feed among disks or dispersion units is accomplished by way of a central rotating feed tube.
- the PFC liquid can be introduced into the feed tube from either the top or bottom of the vertical tube.
- Fluid can also be fed through tubes aligned parallel and along sides of a center shaft.
- the center rotating shaft would not need to be hollow.
- fluid can be fed through a manifold, so that each dispersion unit has a dedicated tube aligned perpendicular to the center shaft which extends into the dispersion unit assembly for the purpose of depositing liquid onto the initial contact position.
- Other means for introducing fluid feed include using a rotating screw (e.g., an Archimedian screw, or the like) to move liquid through the center tube and onto each dispersion unit.
- An Archimedian screw may also be inserted into the hollow feed tube to draw fluid from the bottom of the chamber upward to a point wherein the fluid is then brought into contact with each unit in the vertical dispersion unit assembly.
- the same screw is used to recycle fluid which collects at the bottom of the chamber for a second pass, permitting an internal recycle mode as required for effective gas transfer into and/or out of the fluid.
- fluid no longer needs to be fed through the central hollow tube, but rather can be introduced into a preferably cylindrical walled-off region near the bottom chamber. This isolated region near the bottom of the feed tube is the entry point for the fluid, which is drawn upward by Archimedian action. Fluid that has been dispersed and cleansed would then be collected outside the walled-off region for subsequent oxygenation, as required.
- holes or perforations in the disk surface may be utilized to allow fluid to drain down onto successive disks.
- hydrostatic forces are used to distribute fluid in a partitioning scheme based on flow rate and vertical height. Since each dispersion unit has a given vertical height, the hydrostatic variation between dispersion unit is fixed by virtue of this height.
- To alter the hydrostatic partition effect without changing dispersion unit spacing can be accomplished by tilting the contact chamber, for example, to reduce the effective vertical direction. Since the spinning dispersion units operate in any near-vertical orientation, the axis of rotation can be tilted without substantial impairment of the dispersion process. A degree of freedom can be built into the device to allow for such orientational flexibility.
- dispenser units or “fluid dispersion units” means any apparatus that can be employed to form discrete thin planar dispersion layers of liquid.
- the present invention is not limited to the specific use of rotating disks to form the discrete thin planar liquid dispersion layers.
- Other potential devices and methods for droplet formation, as described herein, can be equally as effective and are contemplated for use in the practice of the present invention. Examples of such devices and methods follow. Centrifugal Shear-Thinning Type
- shapes other than disk made of various materials, rigid or otherwise, such as cones, funnels, perforated plates, etched or dimpled surfaces, and the like, can be used to shear-thin fluid streams and produce droplets, provided that the fluid sufficiently adheres to the surface of such material and that the transition to droplets occurs in non-chaotic fashion.
- Various stacking arrangements of these alternative embodiments are also possible.
- rotation of shapes, other than disks, that are semi-immersed in fluid can effectively promote formation of droplets.
- a film of fluid forms thereon and climbs up to the equator of the half-sphere before departing in the form of droplets.
- optimal dispersion and droplet formation can be achieved.
- Cone shaped and funnel shaped objects have also been employed in this manner with great effect. Funnel shaped or gravity-well shaped objects may also be employed in the practice of the present invention, thereby permitting stacking.
- both sides of the surface can be utilized to first form a film and then launch droplets in accordance with the present invention.
- a scaleable discrete thin planar liquid dispersion is created using a high pressure jet impinging on a rotating sphere, toothed gear, pin-wheel, or like arrangement.
- a rotating hollow tube without disks can be employed for casting of droplets into a thin planar layer.
- Rotating spiral armed sprayers using orificial breakup of liquid or oscillating impingement type rotating sprayers, and the like, can also be used.
- Ultrasonic Means Ultrasound may also be used in the practice of the present invention to produce one or more discrete thin planar layers of droplets. This, as with the other embodiments described herein, serves to illustrate that it is the formation of discrete thin planar dispersions of liquid droplets that is most important to the practice of the present invention, not the manner in which this is accomplished.
- Ink- Jet technology may also be used in the practice of the present invention to produce one or more discrete thin planar layers of droplets.
