EP1078208B1 - Procede et dispositif pour produire du froid - Google Patents

Procede et dispositif pour produire du froid Download PDF

Info

Publication number
EP1078208B1
EP1078208B1 EP99924849A EP99924849A EP1078208B1 EP 1078208 B1 EP1078208 B1 EP 1078208B1 EP 99924849 A EP99924849 A EP 99924849A EP 99924849 A EP99924849 A EP 99924849A EP 1078208 B1 EP1078208 B1 EP 1078208B1
Authority
EP
European Patent Office
Prior art keywords
refrigerant
oil
heat exchanger
joule
cooled
Prior art date
Legal status (The legal status 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 status listed.)
Expired - Lifetime
Application number
EP99924849A
Other languages
German (de)
English (en)
Other versions
EP1078208A1 (fr
Inventor
Alexander Alexeev
Hans Quack
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Messer Griesheim GmbH
Original Assignee
Messer Griesheim GmbH
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 DE1998120961 external-priority patent/DE19820961A1/de
Priority claimed from DE19821308A external-priority patent/DE19821308A1/de
Application filed by Messer Griesheim GmbH filed Critical Messer Griesheim GmbH
Publication of EP1078208A1 publication Critical patent/EP1078208A1/fr
Application granted granted Critical
Publication of EP1078208B1 publication Critical patent/EP1078208B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • F25B40/00—Subcoolers, desuperheaters or superheaters
    • F25B40/02—Subcoolers
    • 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
    • F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
    • F25B43/02—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat for separating lubricants from the refrigerant
    • 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
    • F25B7/00—Compression machines, plants or systems, with cascade operation, i.e. with two or more circuits, the heat from the condenser of one circuit being absorbed by the evaporator of the next circuit
    • 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
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/02—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point using Joule-Thompson effect; using vortex effect
    • 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
    • F25B31/00—Compressor arrangements
    • F25B31/002—Lubrication
    • F25B31/004—Lubrication oil recirculating arrangements
    • 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
    • F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
    • F25B43/003—Filters
    • 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
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component

