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WO2017168185A1 - Pompe à chaleur et production d'énergie utilisant des sels hydratés - Google Patents

Pompe à chaleur et production d'énergie utilisant des sels hydratés Download PDF

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Publication number
WO2017168185A1
WO2017168185A1 PCT/GR2017/000016 GR2017000016W WO2017168185A1 WO 2017168185 A1 WO2017168185 A1 WO 2017168185A1 GR 2017000016 W GR2017000016 W GR 2017000016W WO 2017168185 A1 WO2017168185 A1 WO 2017168185A1
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WO
WIPO (PCT)
Prior art keywords
solution
vapor
outlet
electrolyte
vapour
Prior art date
Application number
PCT/GR2017/000016
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English (en)
Inventor
Vasileios STYLIARAS
Original Assignee
Styliaras Vasileios
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
Priority claimed from GR20160100133A external-priority patent/GR20160100133A/el
Priority claimed from GR20160100578A external-priority patent/GR20160100578A/el
Priority claimed from GR20170100114A external-priority patent/GR20170100114A/el
Application filed by Styliaras Vasileios filed Critical Styliaras Vasileios
Priority to AU2017243323A priority Critical patent/AU2017243323A1/en
Priority to CA3021299A priority patent/CA3021299A1/fr
Priority to US16/350,062 priority patent/US20190249909A1/en
Priority to JP2018551416A priority patent/JP2019516056A/ja
Priority to EP17719704.3A priority patent/EP3472535A1/fr
Publication of WO2017168185A1 publication Critical patent/WO2017168185A1/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
    • F25B30/00—Heat pumps
    • F25B30/04—Heat pumps of the sorption type
    • 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
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • F25B15/06—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being water vapour evaporated from a salt solution, e.g. lithium bromide
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems

Definitions

  • This invention refers to a method and the apparatus for thermal compression of a liquid solution and its application for heat transfer based on absorption and adsorption heat pumps and power production from medium temperature heat sources.
  • a saturated solution is cooled from an absorber where it is at high temperature, to lower temperature.
  • This may be an electrolyte solution.
  • Another phase like crystals of electrolyte, is created and separated from the solution.
  • the resulting lower concentration solution is vaporized and the vapor is compressed and driven to absorber, in which the remaining solution is also driven.
  • the lower concentration solution is compressed and heated up to the absorber temperature. It is partially vaporized and the vapor performs a cooling or power cycle and then is absorbed in the absorber.
  • the remaining liquid solution returns to the absorber to where the separated electrolyte is driven to, to form the initial solution. Absorption heat is recovered by evaporation.
  • Another invention (Ref 2) combines two different solutions having the same solvent.
  • the second solution activity does not depend straight on the first solution and may now be much lower than that of the first one, leading to temperature lift. Vapor is produced by the first solution evaporation at low temperature and absorbed by an absorber of the second solution.
  • the second solution is next compressed and heated up to the first solution absorber temperature. It is vaporized there and the vapor returns to the first solution while the rest of the solution returns to the second solution absorber. Cooling, and heating is performed by the solution evaporation and vapor absorption.
  • the vapor pressure of the low (electrolyte) concentration solution is higher than that of the high concentration at the same temperature. Pressure gradient is established between the two solutions although they are at the same temperature. In the same way, two solutions may vaporize at the same pressure but different temperature.
  • Another type of heat pump is the adsorption heat pump in which vapor (gas) is adsorbed by an adsorbent. Operation at high temperature may be achieved but the efficiency is also lower than unit.
  • heat is absorbed, the process is called desorption and the equipment desorber.
  • the reaction can move the opposite direction as well, heat is released, the process is called adsorption and the equipment adsorber.
  • the salt (crystal) that remains when gas has been released, is called regenerated material, as it is ready to adsorb vapour again and release heat.
  • desorbers There are different types of desorbers. Usually, the adsorbent (the salt which is going to adsorb vapor) is stabilized onto a heat transfer material.
  • small size crystals may be provided in a chamber.
  • a thin film of electrolyte may caver the surface of the heat exchanger. This film may adsorb the vapour and then a hot solution passes through and dissolves the crystals or, it may be heated to release the vapour.
  • the space where the crystals are included is a closed space (chamber) provided with a crystal input and output, a vapour output and a pressure valve. This chamber is heated and vapour is produced increasing the pressure. When the pressure reaches a determined level, the valve opens suppling vapour. Vacuum pumps and air compressors may be used to help regulate the pressure during crystal input and output.
  • the coefficient of performance (COP) of the absorption and adsorption cycle is lower than unit.
  • the above stated new cycles have high COP but the temperature lift is considerably lower than in the present invention, even for multi stage compression.
  • the disadvantage of electrolyte hydration turns to advantage now. There is no need for extensive crystallization and separation.
  • the present application can achieve more than 100°C temperature lift applying just one stage compression. Dissolution of just a few moles of electrolyte is enough for the application.
  • the crystals are dissolved into and separated from the solution in cyclic procedure, bypassing the disadvantage of high operation cycles that appear to chemical (adsorption) heat pumps.
  • the adsorbed vapor is dissolved into the solution instead of being desorbed, saving the consumption of the desorption heat and increasing the efficiency.
  • the present invention achieves higher temperature lifting, higher vapor compression and high efficiency, with simplest and more economic method than all the previous methods.
  • Multi stage vapor compression in a way similar to that presented in (Ref.2), is also applied.
  • the hydrated crystals are separated in a few segments, each segment working in different pressure - temperature conditions. Vapor is produced at different pressure levels by the evaporators and disorbers and absorbed or adsorbed at this pressure but higher temperature.
  • the absorption - desorption heat is recovered.
  • the vapor produced at the highest temperature can be expanded for power production before being adsorbed.
  • vapor is produced by adsorption and solution vaporization at low temperature and adsorbed at high temperature. Instead of adsorbent regeneration, dissolution and crystal separation applies, avoiding the consumption of heat of adsorption.