- Such technology is well capable of forming precisely controlled dispersions, and can be applied to form a discrete thin planar layer of droplets, or other suitable structural entity, shape or form that can be propagated with complete linear independence in three dimensions such that combinations of entities introduce no side effect or collaborative behavior other than permitting larger flow rates to be processed.
- Scrubbing gas is often desirable to provide and maintain a favorable air-space environment for CO 2 interphase transport.
- ambient room air compressed air, or bottled oxygen
- the high speed rotation of the dispersion apparatus assembly was found to induce air circulation patterns, thus creating a favorable air-space environment for CO 2 removal.
- the use of room air has the advantage of obviating the need for an active gas feed.
- Scrubbing gas can be recycled and passed in a closed loop through processes which remove or absorb CO 2 . Such a closed-loop embodiment enables evaporative loss to be controlled.
- helium can be used as a recyclable scrubbing gas, and has additional advantages where PFC vapor must be recovered from the gas exhaust.
- the wide disparity in density between helium gas and PFC vapor allows for effective separation techniques, as are known by those of skill in the art. If CO 2 is removed from such a helium exhaust, the helium gas can be recycled for reuse in the chamber in closed-loop fashion. Additionally, if the scrubbing gas is presaturated with PFC vapor, further net transport of PFC to the gas phase is thereby prevented.
- the scrubbing gas is pre- chilled.
- the temperature of the liquid droplets is reduced upon contact with the gas, thereby shifting the vapor pressure equilibrium conditions so as to minimize evaporation.
- oxygen-rich air mixture as the scrubbing gas permits oxygenation and CO 2 removal to be accomplished simultaneously by way of the same process.
- gases that have therapeutic benefits for example gas streams containing therapeutic active agents such as antibiotics, anti-asthmatics, and the like, may also be used in the practice of the present invention.
- a DC motor 102 is used to drive the disk assembly 104.
- Such electric motors coupled to gears 106 or pulleys attached to central shaft 108 either internal or external to the chamber can be used, provided that variable speed rotation of the assembly is achieved.
- any power source can be used that is capable of imparting the high velocity rotation that is preferred for the practice of the present invention.
- pneumatic methods of driving the disk assembly may be employed. Indeed, the scrubbing gas feed itself or other air pressure sources can be harnessed to induce rotation of the dispersion unit assembly.
- one or more appropriately angled gas jets emanating from an armature attached to the central feed tube can be used to force rotational motion of the dispersion unit assembly while simultaneously adding scrubbing gas to the chamber.
- the whole assembly is optionally disposable since a motor is not required.
- the gas exchange with the liquid is best accomplished by generating discrete thin planar dispersions of the liquid in a droplet form. Accordingly, droplet collection is an important consideration to the practice of the present invention. Droplets travel at high velocity through the gas containment chamber air-space and then collide with the chamber wall where they coalesce into bulk fluid. Very small droplets which are formed at the higher speed rotations of dispersion units collide and rebound due to their apparent rigidity (and inability to coalesce instantaneously upon impact). Since the errant scattering of droplets should be avoided, methods are needed to reduce this rebound effect.
- shock-absorbing materials are used to line the interior of the chamber to reduce or cushion the effects of droplet impact and reduce elastic collision effects.
- the wettability characteristics and the fine structure of the shock-absorbing material are important to the time- scale in which droplets coalesce. Materials with protrusions and fibrous, foam, matted, or like materials are effective shock-absorbing materials and will gradually dissipate droplet momentum to the point where droplets do not rebound.
- the side walls of the chamber can be angled to direct or focus the rebounding droplets into specific more controlled flight patterns (preferably downward).
- loss of liquid e.g., PFC
- loss of liquid e.g., PFC
- the following embodiments of the present invention provide both preventative and curative methods to reduce vapor loss during gas exchange.
- vapor loss is reduced by lowering the temperature of the PFC liquid, thereby lowering the vapor pressure of the PFC liquid and the evaporative propensity of the liquid.
- One means for accomplishing this goal is to chill the scrubbing gas because the PFC, once dispersed in the form of droplets, has an enormous surface area exposure thereby allowing for efficient heat transfer.
- the PFC may be cooled prior to entering the chamber as well, although the liquid will quickly equilibrate to the temperature of the surrounding chamber air. Alternatively, or in addition, increasing the air pressure in the chamber will disfavor evaporation of the PFC liquid.
