EP2082175A2 - Machine frigorifique à absorption - Google Patents

Machine frigorifique à absorption

Info

Publication number
EP2082175A2
EP2082175A2 EP07815139A EP07815139A EP2082175A2 EP 2082175 A2 EP2082175 A2 EP 2082175A2 EP 07815139 A EP07815139 A EP 07815139A EP 07815139 A EP07815139 A EP 07815139A EP 2082175 A2 EP2082175 A2 EP 2082175A2
Authority
EP
European Patent Office
Prior art keywords
pump
absorber
pressure
solution
generator
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.)
Withdrawn
Application number
EP07815139A
Other languages
German (de)
English (en)
Inventor
Gerhard Kunze
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.)
Econicsystems Innovative Kuehllosungen Gesmbh
Inner Circle Un Ltd
Original Assignee
Econicsystems Innovative Kuehllosungen Gesmbh
Inner Circle Un Ltd
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
Application filed by Econicsystems Innovative Kuehllosungen Gesmbh, Inner Circle Un Ltd filed Critical Econicsystems Innovative Kuehllosungen Gesmbh
Publication of EP2082175A2 publication Critical patent/EP2082175A2/fr
Withdrawn legal-status Critical Current

Links

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
    • 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
    • F25B15/025—Liquid transfer means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04B—POSITIVE-DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS
    • F04B19/00—Machines or pumps having pertinent characteristics not provided for in, or of interest apart from, groups F04B1/00 - F04B17/00
    • F04B19/20—Other positive-displacement pumps
    • F04B19/24—Pumping by heat expansion of pumped fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04F—PUMPING OF FLUID BY DIRECT CONTACT OF ANOTHER FLUID OR BY USING INERTIA OF FLUID TO BE PUMPED; SIPHONS
    • F04F1/00—Pumps using positively or negatively pressurised fluid medium acting directly on the liquid to be pumped
    • F04F1/06—Pumps using positively or negatively pressurised fluid medium acting directly on the liquid to be pumped the fluid medium acting on the surface of the liquid to be pumped
    • 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
    • F25B15/04—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas the refrigerant being ammonia evaporated from aqueous solution
    • 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

