US20110126552A1 - Producing Cold by a Thermochemical Method for Air-Conditioning a Building - Google Patents

Producing Cold by a Thermochemical Method for Air-Conditioning a Building Download PDF

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Publication number
US20110126552A1
US20110126552A1 US11/793,521 US79352105A US2011126552A1 US 20110126552 A1 US20110126552 A1 US 20110126552A1 US 79352105 A US79352105 A US 79352105A US 2011126552 A1 US2011126552 A1 US 2011126552A1
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heat
temperature
phase
regenerated
during
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US11/793,521
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English (en)
Inventor
Driss Stitou
Jean-Pierre Coudert
Bernard Spinner
Caroline Spinner Brossard
Anne Christel Spinner Kohler
Bruno Spinner
Martin Spinner
Camille Spinner
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Centre National de la Recherche Scientifique CNRS
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Publication of US20110126552A1 publication Critical patent/US20110126552A1/en
Assigned to CENTRE NATIONAL DE LA RECHERCHE SCIENTIFIQUE reassignment CENTRE NATIONAL DE LA RECHERCHE SCIENTIFIQUE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SPINNER (HEIR OF BERNARD SPINNER-DECEASED), BRUNO, BROSSARD (HEIR OF BERNARD SPINNER-DECEASED), CAROLINE SPINNER, KOHLER (HEIR OF BERNARD SPINNER-DECEASED), ANNE CHRISTEL SPINNER, COUDERT, JEAN-PIERRE, SPINNER (HEIR OF BERNARD SPINNER-DECEASED), CAMILLE, SPINNER (HEIR OF BERNARD SPINNER-DECEASED), MARTIN, STITOU, DRISS
Abandoned legal-status Critical Current

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    • 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
    • F25B17/00—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type
    • F25B17/08—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type the absorbent or adsorbent being a solid, e.g. salt
    • F25B17/086—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type the absorbent or adsorbent being a solid, e.g. salt with two or more boiler-sorber/evaporator units
    • 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
    • F25B17/00—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption 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
    • F25B27/00—Machines, plants or systems, using particular sources of energy
    • F25B27/002—Machines, plants or systems, using particular sources of energy using solar energy
    • F25B27/007—Machines, plants or systems, using particular sources of energy using solar energy in sorption type systems
    • 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
    • F25B2315/00—Sorption refrigeration cycles or details thereof
    • F25B2315/005—Regeneration
    • 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
    • Y02A30/272—Solar heating or cooling
    • 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
    • Y02B10/00—Integration of renewable energy sources in buildings
    • Y02B10/20—Solar thermal