- trace amounts of one or more surface active agents are added to the PFC to increase rigidity and/or coat or seal the surface of droplets to prevent PFC molecules from escaping to the gas phase.
- surface active agents e.g., surfactants
- the CO 2 interphase transport is not greatly impeded due to the small size of the solute molecules.
- the surface active agent is removed upon exiting the chamber unless the presence of the surface active agent in no way compromises the patient.
- dust particles, finely divided solids, or other insoluble particulate material may be used to increase the rigidity of droplet surfaces. These parti culates and like materials are more readily removed from the PFC before it is recycled to the patient.
- Variable rotation rate of the dispersion unit assembly may also be employed to control droplet size so as to reduce evaporative loss while still permitting effective CO 2 removal.
- halting rotation of the dispersion unit assembly when liquid is not being fed will reduce the exposure of the PFC liquid to air circulation and thereby reduce its evaporation.
- a condenser placed either within or outside of the gas containment chamber is used to recover vapor from the gas phase.
- the present invention lends itself to the internal inclusion of a condenser.
- a perforated plate type condenser unit positioned internally near the top of the gas containment chamber is provided.
- an upper gas exhaust port near the top of the gas containment chamber.
- Finely meshed wire-screen or like moisture trapping material can be employed as the plate material provided that interference with exit gas flows is not compromised. Condensed PFC would then fall back into the scrubber without effecting its operation. Additionally a low speed fan could be used to remedy any stagnation of air flows in the Z-direction.
- This embodiment may also employ a two compartment design as described herein (i.e., a gas containment chamber and a fluid containment chamber).
- a gas containment chamber i.e., a gas containment chamber and a fluid containment chamber.
- Oxygenation can be achieved by any of the methods described herein.
- helium or other light gas is used as the scrubbing gas
- a separation technique based on gravity or centrifugal force can be used in the practice of the present invention to recover the heavier PFC vapor from the lighter gas phase.
- the outer wall of the chamber in the invention device is heated or cooled by appropriate means including, but not limited to, electrically resistive heat tape, nichrome wire, hot/cold water jacket circulator, or the like.
- the gas containment chamber wall is made of materials with reasonable thermal conductivity characteristics, thereby allowing the gas containment chamber itself to function as a heat exchanger.
- PFC dispersed in the form of droplets has an enormous surface area exposure for heat transfer, the most efficient heat transfer opportunity for altering the temperature of the fluid is during the time that the fluid is dispersed as small droplets.
- the scrubbing gas is heated or chilled, for example, just prior to entering the gas containment chamber.
- the surface area is very large in relation to the volume of the fluid that has to be brought into thermal equilibrium with the surrounding air. Therefore, thermal equilibrium is approached very rapidly, with the droplets almost instantaneously reaching substantially the same temperature as the sunounding gas when the heated or cooled air is brought into contact with the droplets.
- the chamber wall is made of or coated with (inside or outside) material having a high thermal conductivity
- heat exchange can be achieved when the liquid (e.g., PFC) collects on the surface of the chamber wall after droplet collision and coalescence.
- an annular water jacket or similar device can be built around some portion of the outer wall of the gas containment chamber.
- the top and/or bottom plates of the gas containment chamber can also be made of such material.
- the thermally conductive material can also protrude into the chamber (e.g., like a cold-finger or cooling fin).
- rotating disks or alternative dispersion units can themselves be made of conductive material and/or have the temperature thereof altered by electrical resistance heating, or the like, thereby providing, for example, thin film heat exchange.
- the interior-space of the chamber can also be heated by way of radiant sources, such as heat lamps, or the like.
- radiant sources such as heat lamps, or the like.
- any suitable means for oxygenating the scrubbed liquid may be employed in the practice of the present invention.
- pure oxygen gas is supplied directly to the bulk liquid by a flat plate bubbler as the liquid is temporarily pooled and collected at the bottom of the gas containment chamber.
- the requirements for O 2 gas were found to be minimal.
- Alternative methods for achieving oxygenation of the liquid phase are also contemplated for use in the practice of the present invention.