  • the electrolyte crystal that is connected with molecular forces with the solvent is called hereafter hydrated, no matter if the solvent is water or any other solvent.
  • the type of the formed crystal depends on the particular electrolyte and the temperature. Electrolytes which consist of multi charged ions, usually form crystals of high degree of hydration (mainly with water and ammonia). Polar solvents of small molecules, like water and ammonia, form complexes ease. For example, the solubility of pyrosulfite, Na 2 S 2 0 5 , in water is 5M (mole/kg water)at 100 °C and crystallizes as pure crystal. At 10°C the solubility is 3M and crystallizes as pure crystal again.
  • the solubility is 2.5M and the crystal is hydrated with six water molecules (Na 2 S 2 0 5 *6H20).
  • the solubility of CuS0 4 is 0.9M at 0°C and is crystallized with 5 moles of H20, four of which are with strong bond in the form of [Cu(H20) 4 ] 2+ and the one with weak bond.
  • Its solubility at 50°C is 2.5* H20 and at 1 10°C is 4.8*3 H20 while at 130°C the solubility is 5*3H20.
  • the solubility of Na 2 S0 4 is 1 *10 at 0 °C and 3.4M as pure crystal at 40°C.
  • FIG. 1 shows the equipment of crystal dissolution ( ⁇ 1 ) from where the solution is cooled, the equipment (K1 ) and (K1.1 ) where the separated crystals of low and high degree of hydration respectively are stored, the vapor generator (E1 ), the desorbent (E2), and the two adsorbents (A2).
  • Fig. 2 shows the combination of two solutions.
  • ( ⁇ 2) is the crystal dissolution equipment and
  • (K2) is the crystal storage equipment of the second solution.
  • (A1 ) are two absorbers of the second solution.
  • (E1 ) is the vapor generators of the solution
  • (A1 ) is the absorber for the vapor from (E1).
  • (EA1), (AE1 ) is the vapor generator and absorber respectively
  • (H1.1 ),(H1.2), (H1.3) are heat exchangers which are used for recovery of heat through the solutions, gases and crystals and from the absorber (AE1 ), ( ⁇ 1 ) and ( ⁇ 2) are dissolution equipments.
  • a saturated electrolyte solution is cooled from the dissolution equipment ( ⁇ 1 ).
  • the solubility decreases and another phase like electrolyte crystals are formed, separated from the solution and gathered into a storage tank (K1.1 ). These crystals are in hydrated form at this temperature and pressure.
  • the solution contains more electrolytes which are soluble in the solvent and cause strong negative deviation from the ideal solution but their concentration is lower than that determined by the solubility, so that they do not separate.
  • the separated electrolyte is called basic electrolyte , to distinguish from other dissolved electrolytes.
  • the remaining solution is heated, expands, enteYs an absorber (A1 ) and then is successively compressed and driven to other absorbers (A1 ).
  • the crystals from (K1 .1 ) are driven to desorbers (E2), heated to release vapor at a determined pressure, and the vapor is driven to absorbers (A1 ) to be absorbed.
  • the use of a few desorbers (E2) is preferred to supply vapb? to each absorb (A1 ), so that when the vapor from an (E2) is depleted, vapor from the next (E2) is supplied to ensure continuous vapor flow. Besides, more (E2) are used so that vapor can be produced at different pressure levels.
  • Each set of (E2) working at the same pressure is combined with an absorber (A1 ).
  • the crystals from (K1 .1 ) are first driven to an (E2) where the physically bonded moisture, is first vaporized.
  • the pressure of the solution, leaving absorbers (A1 ), is regulated, heated (or cooled, depending on the absorption and dissolution temperature )and driven to the dissolution equipment ( ⁇ 1 ), where the remaining in (E2) crystals of lower hydration degree, are also driven to be dissolved and form the initial solution.
  • the pressure of (E2) is selected according to the available heat source temperature.
  • the vapor that is produced at the highest temperature may be expanded for power production.
  • the solution may be expanded before crystal separation, depending on the required temperature- pressure conditions. In this case, crystals from (E2) are compressed before enter ( ⁇ 1 ). Solution cooling and crystal separation may take place in more that one stages and the dissolution may be performed in the same stages into the solution that returns to ( ⁇ 1 ) after (A1 )
  • Poiar substances of low boiling point and small molecular weight like water, ammonia, alcohols like methanol, e.t.c. are preferred for solvent.
  • Mixtures (solutions) of substances of considerable different boiling point may also be used.
  • the more volatile substance is called gas.
  • Such an example is a water / ammonia solution.
  • the pressure, the temperature and the basic electrolyte of the solution that is being cooled is selected so as the formation of crystals hydrated with the more volatile substance are favored.
  • the pressure of (E2) is also regulated so as desorption of this substance is favored.
  • Electrolytes composed of multi charge ions appearing high degree of hydration at low temperature, are suggested.