Definitions

  • the invention relates to a method for cooling in the temperature range of 65 up to 150 K, where the refrigerant compresses with an oil-lubricated compressor is then cooled to ambient temperature and then oil is separated from the refrigerant before the refrigerant is a Joule-Thomson heat exchanger is fed.
  • the invention further relates to a device for Refrigeration in the temperature range from 65 to 150 K, some. oil-lubricated Compressor for compressing a refrigerant, a downstream after cooler to cool the fuel to ambient temperature, one on it subsequent device for separating oil from the refrigerant and one of the Device for separating the oil downstream Joule-Thomson countercurrent heat exchanger having.
  • refrigerants 320 K Mixtures of gases with normal boiling temperatures are often used as refrigerants 320 K used. These include, for example, hydrogen, nitrogen, oxygen, Noble gases, hydrocarbons and halogenated hydrocarbons. The one before described methods are when using such mixtures as Refrigerant referred to as the "mixture-Joule-Thomson method".
  • an oil-lubricated compressor has the disadvantage that oil can get from the compressor into the refrigerant and can thus be carried into the refrigeration cycle. If the oil gets into the cold part of the refrigeration system, it freezes out at the low temperatures that occur in the evaporator and clogs the evaporator. Corresponding components must therefore be connected downstream of the compressor in order to separate oil from the refrigerant after it has been compressed. Due to the relatively high temperatures of the compressed refrigerant, both aerosols and vaporous oil components are usually present in the refrigerant. A liquid oil separator with oil return to the compressor and a downstream adsorber can advantageously be used as the cleaning unit to remove vaporous oil components and the finest droplets still remaining. This arrangement has been described (RC Longworth, MJ Boiarski, LA Klusmier, 80 K Closed Cycle Throttle Refrigerator, Proceedings of the 8th International Conference cryocooler, Vail Co., June 1994).
  • An adsorber is a container filled with an adsorbent.
  • an adsorbent serve solid substances, due to their properties other substances, in this case the oil, can bind.
  • the adsorption process constitutes an attachment of molecules from the gaseous or liquid phase to the solid surface of the Adsorbent.
  • Activated carbon and silica gel are the main adsorbents and zeolites (molecular sieves) are used.
  • zeolites molecular sieves
  • an adsorber is discontinuous.
  • the adsorber is loaded, if the whole inner surface of the adsorbent from the foreign Molecules is occupied. Then the adsorber can no longer fulfill its function. Therefore, the adsorber is replaced at regular intervals or regenerated.
  • the period between the exchange or regeneration of the Adsorbers adversely determines the maintenance-free period of the entire Käitemaschine.
  • a normal maintenance period is in the range of 5000 to 10000 operating hours.
  • Another disadvantage of the adsorber is the selectivity of the adsorbent in Relation to certain components of a refrigerant mixture, i.e. its Ability to adsorb different components differently (H. Jungnickel, R. Agsten, W.-E. Kraus, basics of refrigeration technology, Verlagtechnik GmbH, 1990, p. 309). As it flows through the adsorber, it shifts Composition of the mixture for this reason usually in favor of low-boiling components.
  • thermodynamic effectiveness of the circuit of the refrigerant mixture important to use certain compositions of the refrigerant mixture.
  • the main criterion for choosing the composition is the size and distribution of the Temperature difference between high and low pressure flow in the Joule-Thomson heat exchanger.
  • the temperature difference should be as small as possible and the distribution the temperature difference in the heat exchanger should be as uniform as possible.
  • Refrigerant mixtures that offer a particularly favorable temperature difference distribution in the heat exchanger are usually not gaseous before entering the Joule-Thomson heat exchanger, but are partially liquefied. This is achieved by adding higher boiling components such as propane or isobutane (A. Alexeev, H. Quack, Ch. Haberstroh, Low cost mixture Joule Thomson Refrigerator, Cryogenics, Proceedings of the 16 th International Cryogenic Engineering Conference, Kitakyushu , Japan, 1996).
  • propane or isobutane A. Alexeev, H. Quack, Ch. Haberstroh, Low cost mixture Joule Thomson Refrigerator, Cryogenics, Proceedings of the 16 th International Cryogenic Engineering Conference, Kitakyushu , Japan, 1996.
