WO2019132855A1 - Dispositif de refroidissement à air ionique - Google Patents

Dispositif de refroidissement à air ionique Download PDF

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Publication number
WO2019132855A1
WO2019132855A1 PCT/US2017/068386 US2017068386W WO2019132855A1 WO 2019132855 A1 WO2019132855 A1 WO 2019132855A1 US 2017068386 W US2017068386 W US 2017068386W WO 2019132855 A1 WO2019132855 A1 WO 2019132855A1
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WO
WIPO (PCT)
Prior art keywords
heat
solution
tank
hot
ionic
Prior art date
Application number
PCT/US2017/068386
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English (en)
Inventor
David John Tanner
Original Assignee
David John Tanner
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.)
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Publication date
Application filed by David John Tanner filed Critical David John Tanner
Priority to PCT/US2017/068386 priority Critical patent/WO2019132855A1/fr
Publication of WO2019132855A1 publication Critical patent/WO2019132855A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B29/00—Combined heating and refrigeration systems, e.g. operating alternately or simultaneously
    • F25B29/003—Combined heating and refrigeration systems, e.g. operating alternately or simultaneously of the compression type system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B41/00—Fluid-circulation arrangements
    • F25B41/10—Fluid-circulation arrangements using electro-osmosis
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B5/00—Compression machines, plants or systems, with several evaporator circuits, e.g. for varying refrigerating capacity
    • F25B5/02—Compression machines, plants or systems, with several evaporator circuits, e.g. for varying refrigerating capacity arranged in parallel

Definitions

  • the present invention in some embodiments thereof, relates to air cooling systems and devices.
  • electrical energy may be generated from the“free” energy produced by the mixing of two ionic solutions by a reversed -electro-dialysis or pressure retarded osmosis (PRO) processes.
  • This process utilizes two ionic solutions of differing concentrations and temperature ranges, passing the solutions through a Reversed-Electro-Dialysis membrane stack, the dilute and concentrated solutions entering on either side of the membrane layer, causing solute to pass from the concentrated side to the dilute side, creating the generation of an electrical output across the electrodes located at either end of the membrane stack.
  • the resulting electrical output is a function, generally speaking, of the difference in the concentrations of the inputted solutions, the type of salts utilized and the corresponding enthalpy of solution of a particular salt, and the characteristics of the membrane and electrodes utilized including the number of membrane cell units.
  • RED reserved-electrodialysis
  • pressure retarded osmosis factories constructed require a continual replenishment of ionic solutions used to conduct their salinity-gradient processes, causing the need to discharge of spent brine into the environment.
  • the solution sources in most RED systems utilize natural fresh water sources (such as rivers) and natural saltwater sources (such as the ocean, or a salt water lake) these sources of solution contain impurities that damage and reduce the efficiency of the RED system's membrane stacks or in the case of pressure retarded osmosis, these impurities cause fouling of the membranes. This situation limits the overall efficiencies of such an open-ended, reversed-dialysis system.
  • An object of the present invention is to provide a method and apparatus using highly efficient means to generate air cooling.
  • Another object of the invention is to improve and extend the utility of the reversed-electro-dialysis processes, in addition to the pressure retarded osmosis process, according to the method and apparatus disclosed herein creating a highly efficient electrical output that has a very low carbon footprint— e.g. it is not reliant on consumption of fossil fuels, thus avoiding the production of greenhouse gas emissions.
  • the invention disclosed herein causes net air cooling, its utility in the reduction of greenhouse gases could be especially useful.
  • a further object of this invention is to associate the disclosed method and apparatus with an industrial low grade heat source, such as the gasification of municipal solid waste, solar, or a gas stream input from for example a petroleum cracking facility, allowing the electrical voltage potential created by this contained ionic gradient system to be applied to the cooling of the ambient air within the system or factory, thus producing a discharge of the amount of cool air created by a system producing 1 megawatt/minute of electrical power output for 52 a gallon system.
