EP3052869A1 - Procédé de réfrigération par absorption et machine de réfrigération par absorption - Google Patents

Procédé de réfrigération par absorption et machine de réfrigération par absorption

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Publication number
EP3052869A1
EP3052869A1 EP14780467.8A EP14780467A EP3052869A1 EP 3052869 A1 EP3052869 A1 EP 3052869A1 EP 14780467 A EP14780467 A EP 14780467A EP 3052869 A1 EP3052869 A1 EP 3052869A1
Authority
EP
European Patent Office
Prior art keywords
sorbent
channel
absorption
heat
absorber
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Withdrawn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
EP14780467.8A
Other languages
German (de)
English (en)
Inventor
Peter Schwerdt
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.)
Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
Original Assignee
Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
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 Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV filed Critical Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
Publication of EP3052869A1 publication Critical patent/EP3052869A1/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Withdrawn legal-status Critical Current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
    • 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
    • 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
    • F25B35/00—Boiler-absorbers, i.e. boilers usable for absorption or adsorption
    • F25B35/02—Boiler-absorbers, i.e. boilers usable for absorption or adsorption using a liquid as sorbent, e.g. brine
    • 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
    • F25B37/00—Absorbers; Adsorbers
    • 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 cooling process, for the provision of
  • a sorbent for absorbing and / or desorbing a refrigerant in the vacuum through a Sorptionsffenkanal at least one phase change module in the form of a
  • Absorbers and / or a desorber is passed. Furthermore, the invention relates to an absorption chiller of the type mentioned with an absorber, a desorber and a sorbent circulation between the absorber and the desorber. Absorption refrigeration processes utilize existing heat to provide refrigeration capacity
  • the heat is in a desorber on a
  • Sorbent transferred in which a refrigerant is absorbed.
  • the refrigerant is desorbed.
  • the refrigerant passes from the liquid phase into the gas phase and is then passed into a, for example, water-cooled, condenser, in which the refrigerant condenses with heat, that is liquefied, is.
  • the liquefied refrigerant is released into an evaporator and evaporated therein.
  • the refrigerant absorbs a considerable amount of heat in the form of heat of vaporization, whereby useful cooling capacity is provided at a low temperature level.
  • Cooling capacity can be used for different cooling purposes.
  • a particularly preferred use is the building air conditioning in the commercial and private sector.
  • the vaporized refrigerant is not released to the environment, but added for the purpose of recycling in an absorber again from the sorbent.
  • the sorbent is fed to the absorber coming from the desorber. Due to the absorption of the refrigerant in the sorbent is in
  • the sorbent is circulated by means of a pump in the sorbent circuit, the pressure side of the pump, the desorber is provided.
  • the desorber is under a higher pressure than the absorber, since the refrigerant vapor in the desorber due to higher temperature has a higher vapor pressure.
  • the sorbent Before entering the absorber, the sorbent is depressurized via a throttle, so that the sorbent in the absorber is at a lower pressure level.
  • the sorbent supplied to the desorber is preheated by the sorbent leaving the desorber, the sorbent leaving the desorber being simultaneously pre-cooled for absorption in the absorber. This is done in an indirect heat exchanger through which the sorbent streams flow separately.
  • the sorbent enriched with refrigerant in the absorber is fed to the desorber for renewed desorption of the refrigerant. In this way, both the refrigerant and the sorbent are recycled, the
  • Sorbent is conducted in a closed sorbent circuit.
  • the pressure level on which the absorption cooling process takes place depends on the sorbent (absorbent) and refrigerant system used
  • the sorbent can be used in the desorber as well as in the absorber under reduced pressure, i. at pressures below normal ambient pressure or
  • Temperature level is incurred and often can hardly be used on the spot makes sense.
  • Useful heat of a solar thermal system is incurred. However, it can also be used, for example, district heating or industrial process waste heat.