  • the higher-boiling mixture components usually also have a higher one Freezing temperature. At low temperatures in the cold part, these components can freeze out and clog the vaporizer. For this reason, the proportion of higher-boiling components in the refrigerant mixture should be as low as possible.
  • the Advantages of using refrigerant mixtures are not fully exploited potential effectiveness is not achieved. That is another disadvantage of Mixture-Joule-Thomson method known in the prior art.
  • the object of the invention is the effectiveness of the mixture Joule-Thomson process with oil-lubricated compressors.
  • the efficiency the method and the device for refrigeration should be increased and the maintenance-free time of an optionally arranged adsorber and thus the Refrigeration device should be extended.
  • the object is achieved in that the refrigerant after it Cooling down to ambient temperature and before entering the Joule-Thomson heat exchanger is additionally cooled.
  • the device for the additional cooling is called an oil condenser here. Because surprisingly, the relatively small additional condense Cooling to a considerable extent advantageous further oil shares from the Refrigerant flow.
  • the method is particularly advantageous for cooling in the temperature range suitable from 90 to 110 K.
  • the refrigerant after it has cooled is cooled to ambient temperature and before oil separation.
  • the refrigerant after Separation of the oil and before entering the Joule-Thomson heat exchanger is additionally cooled.
  • the refrigerant flow advantageously cooled in a further heat exchanger (precooler), so that the Refrigerant is partially liquefied in the Joule-Thomson heat exchanger.
  • precooler a further heat exchanger
  • the Heat exchanger for cooling the high pressure flow under the Ambient temperature that means oil condenser and precooler, relate to them Cooling capacity advantageous from a refrigeration system.
  • the additional cooling in the oil condenser can advantageously only be carried out with a liquid oil separator as Separation stage for the oil a technically meaningful purity of the refrigerant can be achieved.
  • the refrigerant has before entering the Joule-Thomson heat exchanger a temperature of 233 to 243 K.
  • the pressure of the refrigerant before entering the oil-lubricated compressor 1 to 3 bar preferably 1.5 to 2.5 bar and particularly preferably 1.6 to 1.8 bar
  • the refrigerant after it Compression in the oil-lubricated compressor a pressure of 10 to 28 bar, preferably 12 to 18 bar and particularly preferably 14 to 16 bar
  • the predominantly separate vaporous oil from the refrigerant after the predominant separation liquid oil from the refrigerant then the predominantly separate vaporous oil from the refrigerant.
  • the separation takes place advantageous with a liquid oil separator and downstream adsorber, wherein in the liquid oil separator contained in the refrigerant flow Oil droplets are separated and the remaining refrigerant flow with now small amounts of vaporous oil are further cleaned in an adsorber.
  • the oil vapors from the refrigerant gas condense relatively well after compression and are separated relatively well in the liquid oil separator.
  • the Concentration of the residual oil in the gaseous refrigerant after Liquid oil separator is relatively small, which significantly relieves the pressure on the adsorber becomes.
  • the proportion can be advantageous when using refrigerant mixtures of higher-boiling components can be reduced. Because even before entering The Joule-Thomson heat exchanger uses such refrigerant mixtures partially liquefied. This increases and increases the effectiveness of the system the risk of these components freezing out at low temperatures in the cold part the system significantly reduced.
  • a mixture is used as the refrigerant which contains nitrogen, methane, propane and ethane or ethylene
  • the mixture preferably contains 25 to 45 mol% nitrogen, 15 to 42 mol% Methane, 5 to 15 mol% propane, balance ethane or ethylene.
  • the advantage is that the refrigerant mixture consists of relatively few components. components with normal boiling point at ambient temperature, for example isobutane not necessary anymore. The development of refrigerant mixtures and maintenance of the Refrigerant mixture is thus significantly simplified.
  • the object is also achieved by a device for refrigeration, in which between the aftercooler and the Joule-Thomson countercurrent heat exchanger an oil condenser is arranged.
  • the oil condenser is after the after cooler and before one Device for oil separation arranged.
  • According to the invention is an adsorber after the device for oil separation and before the Joule-Thomson countercurrent heat exchanger.