  • It may be calcium chloride CaCI2, cupper salts, magnesium sulfateMgS04, e.t.c, depending on the desired temperature lift. Electrolytes of single charge ions that are not hydrated or are a little hydrated, like KCL04, sodium NaOH and potasium KOH hydroxides, lithium chloride and lithium nitrate LiN03, are suggested for the case the adsorption is based mainly on the moisture of crystals. A heat exchanger, transfers heat from the being cooled solution to that which is heated after cooling. The temperature of crystal dissolution is that corresponding to their hydration number.
  • the solution is cooled from ( ⁇ 1 ) to the lower temperature in which the basic electrolyte is formed in the lowest hydration degree , preferably as pure crystal .
  • the formed crystals are gathered in a storage tank (K1 ) .
  • the solution is cooled again and crystals of higher hydration degree are gathered in (K1 .1 ).
  • Crystals from (K1 ) are dried and driven to the adsorbers (A2).
  • the remaining solution after the last separation, is expanded and enters vapor generator (E1 ) where part of the solvent is vaporized.
  • the vapor is adsorbed by crystals ia one of the adsorbers (A2).
  • Crystals from (K1.1 ) are driven to (E2) and the produced vapor is driven for adsorption by another (A2).
  • the remaining solution, as well as, the crystals from (A2) and (E2), are driven to ( ⁇ 1 ) to reform the initial solution.
  • crystals from E2 and A2 are dissolved in different dissolution equipment ( ⁇ 1 ), according to their hydration degree.
  • Thesolution from the one ( ⁇ 1 ) enters the next ( ⁇ 1 ).
  • the fluxes of solution, crystals and vapor that are heated recover heat from the solution that is cooled. Heating, is the most effective drying way for crystals of (K1 ).
  • the resulting vapor may either be absorbed by the solution or be condensed.
  • the crystals from (K1 ) are driven to a desorber (E2.2), the resulting vapor from the drying process, is heated by a few degrees and compressed so that its condensation temperature becomes higher than that of vaporization from the crystals.
  • the vapor is driven to the heat providing section of the (E2.2) to dry the next amount of crystals.
  • the condensed vapor which is solvent in liquid phase, is driven to a vapor generator (E1 ) for vaporization.
  • the solution in ( ⁇ 1 ) may be saturated in a second electrolyte, which electrolyte is now separated during the first cooling stage and is gathered in (K1). These crystals are dried and driven to (A2).
  • the second electrolyte has been selected so as the vapor adsorption temperature is higher than that of the basic electrolyte under the same conditions.
  • the pressure of (E2) has been selected so that only solvent from the basic electrolyte crystals is vaporized.
  • An example is the use of calcium chloride (CaCI2) as basic and the zinc chloride (ZnCI2) as second electrolyte, using ammonia as solvent.
  • a first solution is combined with a second solution having the same solvent and the same basic electrolyte. Additional soluble electrolytes have been dissolved into the second solution to create strong negative deviation. Only the basic electrolyte has been dissolved in the first solution, which electrolyte is separated and stored into (K1 ) and (K1.1 ) under different hydration degree.
  • the basic electrolyte is preferred to be slightly soluble and crystallize as pure crystal in the first stage of cooling.
  • the remaining after the cooling process solution enters vapor generator (E1 ), where part of the solvent is vaporized. Crystals from (K1.1 ) are driven to (E2) where vapor is also produced.
  • the crystals from (K1 ), are driven to a dissolution equipment of the second solution ( ⁇ 2). From there, the second solution is cooled and electrolyte is separated under higher than in (K1 ) hydration degree and stored in a storage tank (K2). The remaining solution is heated and enters absorbers (A1 ) and from there enters ( ⁇ 2). The vapor from (E1 ) is absorbed by the one absorber (A1 ) and the vapor from (E2) by the other (A1 ). The second solution is compressed to the proper pressure after each absorber. The crystals from (K2) are driven to ( ⁇ 1 ) to be dissolved. The crystals from (E2) are dissolved into ( ⁇ 1 ).
  • the amount of crystals transferred from (K1 ) to the second solution equals the amount of crystals that is transferred from (K2) to the first solution.
  • the solvent that is transferred as vapor from (E1 ) and (E2) to the second solution returns to the first solution through the hydrated crystals of (K2).
  • Highly soluble electrolytes, in water are: NaOH, KOH, LiOH, ZnCI2, LiBr and combination of those.
  • ammonia NaSCN, LiSCN, LiN03 may be used as soluble electrolytes.
  • the first solution is saturated at temperature 100°C in ( ⁇ 1 ). From there, it is cooled to 10°C where the solubility is 3M. Thus, 2 mole of the salt are separated and gathered in (K1) as pure crystals. The solution is cooled again to 0°C where the solubility is 2.5 M and 0.5 mole of Na 2 S20 5 * 6H20 are separated in (K1.1). The remaining solution is vaporized and 12 mole of water vapor are produced and absorbed by the second solution (A1 ).