  • absorption chillers there is a need for small, on-demand mobile, lower power units. This can for example be in the range of 100 W to 10 kW.
  • a disadvantage of such absorption chillers are the high specific equipment costs. Therefore, there is currently a desire to reduce the volume and weight of corresponding absorption chillers. This can be done, for example, by plate absorbers and / or
  • Plate desorber can be achieved, which can be formed as modules and put together into so-called stacks or stacks, similar to fuel cell stacks. In this way, the volume, weight and, ultimately, the cost of absorption chillers can be reduced.
  • the modules in the form of an absorber and / or desorber have a sorbent channel for absorption or desorption, through which sorbent flows.
  • a heat transfer channel is provided, which is flowed through, for example, by warm or cold water.
  • only a thin partition wall is provided for a favorable heat transfer between the heat carrier channel and the sorbent channel. It would be desirable to make the channels and the partition as narrow as possible or thin, in order to provide a stack that has very many absorber modules and / or Desorbermodule at low height and thus allows high specific power. In practice, however, it has been shown that the modules can not be reduced arbitrarily. Neither the partition nor the sorbent channel or the heat transfer channel can be made arbitrarily narrow. The thinner the partition is formed, the easier the partition wall can deform due to the pressure differences of the media, resulting in uneven
  • Sorbent channel and / or the heat transfer channel reduces the performance of a phase change module and thus the specific power of the stack.
  • the present invention has the object, the
  • the object is achieved according to claim 1 by an absorption cooling process of the type mentioned, in which the sorbent for receiving
  • Absorption heat and / or for the delivery of Desorptionskor in negative pressure through a heat transfer channel of the at least one phase change module is passed and wherein the sorbent in at least one heat exchanger at least partially emits the heat of absorption to a heat transfer medium and / or the heat of desorption at least partially from one
  • Heat transfer medium absorbs.
  • Sorptionsstoffniklauf a heat exchanger for emitting heat of absorption to a separate heat transfer medium and / or for receiving desorption heat is provided by a separate heat transfer medium.
  • the invention has therefore recognized that higher specific cooling capacities can be realized with smaller absorption refrigeration machines and thus with correspondingly lower costs, if in the absorber and / or desorber instead of a separate heat transfer medium for supplying Desorptionsblaze for
  • Soprtionsmittel and / or for dissipating heat of absorption from the sorbent and the heat transfer channel is traversed by the sorbent. This allows, namely, the pressure difference between the Sorptionsstoffkanal and the
  • Sorbent channel on the one hand and the heat transfer channel on the other hand are Sorbent channel on the one hand and the heat transfer channel on the other hand.
  • the heat transfer channel of the absorber and / or the desorber is flowed through with sorbent, it is necessary for the actual
  • Heat removal from the absorption cooling process of another heat exchanger which allows a heat exchange with a separate heat transfer medium.
  • This heat exchanger is in the sorbent circuit between the absorber and the Desorber provided. This also means that the design effort of
  • Absorption chiller is higher than in the prior art. According to the invention, however, it has surprisingly been recognized that this additional design effort is more than compensated for by the increase of the specific power to be achieved thereby.
  • the advantage achieved by the invention can be achieved both with respect to the absorber and to the desorber. However, this will be particularly preferred for the absorber, since this is usually operated at a still somewhat lower pressure level than the desorber. In other words, the heat transfer channel of the desorber directly with a separate, providing the heat
  • Heat transfer medium such as in the form of warm water to be flowed through.
  • Heat transfer channel of the absorber flows through sorbent to the
  • Absorption heat is at least partially released to another medium.
  • This may be gaseous (e.g., air) or liquid (e.g., cooling water). The latter, however, will be preferred to reduce the space.
  • the heat exchange is also due to the negative pressure of the sorbent preferably indirectly, ie without direct contact of the heat exchanging media with each other, take place.
  • the flow of sorbent irrespective of the concentration of the substance absorbed in the sorbent, is referred to as a sorbent stream
  • the refrigerant may form a separate refrigerant flow between the desorber and the absorber.