  • the invention is after the aftercooler and after the device for Oil separation arranged a precooler.
  • the oil condenser and / or the precooler are integrated as evaporators in a separate refrigeration cycle.
  • the device for oil separation or a heat exchanger is arranged after the adsorber and before the precooler is.
  • the precooler acts as a three-flow heat exchanger is designed, through which the refrigerant flow from the Joule-Thomson heat exchanger and the flow of the cooling medium from the separate Refrigeration circuit in counterflow to the refrigerant flow from the device for Oil separation or the adsorber is performed.
  • Fig. 1 is a device for performing a mixture throttle process shown. This process can be seen as a modified Joule-Thomson process become.
  • the device consists of an oil-lubricated compressor 1, a Aftercooler 2, a Joule-Thomson heat exchanger 3, a throttle element 4, an evaporator 5, a liquid oil separator 6, a capillary line 8, an oil condenser 9, a precooler 10, a heat exchanger 17 and one Refrigeration system 11.
  • the mixture compressed in the compressor 1 is in the aftercooler 2 to Ambient temperature cooled.
  • the refrigerant is then in the Oil condenser 9 pre-cooled to below ambient temperature, the mixture remains gaseous.
  • the subsequent separation of the oil from the refrigerant mixture takes place in two stages. First, oil droplets and oil aerosol are in the Liquid oil separator 6 separated.
  • the separated oil in the Liquid oil separator 6 is returned to the compressor 1 through a capillary line 8 fed and the oil circuit closed.
  • the high pressure flow after the Liquid oil separator 6 then flows through the heat exchanger 17.
  • Vom Heat exchanger 17 preferably as a countercurrent heat exchanger is formed, the high pressure flow is the precooler 10 and then the Joule-Thomson heat exchanger 3 supplied.
  • the refrigerant mixture is through cooled the precooler 10 so that the refrigerant mixture is partially liquefied.
  • the high pressure flow is countercurrent in the Joule-Thomson heat exchanger 3 cooled to low pressure flow and finally in the throttle body 4 ins Relaxed two-phase area.
  • the refrigerant mixture in the Evaporator 5 partially evaporated with absorption of cooling power. That from the Evaporator 5 coming refrigerant mixture is in the Joule-Thomson countercurrent heat exchanger 3 warmed up.
  • This low pressure flow is over the Heat exchanger 17 fed to the compressor 1 again.
  • the cold for that Oil condenser 9 and the precooler 10 is replaced by at least one additional one Refrigeration system 11 provided.
  • the refrigeration system 11 preferably consists of a compressor 12, a Capacitor 13 and the throttle bodies 14 and 15.
  • a further throttle element 16 is arranged in the line after the oil condenser 9 his.
  • FIG. 2 shows a further development of the device for implementation shown in FIG. 1 of a mixture-throttle process.
  • the precooler 10 after the Liquid oil separation in the liquid oil separator 6 is here as a three-flow heat exchanger designed by which the low pressure flow from the Joule-Thomson heat exchanger 3 and the pre-cooling medium from the refrigeration system 11 in Counter current flow to the high pressure flow and thereby the heat exchanger 17 here eliminated.
  • the cycle is particularly efficient.
  • the cold for the precooler 10 and Oil condenser 9 is generated in at least one refrigerator 11.
  • the device according to FIG. 3 essentially corresponds to that shown in FIG. 1
  • the device and the device according to FIG. 4 essentially agree with that in FIG. 2 shown device match, with an additional adsorber 7 between the Liquid oil separator 6 and the heat exchanger 17 or the three-flow heat exchanger is arranged as a precooler 10. With these devices the vaporous oil components in the adsorber 7 additionally from the refrigerant adsorbed.
  • FIG. 5 An advantageous variant of the device is shown in FIG. 5. there the refrigerant after the aftercooler 2 is only cooled in the oil condenser 9 and the Oil separation in the liquid oil separator 6 is facilitated. After Oil separation, the oil vapors are adsorbed in an adsorber 7. The cleaned Refrigerant enters the Joule-Thomson heat exchanger 3 and is then according to a Joule-Thomson process according to the prior art treated. The cold for the oil condenser 9 is from a refrigerator 11 generated.
  • the device shown in FIG. 6 has only one liquid oil separator 6 Separation of the oil from the refrigerant mixture. With this device no adsorber 7 required. The cold for the oil condenser 9 is in one Chiller 11 generated.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Power Engineering (AREA)
  • Lubricants (AREA)
  • Compressor (AREA)
  • Devices That Are Associated With Refrigeration Equipment (AREA)