  • the invention relates to an absorption refrigeration machine according to the preamble of claim 1.
  • absorption chillers For solar chillers are adsorption and absorption chillers. At present, it is preferred to use the former, although absorption chillers, especially those operated with the refrigerant ammonia and the absorbent water, have significant advantages: much lower cooling temperatures can be achieved, and with a suitable design, the heat number could be much better than that of adsorption chillers. However, there are a number of obstacles in the current state of the art.
  • the classic absorption chiller is based on the principle that a refrigerant in a liquid absorbent at low temperature and low pressure dissolves very well, which takes place in an absorber heat exchanger as an exothermic process, in contrast, in a so-called generator heat exchanger at high temperature even at much higher pressure in Vapor form, which is an endothermic process. If now this refrigerant vapor at high pressure in a condenser heat exchanger heat withdrawn at the so-called recooling temperature which is usually close to the ambient temperature, the refrigerant liquefies. If the pressure is then lowered, the refrigerant in the evaporator can evaporate again at a lower temperature. This endothermic process is the actual cooling process.
  • the absorbent is also cooled to the recooling temperature. Subsequently, the gaseous refrigerant coming from the evaporator and the recooled absorbent are brought together again at low pressure in an absorber heat exchanger.
  • High-refrigerant absorbents such as those derived from the absorber, are called strong solutions, low-refrigerant absorbents, as they come from the generator, are called weak solutions.
  • the object of the invention is to propose an absorption chiller of the type mentioned, which has a long life and low wear. Further task It is to propose an absorption chiller of the type mentioned, which has no or only slight variations in the cooling temperature.
  • the first object is achieved in an absorption refrigeration machine of the type mentioned by the features of claim 1.
  • Pressure barrier of 5-15 bar can be dispensed with.
  • Solution transport may be associated with thermal solar energy
  • the concentration of the solution can be adapted to the respective heating temperature and thus an optimal operation can be achieved. Due to the features of claim 9 results in a very simple construction for a
  • Chiller which differ essentially by the structure of the steam pump.
  • the refrigerating machine comprises a steam pump 100, which has a pump inlet vessel 26, a pressure booster 27 arranged below its level, a pressure reducer 30 arranged below its level, and a pump outlet vessel 46 arranged below its level, it being provided according to the preferred embodiment Pumpenausgangsgefdata 46 with the pump inlet vessel 26 and the Druckabsenker 30, as well as with the generator 6 is in communication.
  • This steam pump 100 is connected via a pump outlet pipe 1, in which a shut-off, in particular a check valve 12 is connected to a pressure stabilizer 3, which is surrounded by a heating jacket 101, and a shut-off device 4, preferably a check valve, and a flow resistance, such as a Throttle 5, connected to a generator 6 for driving the refrigerant out of the solution.
  • the generator 6 is followed by a gas separator 7, the gas space is connected to a capacitor 8.
  • the condenser is acted upon by a recooling medium, which enters at the inlet 42 and exits at the exit 43.
  • the refrigerant condensate leaving the condenser is fed to a concentration regulator 9.
  • a concentration regulator 9 This is essentially formed by a tube which is substantially horizontally aligned and pivotable about a horizontal axis 102. As a result, the tube can be pivoted about the horizontal by a predeterminable angle, whereby more or less refrigerant condensate can be held in the tube.
  • the concentration regulator 9 is connected to a shut-off device, preferably a float valve 2, which in turn is connected to an evaporator 13, which is acted upon by a cooling medium, which enters via the input 44 and exits at the output 45 ,
  • the evaporator 13 is connected via a line 15, in which a shut-off device, e.g. a check valve 14 is arranged, connected to a warm absorber 17, whose cooling circuit 105 is flowed through by the cooled heating medium, which exits at the output 41.
  • a shut-off device e.g. a check valve 14
  • a warm absorber 17 whose cooling circuit 105 is flowed through by the cooled heating medium, which exits at the output 41.
  • the line 15 opens in front of the warm absorber 17, a line 16 which is connected to a connected to the liquid space of the gas separator 7 obturator, in particular a float valve 51, which only liquid, but not gas can pass.
  • the warm absorber 17 is connected to a cold absorber 19 via a U-shaped tube 18, the legs of which drop off downwards.
  • the cold absorber 19 is connected to a vacuum stabilizer 20, which, like the cold absorber 19, is acted upon by a recooling medium, which flows through a cooling circuit 104 in countercurrent.
  • the vapor pump 100 stands - seen in the direction of the circulation of the refrigerant solution, for example a water-ammonia solution - between the absorber and the generator, the pump on the input side with the absorber 17, 19, in particular with the warm Absorber 17 and / or the cold absorber 19, and the output side with the generator 6 in
  • the vacuum stabilizer 20 is connected to the steam pump 100 via a float valve 21 and a check valve 22.
  • the booster 27 is acted upon according to the preferred embodiment of the heating medium, which enters at the entrance 40 and exits at the exit 41.
  • the pressure reducer is acted upon according to the preferred embodiment of the heating medium, which enters at the entrance 40 and exits at the exit 41.
  • the cooling circuit of the evaporator 13 is traversed by the cooling medium and enters at 44 in this and leaves it at 45, wherein the heat exchanger of the evaporator, but preferably not necessarily, is operated in direct current, whereas the remaining
  • Heat exchangers are operated in countercurrent.
  • the cooling circuit of the vacuum stabilizer 20 and the cooling circuit of the cold absorber 19 are connected in series, wherein the recooling medium at the entrance 42 of the cooling jacket 103 of the
  • Vacuum stabilizer 20 enters and at the exit 43 of the cooling circuit 104 of the cold
  • Fluid lift tube 33 is connected, which in one with the liquid space of the
  • the strong refrigerant solution is pressed by the vapor pump, or by the pump outlet vessel 46 via the blocking means 12 in the pressure stabilizer 3. This serves to convert the pump strokes of the solution flow into a uniformly flowing flow with an optimum pressure for the generator process.
  • the pressure stabilizer 3 consists of a heated container of any shape, preferably a horizontal tube, which is surrounded by a flow-through by the heating medium jacket 101, wherein the tube is dimensioned so that always holds a gas bubble in its upper part. If cold solution is fed into the pressure stabilizer 3 by the pump 100, the pressure in the gas bubble of the pressure stabilizer 3 briefly drops, which allows unimpeded inflow of the solution.