  • the sorbent stream fed to the sorbent channel of a phase change module is preferably identical to that from the sorbent channel of the phase change module withdrawn sorbent stream, even if it has more or less refrigerant or in other words enriched with refrigerant or depleted. However, it is different when a sorbent stream is divided into two or more streams. Then the sub-streams each separate
  • Each of the partial flows is preferably considered as long as the same sorbent stream until it is divided again or combined with other sorbent streams.
  • the design effort can be reduced, for example, that the heat exchanger sorbent from several absorbers or
  • Absorber modules of a stack of an absorption chiller is supplied.
  • the heat exchanger can then also be made sufficiently robust, so that the pressure difference between the media streams leads to no appreciable deformation of the partition wall between the media streams.
  • absorber can be in the desorber both the
  • Heat transfer medium for example in the form of warm water, is transferred to the heat transfer medium flowing through the sorbent stream, in a separate heat exchanger.
  • This is also preferably be provided for indirect heat exchange with a liquid heat transfer medium.
  • this heat exchanger can be designed to simultaneously use useful heat for a plurality of desorber or desorber modules of a stack
  • the absorber modules and / or the desorber modules are designed to be similar, preferably of identical construction.
  • the absorbers and / or desorbers can be combined into stacks, for example by stacking on top of each other, around a high mass and heat exchange surface
  • the capacitor, the evaporator, the at least one pump and the at least one heat exchanger provided only once and the stack of absorber modules and Desorbermodulen or the stacks of either absorber modules or
  • the absorbers and / or the desorbers are connected in parallel, and thus through which sorbents are flowed through in parallel with one another, preferably the same. Additionally or alternatively, a plurality of sorbent channels and / or heat transfer channels may be provided in each absorber and / or desorber.
  • the sorbent is circulated between the at least one heat carrier channel and the at least one heat exchanger. So the sorbent is not just in the actual
  • the absorber and the desorber there is also at least one additional partial circuit, which leads sorbent between the absorber or the desorber and the associated heat exchanger in a circle. If the partial circuit is assigned to the desorber, the partial circuit is not passed through the absorber. If the partial circuit is assigned to the absorber alternatively or additionally, the partial circuit is not passed through the desorber. This allows an efficient operation of the absorption cooling process, because then expedient heat dissipated and / or heat can be supplied. However, the at least one partial circuit is preferably not decoupled from the actual sorbent circuit between the absorber and the desorber. Rather, an exchange of sorbent between the
  • the coupling of the sorbent circuit and the at least one partial circuit can be carried out simply and procedurally expedient if the
  • Sorbent channel is at least partially mixed. This applies to both phase change modules in the form of an absorber and a desorber, wherein preferably both phase change modules a corresponding separate
  • Partial circuit can be assigned. However, such a partial cycle can also be assigned only to the absorber or only to the desorber. The two
  • Sorbent streams from the respective heat carrier channel and the respective sorbent channel are therefore preferably merged nach.dem flowing through the heat transfer channel and the sorbent channel.
  • the partial circuit is assigned to the absorber, this preferably takes place only after the adsorber leaving the sorbent channel of the absorber and having been enriched with refrigerant passes the desorber and at least partially discharges the previously received refrigerant there.
  • the sorbent flowing from the desorber to the absorber is mixed with the sorbent flowing from the heat carrier channel of the absorber.
  • Sorbent channel desorber leaving, depleted with refrigerant sorbent has passed the absorber and has been enriched there with refrigerant again.
  • the sorbent flowing from the absorber to the desorber is mixed with the sorbent flowing out of the heat carrier channel of the desorber. It is particularly preferred in this context, if that the
  • Sorptionsffenstrom is first passed through the sorbent channel of the desorber, before the sorbent stream is at least partially mixed with the heat transfer channel of the absorber flowing through the sorbent stream, or vice versa.