- those of skill in the art can achieve oxygenation and CO 2 removal in one step in a single compartment by feeding a desired flow of an oxygen/air mixture into the chamber.
- the gas exchange efficiency of such embodiments is not optimal, however, because the flow of the oxygen air mixture must be maintained at such a high rate for CO 2 removal that excess oxygen would have to be added just to compete and maintain the desired partial pressures of O 2 in the scrubbing gas phase.
- a wetted- wall bubble oxygenator can be created.
- the bulk liquid pool is confined in a lower liquid containment compartment or chamber 126, maintained in fluid separation from the gas exchange space within the gas containment chamber.
- a valve or other like apparatus such as a perforated plate 128 can provide for fluid communication between the gas containment chamber and the liquid containment chamber, while preserving fluid separation between the two chambers.
- the upper gas exchange space is then dedicated to CO 2 removal.
- scrubbing gas requirements are distinct from the oxygenation requirements. Hence, it is no longer necessary to continuously increase O 2 flows in the scrubbing gas to keep the partial pressure of O 2 high enough to oxygenate the liquid phase. Instead, O 2 -containing gas can be supplied to the lower chamber by way of a separate oxygen inlet 130. In this two- compartment chamber, oxygenation can be independently achieved by several methods.
- a specially constructed oxygenator in which a sheet of porous material (made of high density polyethylene, or the like) is integrated into the bottom plate of the chamber.
- the porous sheet is made to cover nearly the entire cross sectional area of the chamber.
- Oxygen gas is fed in pressure distributed fashion by way of a recessed air-space in contact with the entire under-surface of the sheet. Bubble formation is substantially evenly distributed over the porous surface with good air dispersion and minimal coalescence at low flow rates. Since the liquid pool is relatively shallow and air flow is distributed over such a wide area, gas velocity is reduced and good air dispersion is achieved. If the fluid exit port is centrally aligned within the porous surface the natural whirlpool action creates slightly more residence time and mixing of the liquid on the porous surface, thereby providing more efficient oxygenation.
- rotating gears, or the like are used to create a draw-down rotational impeller. Air is drawn down from the upper air-space of the gas containment chamber into the liquid pooled at the bottom of the chamber where it is dispersed.
- the rotation of the gears is coupled to the rotation of the dispersion unit assembly.
- an oxygenating dispersion unit 132 such as a disk apparatus, shaped elements, ultrasonication, ink-jet technology, or the like, can be employed as described herein.
- a separate liquid containment compartment or "oxygenation compartment" where liquid is directed after exiting the gas containment chamber through its exit port.
- the same rotational feed tube could be employed to drive the dispersion units in the liquid containment compartment.
- a plug or the like is preferably placed in the feed tube to prevent mixing of the liquids in the separate compartments.
- the manner in which the disk assembly is configured acts to buffer the performance of the gas-exchange process against the variations in PFC fluid flows required to treat variously sized patients.
- the efficiency of gas-exchange is not adversely effected by varying PFC fluid flows.
- the rotating disk embodiment additionally makes scaling of the device to accommodate larger animal subjects easier to achieve.
- the present invention has as its underlying foundational basis the generation or formation of a finely divided PFC liquid dispersion throughout a continuous gas phase, vacuum, or rarefied gaseous region, enclosed within a bounded contacting volume of suitable size.
- the manner envisioned for uniformly dispersing the liquid such that the process can be predictably scaled and respond to varying liquid flow requirements with equal efficiency, in compliance with the aforementioned necessities of TLV gas exchange, is to cast the liquid dispersion in the form of a discrete thin plane.
- the present invention may be practiced using other suitable structural entities, shapes, or forms which can be propagated with complete linear independence in three dimensions such that combinations of entities introduce minimal side effects or collaborative behavior other than permitting a larger liquid flow rate to be processed.
- the uniqueness of this invention is further augmented by, but not limited to, a novel performance buffering construct in which the promotion of a variably changing number of discrete thin planar liquid dispersion layers occurs in dynamic fashion as flow rates are increased or decreased. Accordingly, in use, the invention device dynamically senses gas exchange demand, by virtue of fluid flow rate, and automatically makes the conesponding compensating adjustment to activate or invoke an appropriate number of the discrete thin planar liquid dispersion units, to ensure that the overall process exhibits a consistently buffered and invariant performance profile.