  • an industrial low grade heat source such as the gasification of municipal solid waste, solar, or a gas stream input from for example a petroleum cracking facility
  • a final object of the invention is to devise a system improving the ionic fluid dynamics within the contained system, so as to speed-up or increase the rate of ionic flow through a given system, without changing the amount of fluids contained within the system.
  • a method of generating air cooling comprising: Releasing an intermediate ionic solution from at least one buffering tank into two equal volume yet separate processing tanks associated with a heat pump, generating a hot-side concentrated ionic solution at a temperature range no less than 140 degrees F.
  • a processing tank designated the dissolving tank associated with at least one of heat exchangers, automatic-flow-valves, heat pumps, and passing this concentrated solution through a reversed-electro-dialysis unit or pressure retarded osmosis unit; generating a cold-side, diluted ionic solution from the processing tank designated the precipitating tank utilizing a reversible vapor-compression pump with a coefficient of performance of at least 3 or above generated at a temperature no less than 33 degrees F., in a processing tank associated with at least one of heat exchangers, automatic-flow-valves, and reversible-vapor-compression pumps, and passing this diluted solution through a reversed-dialysis unit or pressure retarded osmosis system; reconstituting said concentrated and diluted ionic solutions into an intermediate solution before exiting from the reversed-dialysis unit or pressure retarded osmosis system; and recycling the intermediate ionic solution by performing the previous three steps in a contained system.
  • an ionic air cooling device comprising: releasing an intermediate ionic solution from at least one buffering tank associated with a pump, generating a hot-side concentrated ionic solution at a temperature range no less than 140 degrees F.
  • a processing tank associated with at least one of heat exchangers, automatic-flow-valves, heat pumps, and passing this concentrated solution through a reversed dialysis unit; releasing an intermediate ionic solution from at least one buffering tank associated with a pump, into two processing tanks, one of which generating a cold-side (precipitating tank), diluted ionic solution and a hot-side concentrated ionic solution utilizing a reversible-vapor compression pump with a coefficient of performance of at least 3 or above generated at a temperature no less than 33 degrees F., in a processing tank associated with at least one of heat exchangers, automatic-flow-valves, and reversible-vapor-compression pumps, and passing this diluted solution through a reversed-dialysis unit; reconstituting said concentrated and diluted ionic solutions into an intermediate solution before exiting from the reversed-dialysis unit; and recycling the ionic solution by performing steps earlier three steps in a contained system.
  • Said method and apparatus describes a highly efficient electrical current source created by a contained, or closed salient gradient fluid system connected to ambient air sources by means of heat exchangers and heat pumps capable through the above described steps of generating 1 megawatt/min for a 52 gallon system.
  • the present invention has advantages over prior art in the reduced preferred temperature ranges between the ionic solutions; the use of at least one buffering tank; the use of two or more processing tanks— which may vary in shape and design as well as be insulated according to preferred temperature ranges; the use of a set of intermediate ionic solution pathways; the selection of high valence temperature specific salts such as Silver-Nitrate (AgN03) and Ammonium-Nitrate (NH4N03); and the use of at least one automatic flow-valve from the buffering tank allowing this tank to fill before emptying into the two or more processing tanks, further allowing the processing tanks to be switched back and forth from cold-side diluted to hot-side concentrated, causing precipitated sediments to be recycled by dissolving into the hot-side solution, wherein there is no net loss in the electro-chemical cycle.
  • Preferred ranges for this invention are
  • cathode-anode membranes of preferred thickness and cell number such as Fumasep models fks 30, fad 30 or fab 30, obtained from obtained from manufacturer FUMATECH GmbH, create further
  • Electrodes units coated with iridium oxides or titanium -niobium further utilizing K4Fe(CN)6 and K3FE(CN)6 (Potassium-Iron II & III Hexacyonaferrates) as electrode rinsing solutions creating further efficiencies for this invention.