  • This has the advantage that the sorbent stream enriched with refrigerant in the absorber is used only in the desorber, instead of depleting the concentration of the refrigerant beforehand by backmixing with another sorbent stream.
  • the sorbent streams are separated prior to entering the sorbent channel and the heat transfer channel of the absorber and / or desorber, preferably after passing through a heat exchanger for heating or cooling the sorbent. Before the separation of the sorbent streams, these can one
  • Entering the sorbent channel and the heat transfer channel of the desorber and / or absorber have at least substantially the same pressure and / or substantially the same temperature. Since it is generally preferred to operate the absorber at a low temperature level and the desorber at a higher temperature level, it makes sense when coming from the desorber, by the
  • At least one heat exchanger conducted sorbent is then divided into several streams to be passed into the at least one sorbent channel and the at least one heat transfer channel at least one absorber. Then, in the case of an absorber, both the at least one sorbent channel and the sorbent stream fed to the at least one heat carrier channel are then cooled. In the case of a subcircuit associated with the desorber, alternatively or additionally, both the sorbent stream fed to the sorbent channel and to the heat carrier channel of the desorber are heated.
  • Sorbent channel and heat transfer channel enters some sorbent from one in the other channel. Although this can lead to a corresponding change in concentration of refrigerant, but is otherwise less critical for the
  • the advantages of the absorption cooling process are obtained in particular if the negative pressure of the sorbent in the sorbent channel and in the heat transfer channel of the corresponding phase conversion module is at least 50 mbar (relative), in particular at least 100 mbar (relative). These pressures are relative pressures, ie the negative pressure compared to the ambient pressure or normal air pressure. In the case of pressure data without a special note or with the addition (absolute), these are absolute pressures. Underpressures of 50 mbar (relative) or 100 mbar (relative) in the sorbent channel would already be sufficient to deform partitions between the Sorptionsffenal and the heat transfer channel, such as when through the heat transfer medium under
  • Ambient pressure or normal air pressure or a pressure caused by further pumping pressure would flow. This is the case, in particular, if a sheet metal or a foil of metal and / or plastic is used as the dividing wall.
  • the advantages are all the greater if the pressure of the sorbent in the sorbent channel and in the heat transfer channel is less than 0.8 bar (absolute), preferably less than 0.5 bar (absolute), more preferably less than 0.25 bar (absolute), especially less than 0.1 bar (absolute).
  • the at least one phase change module is preferably an absorber and / or a desorber for the reasons mentioned. It can also be provided that an entire stack of, preferably stacked, absorbers and / or desorbers is provided. The absorber modules and / or the desorber modules are then preferably similar. Further preferably, the absorber modules and / or Desorbermodule are formed substantially identical, for example, to use a large number of identical parts. It is particularly preferred if the at least one phase change module
  • Membrane absorber and / or a membrane desorber is. These modules can namely be made very space-saving.
  • the sorbent channel is via a semipermeable membrane suitable for the
  • Hollow fiber membranes used to dissipate heat in a simple manner parallel to the sorption or to be able to supply heat.
  • Lithium bromide (LiBr) solution and / or as a refrigerant, preferably water, an alcohol or the like is used. Then the absorption cooling process is preferably carried out at low pressures. These are included, for example
  • absorption chiller it is preferably in accordance with the described absorption cooling process in terms of
  • Absorption refrigeration machine preferably, when the at least one heat exchanger is provided in at least one sub-circuit of sorbent and wherein the at least one partial circuit includes the absorber and / or the desorber.
  • the subcircuit of the absorber thus leads - if available - to bypass the desorber, while the subcircuit of the desorber - if present - to bypass the absorber.
  • undesirable accumulation or depletion of the sorbent with respect to the refrigerant is avoided.