- FIG. 1 a presently preferred embodiment is exemplified in the following discussion and is represented schematically in Figures 1 - 3.
- This embodiment comprises a vertically oriented cylinder 100 made of transparent rigid plastic ( ⁇ 16 cm inner diameter by -29 cm height).
- Flat plates, of similar material, affixed to both the top 101(a) and bottom 101(b) of the cylinder serve to enclose this gas-liquid contacting volume (gas containment chamber).
- gas containment chamber Housed within this chamber is an assembly comprising a series of thin mylar film disks 104 ( ⁇ 40 ⁇ thick and ⁇ 3.5 inch diameter) uniformly stacked on a centrally aligned fluid feed tube 108 ( ⁇ 0.25 inch OD) about which high speed rotation is made to occur.
- spacer-diverters 110 Between each disk are positioned specially constructed spacer-diverters 110 ( ⁇ 1 cm high) which are designed to deposit fluid onto the upper surface of each disk and ensure uniform initial contacting as the fluid feed makes its way through two pin-hole size orifices 112 located on the fluid feed tube vertically coincident with each disk.
- High speed rotation of the disk assembly is achieved by a gear assembly 106 external to the chamber which is attached to, and concentric with, the feed tube. This gear in turn is engaged by a small variable speed DC motor 102 (e.g., 6-24 V) with matching gears.
- the presently preferred embodiment exemplified in Figure 1 also shows a gas inlet tube 118 where cleansing gas is fed into the chamber at various flow rates.
- This feed tube being adjustable, allowed the air flows to be directed at specific vertical and axial positions within the chamber.
- Other gas feed embodiments that may be used include multiple feed tubes, each with evenly spaced jets made to vertically coincide with the liquid dispersed layers, and the like.
- the depicted embodiment shows a liquid outlet 120 where the scrubbed liquid can exit the chamber (typically, the liquid will enter the chamber through an inlet connecting the liquid source with the fluid feed tube).
- initial fluid contact at each disk is accomplished with a specially designed spacer/diverter.
- the essential features of the diverter are shown schematically in Figure 2, where fluid feed direction is indicated with bold arrows.
- Two pin-hole size orifices 112 (preferably about 0.041 inches diameter), cut into opposite sides of the feed tube 108 and located vertically coincident with the recessed annular region of the diverter 110 provide a contiguous path for the inlet fluid stream to reach the upper surface of the disk 122.
- the annular recessed region provides space for orificial jet velocities to dissipate by impinging on the inner wall of the diverter.
- PFC is then directed downward where it first makes contact with rotating disk through a slightly elevated open skirt at the bottom of the diverter.
- the radial component of the liquid's velocity is effectively reduced, thereby achieving the desired velocity-dissipated, centrally-aligned initial condition upon contact of the fluid with the disk.
- the continuous bulk liquid is deposited onto the disk at its initial contact position, it is then exposed to the centrifugal acceleration induced from high speed rotation, creating a shear- thinned film of fluid.
- the thin liquid film adheres to the disk material (which is preferably mylar) through the surface molecular forces which exist between the mylar and liquid, and those between the liquid molecules themselves. The strength of these frictional forces allows the liquid film to attain a substantial radial velocity as it is accelerated from its initial rest condition to the periphery of the disk.
- a 2- dimensional liquid dispersion of small, uniformly sized, droplets is then produced as the fluid first separates into thin transient filaments which persist momentarily and ride along the periphery of each disk before breaking into droplets. Due to the high radial velocities attained at the periphery, the droplets are ejected tangentially upon departure and travel with high velocity through the air-space of the chamber with minimal gravitational deflection.
- the thin liquid film first formed on the surface of a rotating disk likely contributes to gas exchange. Although probably not the predominant mechanism, such gas exchange is contemplated as within the scope of the present invention.
- Such a liquid film is readily scaleable and may have applicability to TLV (without the necessity of combining it with other embodiments of the present invention).
- the liquid in air dispersion generated by the rotating disk assembly provides sufficient gas-liquid interfacial surface area to ensure efficient removal of dissolved CO 2 from PFC fluids.