Definitions

  • the present invention relates to a device for producing of refrigeration by a thermochemical method, for air conditioning a building.
  • the system consisting of a thermochemical dipole using two reversible thermochemical processes is a means known per se for producing of refrigeration.
  • the thermochemical dipole comprises a reactor BT, a reactor HT and means for exchanging a gas between BT and HT.
  • the two reactors are the seat of reversible thermochemical processes selected such that, at a given pressure in the dipole, the equilibrium temperature in BT is lower than the equilibrium temperature in HT.
  • the reversible process in the reactor HT employs a sorbent S and a gas G and may be a reversible adsorption of G by S or a reversible chemical reaction of S and G, according to the equation
  • the reversible process in the reactor BT employs the same gas G. It may be a liquid/gas phase change of the gas G or a reversible adsorption of G by a sorbent S 1 or a reversible chemical reaction of S 1 and G, the sorbent S 1 being different from S.
  • the production of refrigeration step of the device corresponds to the synthesis step in HT
  • the regeneration step corresponds to the decomposition step in HT
  • thermochemical process in BT and the thermochemical process in HT are such that:
  • thermochemical process in a reactor BT is generally a liquid/gas phase change of G.
  • BT is then an evaporator/condenser unit EC.
  • thermochemical devices for air conditioning buildings is attractive, insofar as the devices concerned are quiet and do not generate vibrations.
  • these devices use the subsoil as a heat sink, which is virtually permanently at a temperature of 15° C. in temperate regions.
  • the air conditioning is mainly necessary during very hot periods, it may be possible to use the solar energy which is particularly abundant during these periods.
  • the heat collected by inexpensive flat collectors is at a temperature which generally does not exceed 70° C. Much higher temperatures can only be obtained with high technology and particularly expensive solar collectors, such as vacuum collectors, or parabolic or cylindro-parabolic concentration collectors.
  • the solar energy undergoes variations in intensity, on the one hand during the year, and on the other during a day.
  • Thermochemical processes are known for producing of refrigeration from a heat source at a temperature Tc of about 70°, and a heat sink at a temperature To of about 15° C.
  • a heat source at a temperature Tc of about 70°
  • a heat sink at a temperature To of about 15° C.
  • use can be made in the reactor BT of the dipole, of an L/G phase change of ammonia (NH 3 ), methylamine (NH 2 CH 3 ) or H 2 O.
  • thermochemical dipoles operating between a heat source at a temperature Tc associated with solar energy and a heat sink at a temperature To of about 15° C., particularly using known thermochemical processes employing a working gas such as ammonia, methylamine or water.
  • the present invention relates to a device and a thermochemical method for air conditioning a building using an intermittent heat source whereof the maximum temperature is about 70° C. and a heat sink at a temperature of about 15° C.
  • FIG. 1 shows, on a Clapeyron diagram, the variation in the temperature and pressure conditions in the device during each of the active phases.
  • the curves 2 correspond to the thermochemical equilibrium in each of the reactors, and the curves 1 correspond to the thermochemical equilibrium in each of the evaporators-condensers.
  • the letters a, b and c indicate the dipole concerned by the variation.
  • FIG. 2 shows, on a Clapeyron diagram, the variation in the temperature and pressure conditions in the device during each of the phases.
  • the curves 2 correspond to the thermochemical equilibrium in each of the reactors, and the curves 1 correspond to the thermochemical equilibrium in each of the evaporators-condensers.
  • the letters a, b and c indicate the dipole concerned by the variation.
  • FIG. 3 shows, on a Clapeyron diagram, the variation in the temperature and pressure conditions in the device during each of the active phases.
  • the curves 1 correspond to the thermochemical equilibrium in each of the evaporators-condensers
  • the curves 2 correspond to the thermochemical equilibrium in each of the reactors Ra and Rc
  • the curves C correspond to the thermochemical equilibrium in the reactors Rb and Rd.
  • the letters a, b, c and d indicate the dipole concerned by the variation.
  • FIG. 4 shows the particular Clapeyron diagram for the phases M 1 and M 2 .
  • refrigeration may be produced at a temperature close to 0° C. using a heat source lower than 50° C.
  • FIG. 5 shows the particular Clapeyron diagram for phases H 1 , H 2 and M 2 .
  • refrigeration may be produced at a temperature close to 0° C. using a heat source lower than 70° C.
  • the inventive device comprises three or four thermochemical dipoles each comprising an evaporator-condenser unit EC and a reactor R connected by means for circulating a gas G between them and means for interrupting the gas flow. It is characterized in that:
  • the temperature in R is naturally higher than the temperature in EC, for a given dipole.
  • thermochemical processes in the various dipoles preferably have similar equilibrium curves to limit the external heat losses of the reactors.
  • Two equilibrium curves of two thermochemical processes are considered to be similar when, at a given equilibrium pressure, the respective equilibrium temperatures differ by not more than 15° C. It is particularly advantageous to select the same thermochemical process in all the dipoles.
  • the dipoles of the inventive device are denoted below by Da (consisting of the evaporator-condenser ECa and the reactor Ra), Db (consisting of ECb and Rb), Dc (consisting of ECc and Rc), and optionally Dd (consisting of ECd and Rd).