  • the partial circuit may be connected to a line via which the partial circuit with a sorbent channel of the absorber or
  • Desorber is connected. This line is preferably used for supplying sorbent from the subcircuit to the sorbent channel. It can thus from the partial circuit via the corresponding line a sorbent stream
  • Partial circuit is assigned. So can a pressure equalization and a
  • Concentration compensation between the sorbent in the sorbent channel and the heat transfer channel can be achieved.
  • a line connecting the partial circuit with a sorbent channel of the absorber or desorber may be provided. This can serve to feed sorbent from the sorption channel to the subcircuit. It is further preferred in this context if the sorbent from the sorbent channel of the absorber is fed to the subcircuit of the desorber or the sorbent from the sorbent channel of the desorber to the subcircuit of the absorber. This leads to a pressure equalization of the two partial flows while avoiding a significant change in the concentration of refrigerant in the sorbent.
  • the at least one heat exchanger of the corresponding subcircuit associated with the absorber and / or the desorber can be arranged between the lines connected to the subcircuit for supplying sorbent to the subcircuit and for discharging sorbent from the subcircuit. Then, the common sorbent stream can be cooled or heated in the heat exchanger. Subsequently, the sorbent stream can be divided into then preferably equal tempered sorbent streams.
  • the heat exchanger is preferably in the flow direction of the sorbent after the line for supplying sorbent to the subcircuit and before the line for supplying
  • Sorbent provided to the sorbent channel of the absorber or desorber.
  • FIG. 1 shows a process flow diagram of an absorption cooling process
  • Fig. 2 is a process flow diagram of a first invention
  • Fig. 4 is an absorber of an absorption chiller of
  • FIG. 1 shows schematically an absorption cooling process known from the prior art.
  • the absorption chiller 1 for performing the absorption refrigeration process has an absorber 2, a desorber 3, a
  • Sorbent circuit 6 is supplied in the desorber 3 heat 7 via hot water, whereby the sorbent is heated and the absorbent absorbed in the sorbent refrigerant is partially desorbed.
  • the refrigerant passes
  • the refrigerant in the condenser 4 is withdrawn via a water cooling means of cooling water heat 8.
  • the now liquid refrigerant is then evaporated in the evaporator 5.
  • the refrigerant cools considerably, which is why the environment can be withdrawn for the purpose of a building cooling heat 9 at a relatively low temperature level.
  • the refrigerant is then re-absorbed in the sorbent. This happens under release of
  • Sorbent absorbed refrigerant is circulated.
  • a pump 12 is provided for circulating the sorbent.
  • the desorber 3 and the suction side of the absorber 2 is arranged.
  • the sorbent flowing back from the desorber 3 is expanded by means of a throttle 13.
  • a throttle 13 For preheating the desorber 3 supplied sorbent of this sorbent stream exchanges heat in a heat exchanger 14 with the heat leaving the desorber 3 and therefore warmer
  • an additional partial circuit of the sorbent comprising an additional heat exchanger 17 and the absorber 2.
  • the absorber 2 has, as in the prior art, a sorbent channel through which sorbent flows to absorb refrigerant.
  • a heat transfer channel is provided, via which during the absorption of the refrigerant absorption heat can be dissipated in the sorbent, so that the sorbent for receiving the refrigerant is not heated too much.
  • both the sorbent channel and the heat transfer channel of sorbent are both the sorbent channel and the heat transfer channel of sorbent
  • a cooling medium 18 in particular cooling water, cooled.
  • the sorbent circuit 6 between the absorber 2 and the desorber 3 and the absorber associated with the subcircuit are before the complementary
  • Heat exchanger 17 and in the illustrated and so far preferred
  • Interconnection can be dispensed with a supplementary pump in the partial circuit 16 of the absorber 2. This is in both the sorbent circuit 6 and in
  • Partial circuit 16 a throttle 13,19 provided, which is not mandatory. About the throttle 19 may, if necessary, a small pressure difference between the
  • Heat transfer channel and the sorbent channel of the absorber 2 are set to the thin partition between sorbent channel and the
  • Heat transfer channel to impose a desired shape, position or curvature.