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP99927131A EP1083982A1 (en) | 1998-06-01 | 1999-06-01 | Liquid breathing-gas exchanger |
AU44110/99A AU4411099A (en) | 1998-06-01 | 1999-06-01 | Liquid breathing-gas exchanger |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US8753098P | 1998-06-01 | 1998-06-01 | |
US60/087,530 | 1998-06-01 |
Publications (2)
Publication Number | Publication Date |
---|---|
WO1999062626A1 true WO1999062626A1 (en) | 1999-12-09 |
WO1999062626A9 WO1999062626A9 (en) | 2000-03-16 |
Family
ID=22205730
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US1999/012132 WO1999062626A1 (en) | 1998-06-01 | 1999-06-01 | Liquid breathing-gas exchanger |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP1083982A1 (en) |
AU (1) | AU4411099A (en) |
WO (1) | WO1999062626A1 (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1424090A1 (en) * | 2002-11-29 | 2004-06-02 | Université de Sherbrooke | Method and apparatus for conducting total liquid ventilation with control of residual volume and ventilation cycle profile |
RU2768952C1 (en) * | 2021-01-14 | 2022-03-25 | Общество с ограниченной ответственностью "Старт-Катализатор" | Heat exchanger |
CN114768511A (en) * | 2022-04-30 | 2022-07-22 | 福建德尔科技股份有限公司 | A tail gas absorbing device for production of electron-level trifluoromethane |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE545606C (en) * | 1929-07-26 | 1932-03-03 | Chem Fab Dr Hugo Stoltzenberg | Device for carrying out reactions between liquids and gases |
US4007920A (en) * | 1973-08-29 | 1977-02-15 | Mark Plunguian | Mixing and aerating device |
GB2113562A (en) * | 1981-11-24 | 1983-08-10 | Ici Plc | Treatment process |
US5226727A (en) * | 1991-09-30 | 1993-07-13 | Reichner Thomas W | Agitator/mixer |
WO1997019719A1 (en) * | 1995-12-01 | 1997-06-05 | Alliance Pharmaceutical Corp. | Methods and apparatus for closed-circuit ventilation therapy |
-
1999
- 1999-06-01 AU AU44110/99A patent/AU4411099A/en not_active Abandoned
- 1999-06-01 EP EP99927131A patent/EP1083982A1/en not_active Withdrawn
- 1999-06-01 WO PCT/US1999/012132 patent/WO1999062626A1/en not_active Application Discontinuation
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE545606C (en) * | 1929-07-26 | 1932-03-03 | Chem Fab Dr Hugo Stoltzenberg | Device for carrying out reactions between liquids and gases |
US4007920A (en) * | 1973-08-29 | 1977-02-15 | Mark Plunguian | Mixing and aerating device |
GB2113562A (en) * | 1981-11-24 | 1983-08-10 | Ici Plc | Treatment process |
US5226727A (en) * | 1991-09-30 | 1993-07-13 | Reichner Thomas W | Agitator/mixer |
WO1997019719A1 (en) * | 1995-12-01 | 1997-06-05 | Alliance Pharmaceutical Corp. | Methods and apparatus for closed-circuit ventilation therapy |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1424090A1 (en) * | 2002-11-29 | 2004-06-02 | Université de Sherbrooke | Method and apparatus for conducting total liquid ventilation with control of residual volume and ventilation cycle profile |
US7726311B2 (en) | 2002-11-29 | 2010-06-01 | Universite De Sherbrooke | Method and apparatus for conducting total liquid ventilation with control of residual volume and ventilation cycle profile |
RU2768952C1 (en) * | 2021-01-14 | 2022-03-25 | Общество с ограниченной ответственностью "Старт-Катализатор" | Heat exchanger |
CN114768511A (en) * | 2022-04-30 | 2022-07-22 | 福建德尔科技股份有限公司 | A tail gas absorbing device for production of electron-level trifluoromethane |
CN114768511B (en) * | 2022-04-30 | 2023-04-21 | 福建德尔科技股份有限公司 | Tail gas absorbing device for electronic grade trifluoromethane production |
Also Published As
Publication number | Publication date |
---|---|
EP1083982A1 (en) | 2001-03-21 |
AU4411099A (en) | 1999-12-20 |
WO1999062626A9 (en) | 2000-03-16 |
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