  • the solar collectors supply heat available at a temperature Tc that varies according to the phases of the cycle.
  • Tc a temperature that varies according to the phases of the cycle.
  • the heat supplied is close to the value Th of about 70° C.
  • the heat produced is an intermediate temperature Tm of between Th and To but nevertheless usable as a heat source.
  • the heat is at a temperature Tb close to the ambient temperature To, and therefore too low to be usable as a heat source.
  • the method of the present invention is intended for producing of refrigeration by 24-hour cycles which each comprise the successive phases M 1 , H 1 , H 2 , M 2 , B, using a heat source whereof the temperature is at a value Th of about or higher than 70° C. during the phases H 1 and H 2 , at an intermediate value Tm during the phases M 1 and M 2 , and at a value Tb close to the ambient temperature during phase B. It is characterized in that it consists in operating the inventive device, in order to create internal heat sources at a temperature above the temperature of the external source, during the periods when said temperature is too low, particularly during phases M 1 and M 2 .
  • the producing of refrigeration method of the invention consists in operating the inventive device under the following conditions:
  • a given dipole is totally or partially regenerated at the end of a complete cycle, according to the quantity of heat available during the regeneration step and the quantity of refrigeration required during the production of refrigeration step of a complete cycle.
  • the inventive method is implemented in a device consisting of three dipoles Da, Db and Dc in which the thermochemical processes are identical, in order to produce refrigeration during phases H 1 and H 2 during which the heat is available at the highest temperature Th, during phase M 2 during which the heat is available at an intermediate temperature Tm, the device being in regeneration during phase M 1 and inactive in phase B.
  • FIG. 1 shows, on a Clapeyron diagram, the variation in the temperature and pressure conditions in the device during each of the active phases.
  • the curves 2 correspond to the thermochemical equilibrium in each of the reactors, and the curves 1 correspond to the thermochemical equilibrium in each of the evaporators-condensers.
  • the letters a, b and c indicate the dipole concerned by the variation.
  • the evaporator-condenser is isolated from the reactor in each of the dipoles, and the various dipoles are in the following state:
  • phase M 1 the gas connection between ECa and Ra is opened, on the one hand, and between ECc and Rc on the other, and heat is added at the temperature Tm to ECc of the dipole Dc (point D 1 ).
  • This heat addition causes the evaporation of the gas G which is transferred to the reactor Rc in which the exothermic synthesis phase then takes place (point S 2 ).
  • the heat liberated by said synthesis is transferred to Ra where it causes the liberation of the gas G (point D 2 ).
  • the gas liberated in Ra is transferred to ECa where it condenses while liberating heat (point S 1 ).
  • the dipoles are in the following state:
  • phase H 1 the gas connection between ECb and Rb is opened.
  • phase H 1 the dipoles Db and Dc are regenerated by direct addition of heat at the temperature Th in Rb and Rc (points D 2 ).
  • the gas liberated in Rb and Rc is transferred respectively to ECb and ECc where it condenses (points S 1 ).
  • refrigeration is produced by the dipole Da in ECa by removing heat from the medium to be cooled (point D 1 ).
  • the dipoles are in the following state:
  • phase H 2 heat is added at the temperature Th to the reactors Ra and Rb (points D 2 ) to continue regenerating Db and to start regenerating Da. Simultaneously, refrigeration is produced spontaneously in ECb (point D 1 ).
  • the dipoles are in the following state:
  • phase M 2 heat is added at the temperature Tm to ECa (point D 1 ) to cause the exothermic synthesis in Ra whereof the heat is transferred to Rc to regenerate the dipole Dc. Simultaneously, refrigeration is produced spontaneously in ECb.
  • the dipoles are in the following state:
  • phase M 2 At the end of phase M 2 , the gas connections between the evaporators-condensers and the reactor of the same dipole are closed and the installation is left as such during phase B, up to the start of phase M 1 of the next cycle.
  • the method is implemented in a device which comprises three identical dipoles Da, Db and Dc, in order to produce refrigeration during all the phases of a 24-hour cycle.
  • FIG. 2 shows, on a Clapeyron diagram, the variation in the temperature and pressure conditions in the device during each of the phases.
  • the curves 2 correspond to the thermochemical equilibrium in each of the reactors, and the curves 1 correspond to the thermochemical equilibrium in each of the evaporators-condensers.
  • the letters a, b and c indicate the dipole concerned by the variation.
  • the evaporator-condenser is isolated from the reactor in each of the dipoles, and the various dipoles are in the following state:
  • phase M 1 heat is added at the temperature Tm to ECc (point D 1 / c ) to cause the exothermic synthesis in Rc (point S 2 / c ) whereof the heat is transferred to Rb (point D 2 / b ) to regenerate the dipole Db. Simultaneously, refrigeration is produced spontaneously at ECa (point D 1 / a ).
  • the dipoles are in the following state:
  • phase H 1 the dipoles Db and Dc are regenerated by direct addition of heat at the temperature Th in Rb and Rc (points D 2 / b and D 2 / c ). Simultaneously, refrigeration continues to be produced at ECa (point D 1 / a ). At the end of phase H 1 , the dipoles are in the following state:
  • phase H 2 heat is added at the temperature Th to the chambers Ra and Rc (points D 2 / a and D 2 / c ) to continue regenerating Dc and to start the regeneration of Da. Simultaneously, refrigeration is produced spontaneously at ECb (point D 1 / b ).