Claims (16)

  1. Procédé de production de froid dans le domaine de température de 65 à 150 K, lors duquel l'agent réfrigérant est comprimé dans un compresseur lubrifié à l'huile (1), est ensuite refroidi à la température ambiante et lors duquel l'huile est ensuite séparée de l'agent réfrigérant, avant de conduire l'agent réfrigérant à un dispositif de transfert de chaleur Joule-Thomson (3), caractérisé en ce que l'agent réfrigérant subit un refroidissement supplémentaire, après son refroidissement à la température ambiante et avant l'entrée dans le dispositif de transfert de chaleur Joule-Thomson (3).
  2. Procédé selon la revendication 1, caractérisé en ce que l'agent réfrigérant subit un refroidissement supplémentaire, après son refroidissement à la température ambiante et avant la séparation de l'huile.
  3. Procédé selon la revendication 1, caractérisé en ce que l'agent réfrigérant subit un refroidissement supplémentaire, après la séparation de l'huile et avant l'entrée dans le dispositif de transfert de chaleur Joule-Thomson (3).
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que l'agent réfrigérant présente, avant l'entrée dans le dispositif de transfert de chaleur Joule-Thomson (3), une température de 233 à 243 K.
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que la pression de l'agent réfrigérant, avant l'entrée dans le compresseur lubrifié à l'huile (1), est de 1 à 3 bars, de préférence de 1,5 à 2,5 bars et en particulier de préférence de 1,6 à 1,8 bars et en ce que l'agent réfrigérant, après sa compression dans le compresseur lubrifié à l'huile (1), présente une pression de 10 à 28 bars, de préférence de 12 à 18 bars et en particulier de préférence de 14 à 16 bars.
  6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que l'on sépare de l'agent réfrigérant, après le refroidissement de l'agent réfrigérant à la température ambiante, des portions d'huile essentiellement liquides.
  7. Procédé selon la revendication 6, caractérisé en ce que l'on sépare de l'agent réfrigérant, après la séparation de la portion d'huile essentiellement liquide de l'agent réfrigérant, la portion d'huile qui se présente essentiellement sous forme de vapeur.
  8. Procédé selon l'une quelconque des revendications 1 à 7, caractérisé en ce que l'on utilise, en tant qu'agent réfrigérant, un mélange contenant de l'azote, du méthane, du propane et de l'éthane ou de l'éthylène.
  9. Procédé selon la revendication 8, caractérisé en ce que le mélange contient de 25 à 45 % en moles d'azote, de 15 à 42 % en moles de méthane, de 5 à 25 % en moles de propane, le reste étant de l'éthane ou de l'éthylène.
  10. Dispositif de production de froid dans le domaine de température de 65 à 150 K, qui présente un compresseur lubrifié à l'huile (1) en vue de la compression d'un agent réfrigérant, un réfrigérant complémentaire (2), placé à la suite en vue du refroidissement de l'agent réfrigérant à la température ambiante, un dispositif subséquent en ce point en vue de la séparation de l'huile de l'agent réfrigérant et un dispositif de transfert de chaleur Joule-Thomson à contre-courant (3), placé à la suite du dispositif en vue de la séparation de l'huile, caractérisé en ce que l'on dispose, entre le réfrigérant complémentaire (2) et le dispositif de transfert de chaleur Joule-Thomson à contre-courant (3), un condenseur d'huile (9).
  11. Dispositif selon la revendication 10, caractérisé en ce que l'on dispose le condenseur d'huile (9) après le réfrigérant complémentaire (2) et avant un dispositif en vue du dépôt de l'huile (6).
  12. Dispositif selon la revendication 11, caractérisé en ce que l'on dispose un dispositif d'adsorption (7) après le dispositif en vue du dépôt de l'huile (6) et avant le dispositif de transfert de chaleur Joule-Thomson à contre-courant (3).
  13. Dispositif selon l'une quelconque des revendications 10 à 12, caractérisé en ce que l'on dispose, après le réfrigérant complémentaire (2) et après le dispositif en vue du dépôt de l'huile (6), un réfrigérant antérieur (10).
  14. Dispositif selon la revendication 13, caractérisé en ce que le condenseur d'huile (9) et/ou le réfrigérant antérieur (10) sont reliés en tant qu'évaporateur dans un circuit de circulation de froid séparé (11).
  15. Dispositif selon la revendication 13 ou 14, caractérisé en ce que l'on dispose un dispositif de transfert de chaleur (17) après le dispositif en vue du dépôt de l'huile (6) ou après le dispositif d'adsorption (7) et avant le réfrigérant antérieur (10).
  16. Dispositif selon la revendication 15, caractérisé en ce que le réfrigérant antérieur (10) est conçu en tant que dispositif de transfert de chaleur à trois courants, à travers lequel le courant d'agent réfrigérant en provenance du dispositif de transfert de chaleur Joule-Thomson (3) et le courant du milieu réfrigérant provenant du circuit de circulation de froid séparé (11) sont conduits à contre-courant par rapport au courant d'agent réfrigérant provenant du dispositif en vue du dépôt de l'huile (6) ou du dispositif d'adsorption (7).
EP99924849A 1998-05-12 1999-04-30 Procede et dispositif pour produire du froid Expired - Lifetime EP1078208B1 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE1998120961 DE19820961A1 (de) 1998-05-12 1998-05-12 Verfahren und Vorrichtung zur Kälteerzeugung
DE19820961 1998-05-12
DE19821308A DE19821308A1 (de) 1998-05-13 1998-05-13 Verfahren und Vorrichtung zur Kälteerzeugung
DE19821308 1998-05-13
PCT/EP1999/002932 WO1999058905A1 (fr) 1998-05-12 1999-04-30 Procede et dispositif pour produire du froid