  • K4Fe(CN)6 and K3FE(CN)6 Pitassium-Iron II & III Hexacyonaferrates
  • the method and resulting apparatus may include the use of an external industrial heat source input, instead of relying solely upon the absorption of ambient air heat sequestered from the heat exchangers used by the heat pump to create the temperature differential of the system so as to create additional efficiency advantages.
  • an external industrial heat source input by an industrial process exceeding the operational temperature of the heat pump (140-150 degrees Fahrenheit)
  • the system is able to increase the concentration of solute on the hot side, further increasing the salinity differential between hot and cold sides which corresponds to an increase in power density of the ionic solution.
  • Energy is further conserved through the disclosed use of an underlying processing tank sediment drain activated by an automatic-flow-valve, pumped towards the hot-side of the system at or above 140 degrees F., causing the sediment created on diluted cold-side, to be reabsorbed by the hot-side concentrated ionic solution using heat from processes that produce heating at higher than 140 degrees F, as in heat sources other than a heat pump absorbing heat from the ambient air, an example of this could be concentrated sunlight, or various industrial processes.
  • Additional RED/PRO units may be added, which may be contained in separate systems solutions of opposing enthalpies of solution, and separate electrode rinse cycles. Or the additional RED units may be configured in the same contained system utilizing the same solution constituents and electrode rinse cycle.
  • FIG.1 illustrates the generalized concept and features of the method and apparatus of this invention
  • FIG. 2 is an illustration of the use of the manifold system pathways showing the different flow directions for refrigerant within the two evaporator coils, the expansion valves, the condenser coil, and how these components interconnect to the refrigerant compressor.
  • FIG. 2A is a diagram illustrating a phase in the thermodynamic cycle of the present invention, wherein heat is pumped from a cold side tank and transferred to a hot side tank.
  • FIG. 2B is a diagram illustrating a phase in the thermodynamic cycle of the present invention, wherein the heat is pumped from the ambient environment and transferred to a hot side tank.
  • FIG. 2C is a diagram illustrating a phase in the
  • thermodynamic cycle of the present invention wherein the functions of the tanks are switched from previously hot side to cold side and previously cold side to hot side, and heat is pumped from the newly switched cold side tank and transferred to the newly switched hot side tank.
  • FIG. 2D is a diagram illustrating a phase in the thermodynamic cycle of the present invention, wherein the functions of the tanks are switched from previously hot side to cold side and previously cold side to hot side, and heat is pumped from the ambient environment and transferred to the newly switched hot side tank.
  • FIG. 3 illustrates an embodiment having external heat sources and a precipitate transfer line increasing the salinity difference.
  • FIG. 4 is an illustration of a more efficient fluid flow system utilizing a back-up buffering tank with a heat exchanger loop, and two additional designated hot and cold buffering tanks which do not switch sides (hot to cold; cold to hot) located between the processing tanks and the RED or PRO unit, the purpose is to store hot-concentrated and cold diluted solutions created via the processing tanks, and allow a continuous supply of solution to the RED/PRO system during the dwell time required to heat, and cool the intermediate solution to form the concentrate and dilute solutions within both the heated and cooled processing tanks, before the two solutions have achieved the salinity differential required for a proper RED/PRO electrical production cycle can be initiated.
  • an embodiment of the present invention utilizes a contained ionic fluid system with a reversed-electro- dialysis (RED) or pressure retarded osmosis (PRO) unit
  • RED reversed-electro- dialysis
  • PRO pressure retarded osmosis
  • Buffering tank one acts as a holding tank for incoming fluid from the RED/PRO until buffering tank two (15) has completely drained its contents into both processing tanks (20, 21), at which point buffering tank one is bypassed, buffering tank two continues to accept intermediate solution from the RED, and buffering tank one drains its contents into buffering tank two via automatic valve (16) and pump (11) while buffering tank two, simultaneously receives intermediate solution from buffering tank one bypass line and automatic valve (13).