  • the gas pressure in the pressure stabilizer 3 rises again to just above the generator pressure, since the solution is warmed up to the evaporation temperature.
  • the heating jacket 101 of the pressure stabilizer 3 is connected to the output of the generator heater 106.
  • the flow resistance 5, preferably a throttle and by the blocking means 4, preferably a check valve it is ensured that in the generator 6, a uniform solution flow occurs.
  • the solution flows in countercurrent to the heating medium flow input 40, heats up and forms gas bubbles.
  • the use of the pressure stabilizer 3 allows the use of a heat exchanger for the generator 6 with a narrow cross-section, but with a very large hydraulic length, ie a heat exchanger with high flow resistance, preferably a spiral heat exchanger, and because of the large flow rate is an extremely high heat transfer per unit area reached. This results in a particularly large temperature range of the heating medium on the way from the heating medium flow input 40 to the output of the generator 6. Since the heating medium during the passage through the heating jacket of the pressure stabilizer 3 further cools, its temperature is suitable to the warmer part of the absorption process cool.
  • the heating medium from the pressure stabilizer 3 is passed to the heat exchanger of the warm absorber 17, where it is reheated by the absorption process and finally out at 41 Bankmediumshne output back to the heater, not shown.
  • the hot weak solution passes together with the gas bubbles formed in the gas separator 7.
  • the blocking means 51 preferably a float valve
  • the hot solution then passes to the warm absorber 17th
  • Gas separator 7 passes the gas into the heat exchanger of the condenser 6, where heat is withdrawn by the recooling medium flowing in at 42 and 43, resulting in the condensation of the refrigerant. This now runs through the flexible inflow pipe 10 to the concentration regulator 9.
  • the concentration regulator 9 is rotatable about a rotatable suspension in the form of a horizontal axis 102 upwards or downwards and can be fixed in this position. Depending on the angle of inclination of the concentration regulator 9, a different amount of refrigerant then accumulates in the container 9 before it can continue to flow via the second flexible discharge pipe 11 via the float valve 2 to the evaporator 13. The amount of refrigerant accumulated in the concentration regulator 9 is withdrawn from the refrigeration cycle, so that the average concentration of the refrigerant solution in the entire machine is reduced. This adjustment is advantageous for solar cooling, since the optimum solution temperature is dependent on heating temperature, recooling temperature and desired cooling temperature, these three temperatures are climate-dependent.
  • the evaporation process of the refrigerant cools the cooling medium flow through 44 and 45.
  • the resulting refrigerant vapor passes through the supply line 15 to the warm absorber 17.
  • the supply line 15 unites with the supply line 16, which the Generator 6 incoming weak solution to the warm absorber 17 feeds.
  • the warm absorber 17 is cooled in countercurrent to the solution by the coming from the pressure stabilizer 3 cooled heating medium. The temperature of the heating medium rises, so that its temperature at the outlet of the warm absorber 17 reflects the amount of energy recovered from the absorption process.
  • the absorption process in the warm absorber 17 can not be completed, since in this a lower pressure than in the generator 6 prevails, thus the temperature for a complete absorption also must be lower than in the pressure stabilizer 3.
  • the mixture of solution and residual refrigerant vapor is therefore conducted via the connecting line 18 into the cold absorber 19.
  • the absorption process is completed and the resulting strong refrigerant solution is fed into the vacuum stabilizer 20.
  • This is similar in construction to the pressure stabilizer 3, but its outer jacket is cooled, so that in the inner tube Stored solution is always almost at the recooling temperature.
  • the recooling medium should first flow through the vacuum stabilizer 20 and then only the cold absorber 19, the latter in countercurrent to the mixture of solution and refrigerant vapor.
  • the vacuum stabilizer 20 also serves as a refrigerant solution reserve for the pump 100 so that it can work uniformly.
  • the strong solution enters the vapor pump, but only during the periods when the pressure in the vapor pump is low enough. If this is the case, then the main part of the solution flows through the first pump inlet pipe 38 and the controllable flow resistance 39 into the pump outlet vessel 46 and fills it. At the same time, however, also a smaller part of the solution flows through the second pump inlet pipe 23 into the pump inlet vessel 26.
  • 1st phase The pump inlet vessel 26 and the pump outlet vessel 46 fill.
  • 2nd phase As soon as the pump inlet vessel 26 has filled, the siphon tube 24 is filled up to its upper vertex. As solution flows over this apex, the siphon tube 24 draws solution from the pump inlet vessel 26 and allows it to flow into the lower portion of the pump, namely, the depressurizer 30 and the pressure riser 27. However, the solution can not flow immediately to the lowermost part of the pump via the fluid lift tube 33, which connects the suction tube 32 to the pump outlet vessel 46, since the static hydraulic pressure of the solution filled pump outlet vessel 46 prevents this.
  • the amount of solution per pump stroke must be dimensioned so that the pressure booster 27, preferably a horizontal tube, surrounded by a heating jacket, partially filled.
  • the pressure booster 27 preferably a horizontal tube, surrounded by a heating jacket, partially filled.
  • Druckabsenker 30, which is preferably formed by a horizontal tube, surrounded by a cooling jacket, while a gas bubble remains, due to the suction pipe 32, which opens from above into the pressure dropper 30.
  • FIG. 2 shows a refrigerating machine according to the invention with another vapor pump.
  • the filling of the pump takes place only via the pump inlet pipe 23 into the pump inlet vessel 26. Once the latter has been filled with solution, this flows through the siphon tube 24 to the pressure booster 27. Exactly on the level, however, where in the booster 27, the solution surface is located in the siphon tube 24 a branch to the overflow 107 out, which directs the excess solution through the pump inlet pipe 38 to the pump outlet vessel 46.
  • a vent 108 of the overflow 107 in order to prevent this cross-connection between the siphon tube 24 and the pump inlet tube 38 itself acts as a liquid lift.
  • the purpose of the overflow 107 is to convey a majority of the solution directly to the pump outlet vessel 46, which thus does not participate in the heating and cooling in the pressure booster 27 and the pressure drop 30, thereby saving energy.