  • the dipoles are in the following state:
  • phase M 2 At the end of phase M 2 , the gas connections between ECb and Rb are closed on the one hand, and between ECc and Rc on the other. During phase B, the gas connection is maintained in the dipole Da and refrigeration is produced at ECa (point D 1 / a ). At the end of phase M 2 , the dipoles are in the following state:
  • phase B the device continues to produce refrigeration by the dipole Da.
  • the method is implemented in a device which comprises four dipoles Da, Db, Dc and Dd, in order to produce refrigeration during phases H 1 , H 2 , M 2 and B, the device being in regeneration during phase M 1 .
  • the dipoles Da and Db are thermally coupled.
  • the dipoles Dc and Dd are thermally coupled.
  • FIG. 3 shows, on a Clapeyron diagram, the variation in the temperature and pressure conditions in the device during each of the active phases.
  • the curves 1 correspond to the thermochemical equilibrium in each of the evaporators-condensers
  • the curves 2 correspond to the thermochemical equilibrium in each of the reactors Ra and Rc
  • the curves C correspond to the thermochemical equilibrium in the reactors Rb and Rd.
  • the letters a, b, c and d indicate the dipole concerned by the variation.
  • the reactors Ra and Rc of the dipoles Da and Dc are the seat of the same thermochemical process, and the reactors Rb and Rd of dipoles Db and Dd are the seat of the same process, different from the one taking place in the dipoles Da and Dc. Furthermore, all the chemical processes employ the same working gas G, so that all the evaporators-condensers are the seat of a liquid-gas phase change of the same gas G.
  • the equilibrium temperatures in the various chambers are as follows:
  • phase M 1 the gas connection between ECa and Ra is opened on the one hand, and between ECb and Rb on the other, heat is added at the temperature Tm to ECa (point E 1 / a ) of the dipole Da to cause the exothermic synthesis in Ra (point S 2 / a ) whereof the heat is transferred to Rb (point D 3 / b ) to regenerate the dipole Db.
  • the dipoles are in the following state:
  • phase H 1 the gas connection between ECa and Ra is opened on the one hand, and between Ecd and Rd on the other.
  • heat is added at the temperature Tm to ECc of the dipole Dc (point D 1 / c ) to cause the exothermic synthesis in Rc (point S 2 / c ) whereof the heat is transferred to Rd (point D 3 /D) to regenerate the dipole Dd.
  • refrigeration is produced spontaneously at ECb (point E 1 / b ), causing the exothermic synthesis in Rb (point S 3 / b ) whereof the heat is transferred to Ra (point D 2 / a ) to regenerate the dipole Da.
  • the dipoles are in the following state:
  • phase H 2 heat is added at the temperature Tm to ECa (point E 1 / a ) of the dipole Da to cause the exothermic synthesis in Ra (point S 2 / a ) whereof the heat is transferred to Rb (point D 3 / b ) to regenerate the dipole Db.
  • refrigeration is produced spontaneously at ECd (point E 1 / d ), causing the exothermic synthesis in Rd (point S 3 / d ) whereof the heat is transferred to Rc (point D 2 / c ) to regenerate the dipole Dc.
  • the dipoles are in the following state:
  • phase M 2 heat is added at the temperature Tm to ECc (point E 1 / c ) of the dipole Dc to cause the exothermic synthesis in Rc (point S 2 / c ) whereof the heat is transferred to Rd (point D 3 / d ) to regenerate the dipole Dd.
  • refrigeration is produced spontaneously at ECb (point E 1 / b ), causing the exothermic synthesis in Rb (point S 3 / b ) whereof the heat is transferred to Ra (point D 2 / a ) to regenerate the dipole Da.
  • the dipoles are in the following state:
  • phase M 2 At the end of phase M 2 , the gas connections between ECa and Ra are closed on the one hand, and between ECb and Rb on the other.
  • phase B refrigeration is produced spontaneously at Rd (point E 1 / d ), causing the exothermic synthesis in Rd (point S 3 / d ) whereof the heat is transferred to Rc (point D 2 / c ) to regenerate the dipole Dc.
  • the dipoles At end of phase B, the dipoles are in the following state:
  • This example illustrates an implementation of the 2 nd embodiment of the inventive method.
  • the evaporator-condenser of each of the three dipoles is the seat of a liquid/gas phase change of NH 3 .
  • the reactor of each of the dipoles is the seat of a reversible chemical reaction between NH 3 and BaCl 2 .
  • FIG. 4 shows the particular Clapeyron diagram for the phases M 1 and M 2 .
  • refrigeration may be produced at a temperature close to 0° C. using a heat source lower than 50° C.
  • This example illustrates an implementation of the 3 rd embodiment of the inventive method.
  • the evaporator-condenser of each of the four dipoles is the seat of a liquid/gas phase change of NH 3 .
  • the reactor of each of the dipoles Da and Dc is the seat of a reversible chemical reaction between NH 3 and BaCl 2 .
  • the reactor of the dipole Db and Dd is the seat of a reversible chemical reaction between NH 3 and ZnSO 4 .
  • FIG. 5 shows the particular Clapeyron diagram for phases H 1 , H 2 and M 2 .
  • refrigeration may be produced at a temperature close to 0° C. using a heat source lower than 70° C.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Other Air-Conditioning Systems (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US11/793,521 2004-12-20 2005-12-13 Producing Cold by a Thermochemical Method for Air-Conditioning a Building Abandoned US20110126552A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR0413569A FR2879727B1 (fr) 2004-12-20 2004-12-20 Dispositif pour la production de froid pour la climatisation d'un batiment
FR0413569 2004-12-20
PCT/FR2005/003119 WO2006067302A2 (fr) 2004-12-20 2005-12-13 Production de froid par un procede thermochimique, pour la climatisation d'un batiment.