  • buffering tank two When the buffering tank two (15) is completely full of intermediate solution, buffering tank one bypass line and automatic valve (13) is deactivated (closed), while automatic valve (12) is activated (open) and intermediate solution begins to fill buffering tank one, buffering tank two drains its contents via automatic valves (19, 18) or (19, 17). 50 percent of solution moves through a radiator to decrease solution temperature to ambient environmental temperature (18), and this solution will next enter the processing tank designated the cold-side precipitating tank (20). The additional 50 percent of intermediate solution bypasses radiator (17) and moves through radiator bypass valve (19). As this solution will be received by the processing tank designated the hot-side dissolving tank, the added heat not dissipated to the ambient will be used to dissolve the salt in the concentrated solution hot-side dissolving tank (21).
  • the heat pump is activated.
  • the heat pump is comprised of a refrigerant compressor (22), a condenser coil (23), through which refrigerant and heat is transferred to the liquid in the hot side dissolving tank, an expansion valve (50a, 50b, 50c, 50d) through which refrigerant cooled by the liquid in the dissolving tank is moved to the evaporator coil, and an evaporator coil (24) where heat is removed from the cold-side precipitating tank and transferred by the refrigerant to the compressor (22) to the condenser which radiates this heat to hot-side dissolving tank (21).
  • the condenser coil After the temperature of the cold-side precipitating tank (20) has been reduced to approximately 32 degrees F from 72 degrees starting ambient temp, (37 degree change) and the condenser coil has increased the hot side dissolving tank from 80 degrees (approximate) to 95 degrees (a 15 degree change), a heat pump with a coefficient of performance of 4.5 will begin to suffer efficiency losses if the temperature differential is to increase beyond 68 degrees; to combat this loss, the evaporator coil in the cold side tank (20) is bypassed and heat from the air (72 degrees) is used to heat the dissolving tank (21) using the external evaporator coil (25) to increase the dissolving tank temperature from 95 F to 140 F while the cold side remains at 32F.
  • the heat pump maintains a lower temperature differential between hot and cold sides, which positively influences heat pump efficiency, as efficiency of a heat pump is equal to the reciprocal of the efficiency of a heat engine.
  • the cold side solution is ambient temperature of 72 degrees F
  • the hot side because it bypassed radiator (17)
  • the temperatures of the processing tanks are: 32 degrees F on the cold side and 95 degrees F on the hot side.
  • the temperature differential between the two tanks is 63 degrees, and the temperature differential in the second phase of the cycle, when the heat is taken from the air absorbed by the external evaporator coil (25), and transferred to the dissolving tank, the ambient temperature of the air is 72 degrees, the condenser will transfer heat from the ambient air to the solution until the solution is heated to 140 degrees F.
  • This increase from 72 degrees to 140 F makes this a 68 degree temperature differential, maintaining a high coefficient of performance for the heat pump.
  • the processing tanks are at 32 degrees F and 140 degrees respectively.
  • the hot side tank (21) started with precipitated salt settled at the bottom of the tank and could not dissolve the salt until the intermediate solution at 28 lg per 100 g of H20 was heated to 140 degrees.
  • the 159 grams of precipitate settled at the bottom of the dissolving tank reconstitutes with the solution to total 440 grams of AgN03 in 100 grams of water.
  • the intermediate solution starts at 281 grams at 72 degrees and is cooled to 32 degrees F.
  • the cooled AgN03 solution is at 122 g per 100 grams of water.
  • the unit at this point has two options:
  • Option 1 Drain each tank immediately. The cold side will open automatic valve (30) and close automatic valve (32) thereby heating the cold solution with ambient air, warming the solution while simultaneously cooling the surrounding environment (since the
  • the hot tank solution will close automatic valve (33) and open automatic valve (31) to prevent the heat absorber (35) from dissipating heat to the environment, as this heat is necessary for preventing premature precipitation of the salt dissolved in the hot solution, as it is critical for the solution concentration differential to remain high before entering the RED/PRO unit.