  • the second solution starts cooling from ( ⁇ 2) where the concentration is 4.5 M, down to 0°C (2.5 M), rejecting (4.5-2.5) 2 mole of Na 2 S 2 0 5 * 6H20 (K2).
  • the desorbent (E2) is not used.
  • the crystals from (K1.1 ) are dissolved into ( ⁇ 1).
  • 2 mole of pure salt from (K1) are dissolved into ( ⁇ 2) and 2 moles of Na 2 S 2 0 5 * 6H20 from (K2) are dissolved into ( ⁇ 1 ).
  • 2 moles of salt are transferred from the first to the second solution and vice versa.
  • 12 moles of water are transferred as vapor from the first solution to the second and return to the first solution through the salt (2 mole salt * 6H20).
  • Soluble electrolytes like KOH, ZnCI2, LiBr are also dissolved into the second solution, so that the water activity in (A1) is much lower than in (E1).
  • the application works better using as solvent, a volatile substance dissolved into a liquid solvent.
  • the volatile substance is vaporized in ( E1 ), while the liquid solvent does not form hydrates with the salt.
  • a mix solvent may be ammonia dissolved into organic polar liquid of long chain molecule like high boiling point amines and PG.
  • the pressure during cooling, is regulated to favor the formation of hydrates of the volatile substance only.
  • the solution from ( ⁇ 1 ), is cooled, expands, enters an absorber (A1), absorbs vapor coming from a vapor generator (E1 ), is compressed to the pressure of ( ⁇ 1), is cooled through an absorber (AE1) absorbing vapor coming from the described below vapor generator (EA1 ), keeps cooling and rejects the electrolyte which is stored into the storage tank (K1.1).
  • the solution expands and enters vapor generator (E1) where part of the vapor is released and absorbed by (A1 ) as stated above.
  • the solution is compressed, heated and enters another dissolution equipment ( ⁇ 2) in which another electrolyte is dissolved and then the solution enters the vapor generator (EA1 ) that stated above. Vapor is released there and then the solution is cooled to separate this electrolyte and then the solution is heated and enters ( ⁇ 1 ).
  • the solvent is a pure polar solvent like water or ammonia as stated before. Vaporizing the solution through (EA1 ), the amount of solvent in the solution is reduced, consequently the resulting solution entering (A1), has higher electrolyte concentration and lower solvent vapor pressure.
  • the solution entering (AE1) has higher solvent concentration than that exiting (EA1) because of the solvent which absorbed into (A1).
  • the dissolved in ( ⁇ 2) electrolyte is selected to carry and add to the solution which is vaporized, a lot of solvent molecules, meaning that it is a highly hydrated electrolyte.
  • the dissolved into ( ⁇ 1 ) electrolyte is selected not to be hydrated but exhibiting negative deviation.
  • the method is applicable even by dissolving only one of the electrolytes.
  • the method is also applicable in the case that a gas has been dissolved into the solvent and electrolytes that decrease and increase gas solubility are dissolved into (EA1) and (AE1) respectively.
  • the change in solvent solubility can be repeated by applying a second pair of (EA1/AE1), in a way that the solution exiting the first (EA1), enters the second (EA1) and rejecting electrolyte after the first (AE1 ), enters the second (AE1 ).
  • the same set up can be repeated and the first apparatus cooperates with the second, in a way that he vapor from the (E1) of the first set up is absorbed by the absorber (A1) of the second set up and the vapor from (E1) of the second set up is absorbed by the absorber (A1) of the first.
  • the absorber of the outlet of this machine is connected at the liquid exit of the crystallizer unit (K1)
  • a fifth application two solutions are combined.
  • Mixed solvent liquid- gas
  • the dissolved in ( ⁇ 2) electrolyte is such that increases the gas pressure (reduces the gas solubility).
  • the dissolved in ( ⁇ 1 ) electrolyte increases the gas solubility.
  • the method can work applying only dissolution in ( ⁇ 2).
  • the two or just one of the electrolytes are used to equalize the gas pressure of (E) with (A), so that these equipments work at the same pressure and temperature.
  • the gas concentration in the second solution (A1) is lower than in the first (E1).
  • Vapor generators evaporators
  • absorbers evaporators
  • heat exchangers evaporators
  • liquid pumps evaporators
  • Heat exchangers may also be used for the recovery of absorption heat from the vapor generators. It is preferred though, that vapor generator is included into the absorber. The vaporized solution passes inside of tubes. The produced vapor is separated from the remaining solution and is driven into the absorber shell that surrounds the vapor generator tubes. In the same space is driven the liquid which is going to absorb the vapor. Ionic liquid can be used when electrolyte is not dissolved, or as electrolyte when it crystallizes and separates at low temperature. Gas selectively permeable membrane can used during vaporization. The crystals may be separated by deposition alternatively on the one and the other heat transfer surface and dissolved by the heating solution which flows from the other side.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Sorption Type Refrigeration Machines (AREA)