Landscapes

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

Abstract

Machine frigorifique à absorption, notamment pour le fonctionnement en liaison avec une installation héliothermique, comprenant un générateur (6) pour expulser l'agent réfrigérant, notamment de l'ammoniaque, d'une solution et alimentée en agent caloporteur, un évaporateur (13) parcouru par un agent réfrigérant, un condensateur (8) pour la liquéfaction de l'agent réfrigérant évaporé et alimenté en agent de refroidissement de retour, un absorber (17, 19) et une pompe qui sont en liaison et permettent un circuit d'une solution d'agent réfrigérant, par exemple d'une solution eau-ammoniaque, la pompe étant raccordée côté entrée à l'absorbeur (17, 19) et côté sortie au générateur (6). La pompe est conçue comme pompe à vapeur (100) et la pompe à vapeur (100) présente un récipient d'entrée de pompe (26). Pour pouvoir fonctionner sans ou avec peu de variations de la température de refroidissement et présenter une durée de vie élevée, la pompe à vapeur (100) comprend un dispositif amplificateur de pression (27) placé sous le niveau du récipient d'entrée de pompe (26) et alimenté en agent caloporteur, un dispositif réducteur de pression (30) placé sous son niveau et alimenté en agent de refroidissement de retour et un récipient de sortie de pompe (46) placé sous son niveau.
EP07815139A 2006-10-19 2007-10-04 Machine frigorifique à absorption Withdrawn EP2082175A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT0174406A AT504399B1 (de) 2006-10-19 2006-10-19 Absorptionskältemaschine
PCT/AT2007/000472 WO2008046120A2 (fr) 2006-10-19 2007-10-04 Machine frigorifique à absorption

Publications (1)

Publication Number Publication Date
EP2082175A2 true EP2082175A2 (fr) 2009-07-29

Family

ID=39314378

Family Applications (1)

Application Number Title Priority Date Filing Date
EP07815139A Withdrawn EP2082175A2 (fr) 2006-10-19 2007-10-04 Machine frigorifique à absorption

Country Status (6)

Country Link
EP (1) EP2082175A2 (fr)
AT (1) AT504399B1 (fr)
AU (1) AU2007312922A1 (fr)
CA (1) CA2666172A1 (fr)
NO (1) NO20091911L (fr)
WO (1) WO2008046120A2 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NO20093003A1 (no) 2009-09-15 2011-03-16 Aquasolair As Vannutvinning
AT511228B1 (de) 2011-03-23 2013-01-15 Solarfrost Forschung Gmbh Solarkühlung mit einer ammoniak-wasser-absorptionskältemaschine
AT514997B1 (de) * 2013-10-21 2015-11-15 Gerhard Dr Kunze Modulare Absorptionskältemaschine in Plattenbauweise
CN117006728B (zh) * 2023-07-31 2026-02-03 大连海事大学 一种压力控制型溴化锂吸收式制冷气泡泵

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB382654A (en) * 1930-08-13 1932-10-31 Electrolux Ltd Improvements in or relating to absorption refrigerating apparatus
GB434978A (en) * 1933-07-17 1935-09-12 Hoover Ltd Improvements in or relating to continuous absorption refrigerating apparatus
US2454344A (en) * 1944-08-21 1948-11-23 Montcalm Inc Absorption refrigeration system
US2688923A (en) * 1951-11-05 1954-09-14 Filiberto A Bonaventura Solar energy pump
US3053198A (en) * 1958-02-21 1962-09-11 Midland Ross Corp Thermopump system
DE2910288A1 (de) * 1979-03-15 1980-09-25 Vaillant Joh Gmbh & Co Waermepumpe, insbesondere strahl- kompressions-waermepumpe
DD219060A3 (de) * 1983-07-11 1985-02-20 Dsf Waermeanlagenbau Absorptionswaermepumpe
US5157942A (en) * 1991-06-14 1992-10-27 Kim Dao Regenerative absorption cycles with multiple stage absorber
DE10240659B4 (de) * 2001-11-30 2011-07-07 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V., 80686 Verfahren und Vorrichtung zur solarthermischen Kälteerzeugung

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2008046120A2 *

Also Published As

Publication number Publication date
AT504399B1 (de) 2008-12-15
NO20091911L (no) 2009-05-15
CA2666172A1 (fr) 2008-04-24
WO2008046120A2 (fr) 2008-04-24
AT504399A1 (de) 2008-05-15
AU2007312922A1 (en) 2008-04-24
WO2008046120A3 (fr) 2008-11-13

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