  • the two solutions pass through a manifold system (36).
  • This manifold system detects temperature differences between the two fluids, as the processing tanks alternate roles each cycle to allow the precipitated salt in the cold tank to be dissolved again by redesignating it the hot tank, the manifold system must alternate the direction of the liquids to ensure the hot concentrated liquid will consistently enter the designated concentrated solution buffering tank (38), and the cold diluted liquid will consistently enter the dilute solution buffering tank (37).
  • the purpose of the buffering tanks is to provide a continuous supply of dilute and concentrated solution to the RED, as the processing tanks require time to heat and cool the intermediate solution, in order to manipulate the specific concentrations required in each tank
  • the hot solution enters the RED through pipe (2) and from the cold buffering tank (37) the solution enters the RED from pipe (3)
  • Option 2 After the processing tanks have achieved their temperature differentials of 32 degrees Fahrenheit on the cold side dissolving tank (20) and 140 degrees F on the hot side, the heat pump is deactivated and refrigerant movement is halted. In the hot tank (21), pump (28) is activated and begins pumping concentrated solution to a heat exchanger, which absorbs heat from a heat source beyond the operating temperature of the heat pump. This source heat can be virtually any temperature, however, the solution will be limited to the amount of precipitate available for use, and the precipitate on the cold diluted side is 159 grams per 100 grams of H20.
  • FIG. 2 a processing tank and refrigeration sub system is provided in accordance with one embodiment of the present invention.
  • FIG. 2A is a diagram illustrating a phase in the thermodynamic cycle of the present invention, wherein heat is pumped from a cold side tank and transferred to a hot side tank.
  • FIG. 2B is a diagram illustrating a phase in the thermodynamic cycle of the present invention, wherein the heat is pumped from the ambient environment and transferred to a hot side tank.
  • FIG. 2C is a diagram illustrating a phase in the thermodynamic cycle of the present invention, wherein the functions of the tanks are switched from previously hot side to cold side and previously cold side to hot side, and heat is pumped from the newly switched cold side tank and transferred to the newly switched hot side tank.
  • FIG. 2D is a diagram illustrating a phase in the thermodynamic cycle of the present invention, wherein the functions of the tanks are switched from previously hot side to cold side and previously cold side to hot side, and heat is pumped from the ambient environment and transferred to the newly switched hot side tank.
  • a system for air cooling in accordance with the present invention operates without the use of buffering tanks (37, 38). Manifold system pathways along with flow directions for refrigerant within the two evaporator coils, expansion valves, condenser coil, connect to the refrigerant compressor. [0041] In a variant, FIG.
  • FIG. 4 is an illustration of a more efficient fluid flow system utilizing a back-up buffering tank with a heat exchanger loop, and two additional processing buffering tanks which do not switch sides (hot to cold; cold to hot) located between the processing tanks and the reversed-dialysis unit, the purpose is to store hot-concentrated and cold-diluted solutions created via the processing tanks, and allow a continuous supply of solution to the RED system during the dwell time required to heat, and cool the intermediate solution to form the concentrate and dilute solutions within both the heated and cooled processing tanks, before the two solutions have achieved the salinity differential required for proper RED electrical production cycle to be
  • the system uses a pressure retarded osmosis generator (PRO) and entry lines (2, 3) feed a PRO.
  • PRO pressure retarded osmosis generator
  • a salinity differential heat engine has a heat pump which serves as the primary heat source for the engine and the heat pump establishes a temperature differential between two working fluid solutions.
  • thermodynamic cycle for yields a high thermodynamic efficiency in heat to energy conversion with a low temperature differential between high and low temperature sides, wherein the cycle yields a net ambient temperature cooling effect by directly or indirectly converting ambient environmental low grade heat to electricity or potential kinetic energy or mechanical work.