Abstract

Cycle thermodynamique pour la valorisation de la chaleur et la production d'énergie, combinant des processus d'absorption, d'adsorption et de désorption, promettant un rendement élevé pour des applications de pompe à chaleur et une production d'énergie renouvelable basse-température. La régénération d'adsorbant a été remplacée à partir de la dissolution et de la séparation de cristaux d'électrolyte issus d'une solution d'électrolytes, ce qui permet d'économiser la consommation de chaleur de régénération.
PCT/GR2017/000016 2016-04-01 2017-03-28 Pompe à chaleur et production d'énergie utilisant des sels hydratés WO2017168185A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
AU2017243323A AU2017243323A1 (en) 2016-04-01 2017-03-28 Heat pump and power production utilizing hydrated salts
CA3021299A CA3021299A1 (fr) 2016-04-01 2017-03-28 Pompe a chaleur et production d'energie utilisant des sels hydrates
US16/350,062 US20190249909A1 (en) 2016-04-01 2017-03-28 Heat pump and power production utilizing hydrated salts
JP2018551416A JP2019516056A (ja) 2016-04-01 2017-03-28 水和塩を利用するヒートポンプ及び発電
EP17719704.3A EP3472535A1 (fr) 2016-04-01 2017-03-28 Pompe à chaleur et production d'énergie utilisant des sels hydratés

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
GR20160100133 2016-04-01
GR20160100133A GR20160100133A (el) 2016-04-01 2016-04-01 Αντλια θερμοτητας και παραγωγη εργου με διαχωρισμο ηλεκτρολυτη
GR20160100578 2016-11-04
GR20160100578A GR20160100578A (el) 2016-11-04 2016-11-04 Αντλια θερμοτητας και παραγωγη εργου με εκροφηση αεριου
GR20170100114A GR20170100114A (el) 2017-03-22 2017-03-22 Αντλια θερμοτητας με απορροφηση και χρηση ενδιαλυτωμενων ηλεκτρολυτων
GR20170100114 2017-03-22

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WO2017168185A1 true WO2017168185A1 (fr) 2017-10-05

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US (1) US20190249909A1 (fr)
EP (1) EP3472535A1 (fr)
JP (1) JP2019516056A (fr)
AU (1) AU2017243323A1 (fr)
CA (1) CA3021299A1 (fr)
WO (1) WO2017168185A1 (fr)

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JP2019516056A (ja) 2019-06-13
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US20190249909A1 (en) 2019-08-15
AU2017243323A1 (en) 2018-12-06

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