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US20110126552A1 true US20110126552A1 (en) 2011-06-02

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US11/793,521 Abandoned US20110126552A1 (en) 2004-12-20 2005-12-13 Producing Cold by a Thermochemical Method for Air-Conditioning a Building

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US (1) US20110126552A1 (fr)
EP (1) EP1831616B1 (fr)
JP (1) JP5101297B2 (fr)
ES (1) ES2648389T3 (fr)
FR (1) FR2879727B1 (fr)
WO (1) WO2006067302A2 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102954618B (zh) * 2011-08-31 2015-06-03 成都易生玄科技有限公司 一种缩聚、传输太阳光制冷的方法

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2456386A (en) * 1946-05-07 1948-12-14 Howell C Cooper Cascade refrigeration unit with controls therefor
US3585810A (en) * 1968-07-15 1971-06-22 G U E Zimmermann Intermittent absorption refrigerating machine
US4135371A (en) * 1976-05-18 1979-01-23 Fritz Kesselring Storage element for a sorption heat storage system
US5174367A (en) * 1989-03-13 1992-12-29 Sanyo Electric Co., Ltd. Thermal utilization system using hydrogen absorbing alloys
US5335519A (en) * 1991-07-26 1994-08-09 Societe Nationale Elf Aquitaine Plant for producing cold by solid/gas reaction, reactor comprising means of cooling
US5507158A (en) * 1992-07-22 1996-04-16 Elf Aquitaine Device for indirect production of cold for refrigerating machine
US5715701A (en) * 1996-10-01 1998-02-10 Fmc Corporation Double blower air conditioning unit
US5966955A (en) * 1996-01-16 1999-10-19 Ebara Corporation Heat pump device and desiccant assisted air conditioning system
US20080245086A1 (en) * 2007-03-02 2008-10-09 Polar King International, Inc. Multi-zone low temperature freezer

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH01305273A (ja) * 1988-06-03 1989-12-08 Seijiro Suda 金属水素化物ヒートポンプ
DE4410545A1 (de) * 1994-03-26 1995-09-28 Linde Ag Verfahren zum Betrieb einer Adsorptionskälteanlage

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2456386A (en) * 1946-05-07 1948-12-14 Howell C Cooper Cascade refrigeration unit with controls therefor
US3585810A (en) * 1968-07-15 1971-06-22 G U E Zimmermann Intermittent absorption refrigerating machine
US4135371A (en) * 1976-05-18 1979-01-23 Fritz Kesselring Storage element for a sorption heat storage system
US5174367A (en) * 1989-03-13 1992-12-29 Sanyo Electric Co., Ltd. Thermal utilization system using hydrogen absorbing alloys
US5335519A (en) * 1991-07-26 1994-08-09 Societe Nationale Elf Aquitaine Plant for producing cold by solid/gas reaction, reactor comprising means of cooling
US5507158A (en) * 1992-07-22 1996-04-16 Elf Aquitaine Device for indirect production of cold for refrigerating machine
US5966955A (en) * 1996-01-16 1999-10-19 Ebara Corporation Heat pump device and desiccant assisted air conditioning system
US5715701A (en) * 1996-10-01 1998-02-10 Fmc Corporation Double blower air conditioning unit
US20080245086A1 (en) * 2007-03-02 2008-10-09 Polar King International, Inc. Multi-zone low temperature freezer

Also Published As

Publication number Publication date
FR2879727B1 (fr) 2012-12-14
EP1831616A2 (fr) 2007-09-12
JP2008524544A (ja) 2008-07-10
FR2879727A1 (fr) 2006-06-23
WO2006067302A2 (fr) 2006-06-29
JP5101297B2 (ja) 2012-12-19
EP1831616B1 (fr) 2017-08-16
WO2006067302A3 (fr) 2006-08-31
ES2648389T3 (es) 2018-01-02
WO2006067302A8 (fr) 2008-02-21

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