  • the system comprises a salinity differential heat engine in which heat energy is converted to kinetic or electrical energy via one of pressure retarded osmosis, pressurized gas through volume confinement, and reversed electro dialysis.
  • a method comprising operating a heat engine using a heat pump to extract and convert low grade heat sources into useable work (kinetic energy or electricity) in order to achieve at least a 90% thermal efficiency of the heat engine.
  • a group of items linked with the conjunction“and” should not be read as requiring that each and every one of those items be present in the grouping, but rather should be read as“and/or” unless expressly stated otherwise.
  • a group of items linked with the conjunction“or” should not be read as requiring mutual exclusivity among that group, but rather should also be read as“and/or” unless expressly stated otherwise.
  • items, elements or components of the invention may be described or claimed in the singular, the plural is contemplated to be within the scope thereof unless limitation to the singular is explicitly stated.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un dispositif de refroidissement à air ionique qui comprend un moteur thermique à différence de salinité utilisant une pompe à chaleur comme source de chaleur primaire et le mécanisme par lequel le différentiel de température est obtenu. L'invention concerne également un cycle thermodynamique à boucle fermée qui produit un rendement thermodynamique élevé par conversion de chaleur en énergie avec un différentiel à basse température entre les côtés haut et bas, en plus d'un effet de refroidissement net de la température ambiante par conversion directe ou indirecte de la chaleur ambiante/de la chaleur de faible niveau environnemental en électricité ou en énergie cinétique potentielle ou en travail mécanique. Plus particulièrement, l'invention concerne un dispositif de refroidissement à air ionique qui utilise un moteur thermique à différence de salinité dans lequel l'énergie thermique peut être convertie en énergie cinétique ou électrique au moyen d'une osmose retardée par pression, d'un gaz sous pression par confinement de volume, ou d'une électrodialyse inversée.
PCT/US2017/068386 2017-12-25 2017-12-25 Dispositif de refroidissement à air ionique WO2019132855A1 (fr)

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Application Number Priority Date Filing Date Title
PCT/US2017/068386 WO2019132855A1 (fr) 2017-12-25 2017-12-25 Dispositif de refroidissement à air ionique

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PCT/US2017/068386 WO2019132855A1 (fr) 2017-12-25 2017-12-25 Dispositif de refroidissement à air ionique

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4593531A (en) * 1985-01-15 1986-06-10 Ebara Corporation Absorption cooling and heating apparatus and method
US5600967A (en) * 1995-04-24 1997-02-11 Meckler; Milton Refrigerant enhancer-absorbent concentrator and turbo-charged absorption chiller
US7823396B2 (en) * 2004-06-11 2010-11-02 Surrey Aquatechnology Limited Cooling apparatus
US20130340468A1 (en) * 2011-03-16 2013-12-26 Carrier Corporation Air conditioning system with distilled water production from air
US9677809B1 (en) * 2011-10-10 2017-06-13 Portland General Electric Company Plural heat pump and thermal storage system for facilitating power shaping services on the electrical power grid at consumer premises
US9851129B1 (en) * 2015-05-25 2017-12-26 David John Tanner Ionic air cooling device

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4593531A (en) * 1985-01-15 1986-06-10 Ebara Corporation Absorption cooling and heating apparatus and method
US5600967A (en) * 1995-04-24 1997-02-11 Meckler; Milton Refrigerant enhancer-absorbent concentrator and turbo-charged absorption chiller
US7823396B2 (en) * 2004-06-11 2010-11-02 Surrey Aquatechnology Limited Cooling apparatus
US20130340468A1 (en) * 2011-03-16 2013-12-26 Carrier Corporation Air conditioning system with distilled water production from air
US9677809B1 (en) * 2011-10-10 2017-06-13 Portland General Electric Company Plural heat pump and thermal storage system for facilitating power shaping services on the electrical power grid at consumer premises
US9851129B1 (en) * 2015-05-25 2017-12-26 David John Tanner Ionic air cooling device

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