Publications (2)

Publication Number Publication Date
EP1078208A1 EP1078208A1 (fr) 2001-02-28
EP1078208B1 true EP1078208B1 (fr) 2002-04-17

Family

ID=26046099

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99924849A Expired - Lifetime EP1078208B1 (fr) 1998-05-12 1999-04-30 Procede et dispositif pour produire du froid

Country Status (7)

Country Link
US (1) US6463744B1 (fr)
EP (1) EP1078208B1 (fr)
JP (1) JP2002514734A (fr)
AT (1) ATE216481T1 (fr)
DE (1) DE59901262D1 (fr)
PE (1) PE20000391A1 (fr)
WO (1) WO1999058905A1 (fr)

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2351976B1 (fr) * 2000-05-30 2015-09-09 Brooks Automation, Inc. Système de réfrigération basse température
US6923009B2 (en) * 2003-07-03 2005-08-02 Ge Medical Systems Global Technology, Llc Pre-cooler for reducing cryogen consumption
WO2005005569A1 (fr) * 2003-07-15 2005-01-20 Indian Institute Of Technology Composition refrigerante pour systemes de refrigeration
US7603871B2 (en) * 2006-06-29 2009-10-20 Test Enterprises, Inc. High-flow cold air chiller
DE102008052494A1 (de) * 2008-09-30 2010-04-08 Institut für Luft- und Kältetechnik gGmbH Joule-Thomson-Kühler
DE102009039814A1 (de) * 2009-09-02 2011-03-10 Airbus Operations Gmbh System und Verfahren zum Kühlen mindestens einer Wärme erzeugenden Einrichtung in einem Flugzeug
CN101893354B (zh) * 2010-07-01 2012-10-17 大连三洋压缩机有限公司 一种过冷油冷器和新型经济器螺杆机制冷循环系统
JP5656691B2 (ja) * 2011-03-04 2015-01-21 三菱電機株式会社 冷凍装置
WO2013016224A1 (fr) * 2011-07-22 2013-01-31 Lockheed Martin Corporation Idca pour refroidissement rapide et temps de fonctionnement prolongé
JP5575191B2 (ja) * 2012-08-06 2014-08-20 三菱電機株式会社 二元冷凍装置
US9999885B1 (en) 2014-05-30 2018-06-19 Lockheed Martin Corporation Integrated functional and fluidic circuits in Joule-Thompson microcoolers
EP3162870A1 (fr) 2015-10-27 2017-05-03 Linde Aktiengesellschaft Réfrigérant mélangé basse température pour pré-refroidissement d'hydrogène à grande échelle
FR3133075B1 (fr) * 2022-02-25 2024-02-23 Absolut System Système de refroidissement cryogénique

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0136342A4 (fr) * 1983-02-14 1985-07-01 Gen Pneumatics Corp Appareil de refroidissement cryogenique a cycle ferme.
US4831828A (en) * 1987-05-27 1989-05-23 Helix Technology Corporation Cryogenic refrigerator having a convection system to cool a hermetic compressor
JPH0760027B2 (ja) * 1988-03-25 1995-06-28 三洋電機株式会社 冷凍装置
US5337572A (en) * 1993-05-04 1994-08-16 Apd Cryogenics, Inc. Cryogenic refrigerator with single stage compressor
US5441658A (en) * 1993-11-09 1995-08-15 Apd Cryogenics, Inc. Cryogenic mixed gas refrigerant for operation within temperature ranges of 80°K- 100°K
US5617739A (en) * 1995-03-29 1997-04-08 Mmr Technologies, Inc. Self-cleaning low-temperature refrigeration system
US5595065A (en) * 1995-07-07 1997-01-21 Apd Cryogenics Closed cycle cryogenic refrigeration system with automatic variable flow area throttling device
DE19648902C2 (de) * 1996-11-26 1998-09-10 Univ Dresden Tech Verfahren zur Realisierung eines Gemisch- Joule- Thomson-Prozesses und Vorrichtung zur Durchführung dieses Verfahrens
DE19747985A1 (de) * 1997-10-30 1999-05-27 Univ Dresden Tech Verfahren zur Realisierung eines Gemisch-Joule-Thomson-Prozesses und Vorrichtung zur Durchführung des Verfahrens

Also Published As

Publication number Publication date
JP2002514734A (ja) 2002-05-21
WO1999058905A1 (fr) 1999-11-18
DE59901262D1 (de) 2002-05-23
ATE216481T1 (de) 2002-05-15
US6463744B1 (en) 2002-10-15
EP1078208A1 (fr) 2001-02-28
PE20000391A1 (es) 2000-05-24

Similar Documents

Publication Publication Date Title
EP1078208B1 (fr) Procede et dispositif pour produire du froid
DE69629461T2 (de) Selbstreinigendes tieftemperaturkühlsystem
DE60016690T2 (de) Gasverflüssigung mit Hilfe eines einzigen Kühlmittelgemischkreislaufs
DE2820212A1 (de) Verfahren zum verfluessigen von erdgas
DE2614132B2 (de) Tieftemperaturkälteverfahren
DE10055321A1 (de) Verfahren zum Verflüssigen eines Gases
WO2008022689A2 (fr) Procédé permettant la liquéfaction d'un flux riche en hydrocarbures
DE2207509A1 (de) Verfahren und Vorrichtung zur Neon und Helium Erzeugung aus Luft
DE3528374A1 (de) Verfahren und vorrichtung zur erzeugung von stickstoff mit ueberatmosphaerischem druck
DE2207508A1 (de) Verfahren und Vorrichtung zur Trennung von Neon Helium Gemisch mittels Expansions turbinen
DE19821308A1 (de) Verfahren und Vorrichtung zur Kälteerzeugung
DE19648902C2 (de) Verfahren zur Realisierung eines Gemisch- Joule- Thomson-Prozesses und Vorrichtung zur Durchführung dieses Verfahrens
EP1084207B1 (fr) Procede de production de froid dans la plage de temperature de 90 a 110 k.
WO2015154786A2 (fr) Installation destinée à réduire la teneur en dioxyde de carbone d'un flux gazeux contenant du dioxyde carbone et riche en hydrocarbures et procédé correspondant
DE4017611A1 (de) Verfahren zur verfluessigung von gasen
DE102013012656A1 (de) Verfahren zum Abtrennen unerwünschter Komponenten aus einem Helium-Strom
DE19820961A1 (de) Verfahren und Vorrichtung zur Kälteerzeugung
DE19820960A1 (de) Kältemittelgemisch für einen Gemisch-Drossel-Prozeß
DE19747985A1 (de) Verfahren zur Realisierung eines Gemisch-Joule-Thomson-Prozesses und Vorrichtung zur Durchführung des Verfahrens
DE19821272A1 (de) Kältemittelgemisch für einen Gemisch-Drossel-Prozeß
DE19748966B4 (de) Vorrichtung und Verfahren zur Herstellung und Lagerung von flüssiger Luft
EP0537616B1 (fr) Procédé pour séparer des hydrocarbures fluorés-chlorés de mélanges gazeux
EP1140323B1 (fr) Procede de separation d'hydrocarbures dans un courant gazeux au moyen d'un dispositif de separation a membrane
DE19922364B4 (de) Vorrichtung und Verfahren zur Kryolagerung biologischer Stoffe
DE102014008770B4 (de) Xenon-Gewinnung aus methanhaltigen Gasen

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20001212

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

17Q First examination report despatched

Effective date: 20010814

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 20020417

Ref country code: IE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020417

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020417

Ref country code: GB

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020417

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020417

REF Corresponds to:

Ref document number: 216481

Country of ref document: AT

Date of ref document: 20020515

Kind code of ref document: T

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20020430

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20020430

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020430

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: GERMAN

REF Corresponds to:

Ref document number: 59901262

Country of ref document: DE

Date of ref document: 20020523

REG Reference to a national code

Ref country code: CH

Ref legal event code: NV

Representative=s name: SCHMAUDER & PARTNER AG PATENTANWALTSBUERO

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020717

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020717

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020717

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020728

RAP2 Party data changed (patent owner data changed or rights of a patent transferred)

Owner name: MESSER GRIESHEIM GMBH

ET Fr: translation filed
GBV Gb: ep patent (uk) treated as always having been void in accordance with gb section 77(7)/1977 [no translation filed]

Effective date: 20020417

REG Reference to a national code

Ref country code: CH

Ref legal event code: PFA

Free format text: MESSER GRIESHEIM GMBH,FRANKFURT AIRPORT CENTER 1, C9, HUGO-ECKENER-RING,60547 FRANKFURT (DE) -DANN IN- MESSER GRIESHEIM GMBH,FRITZ-KLATTE-STRASSE 6,65933 FRANKFURT AM MAIN (DE)

NLT2 Nl: modifications (of names), taken from the european patent patent bulletin

Owner name: MESSER GRIESHEIM GMBH

REG Reference to a national code

Ref country code: IE

Ref legal event code: FD4D

Ref document number: 1078208E

Country of ref document: IE

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed

Effective date: 20030120

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 20060331

Year of fee payment: 8

BERE Be: lapsed

Owner name: *MESSER GRIESHEIM G.M.B.H.

Effective date: 20070430

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20070430

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: AT

Payment date: 20080311

Year of fee payment: 10

REG Reference to a national code

Ref country code: CH

Ref legal event code: PCAR

Free format text: SCHMAUDER & PARTNER AG PATENT- UND MARKENANWAELTE VSP;ZWAENGIWEG 7;8038 ZUERICH (CH)

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20090430

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20120425

Year of fee payment: 14

Ref country code: CH

Payment date: 20120420

Year of fee payment: 14

Ref country code: DE

Payment date: 20120420

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20120507

Year of fee payment: 14

REG Reference to a national code

Ref country code: NL

Ref legal event code: V1

Effective date: 20131101

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20130430

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20131101

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20130430

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20131231

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20130430

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20131101

REG Reference to a national code

Ref country code: DE

Ref legal event code: R119

Ref document number: 59901262

Country of ref document: DE

Effective date: 20131101