  • each between the heat exchanger 17 and the absorber 2 chokes to adjust the pressures in both channels of the absorber 2 independently.
  • the sorbent in the partial circuit 16 is supplied to the heat carrier channel of the absorber 2, while the sorbent of the sorbent circuit 6 is passed through the sorbent channel of the absorber 2 and then to the desorber 3.
  • a further absorption cooling process is shown schematically, in which the corresponding absorption chiller 21 in comparison with the
  • Absorption chiller 20 of FIG. 2 has a second sub-circuit 22 for the sorbent.
  • This second partial circuit 22 has the same as the first
  • Partial circuit 16 an additional heat exchanger 23 and an additional pump 24. After the preheating of the sorbent, the sorbent is passed through the sorbent stream coming from the desorber 3 through the pump 24 and then through the heat exchanger 23.
  • the sorbent stream is heated by the heat transfer 7 providing heat transfer medium.
  • the heat transfer medium is warm water.
  • Desorber 3 heat transfer channel fed sorbent while the remaining sorbent stream via an optional throttle 25 for setting a small differential pressure between the sorbent channel and the
  • Heat transfer channel of the desorber 3 is passed into the sorbent channel of the desorber 3, where the sorbent emits refrigerant by desorption.
  • the heat removed from the sorbent of the sorbent channel is at least partially replaced by the sorbent flowing through the heat transfer channel transferring heat to the sorbent in the sorbent channel.
  • the refrigerant depleted sorbent from the sorbent channel then flows in the direction of the absorber 2, while the sorbent from the heat transfer channel through a throttle 26 and back into the pump 24 for conveying the sorbent to the desorber 3 and through the second partial circuit 22 flows.
  • Heat transfer channel can be used or adjusted to impose a desired shape, position or curvature of the thin partition between the sorbent channel and the heat transfer channel.
  • the absorbers 2 and the desorbers 3 according to FIGS. 2 and 3 are in particular membrane absorber modules and membrane desorber modules. Their structure corresponds to each other. The processes occurring therein and the material flows are merely inversely to one another. The processes are explained with reference to a schematic cross section of a membrane absorber module according to FIG. 4.
  • the absorber 30 has a plurality of steam chambers which are filled with porous structures 32. In the porous structures 32 enters the vaporized refrigerant 33, which is in the illustrated and so far preferred absorber 30 is water.
  • Refrigerant 33 passes through a semi-permeable membrane 34, which may rest on a support grid 35 in the illustrated and so far preferred absorber module, into the sorbent 36, which flows through a very narrow sorbent channel 37.
  • the refrigerant 33 is absorbed by the sorbent 36.
  • the released heat of absorption is at least partially discharged through a partition wall 38 in the form of a sheet or a foil of metal and / or plastic to the flowing through the heat transfer channel 39 sorbent 40.
  • the heat carrier channel 39 is formed in the illustrated and so far preferred absorber 30 substantially wider than the sorbent channel 37 and the adjacent sorbent channels 37.
  • substantially more sorbent 40 flows through the heat transfer channel 39 than through the adjacent sorbent channel 37 and the adjacent Sorptionsffenkanäle 37 to the sorbent 36 sufficiently cool in at least one sorbent channel 37.
  • a plurality of steam chambers 31, sorbent channels 37 and heat transfer channels 39 are provided. However, this is not necessarily the case.
  • the sorbent channel 37 and the heat transfer channel 39 can be made very thin and can also a very thin film as a partition 38 for the separation of the sorbent channel 37 from the heat transfer channel 39th be used.
  • the resulting phase change module is thus very shallow and thus can be used together with similar modules to form a flat stack.

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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

L'invention concerne un procédé de réfrigération par absorption servant à produire de la puissance frigorifique par utilisation de chaleur (7). Pour pouvoir produire en particulier de faibles puissances frigorifiques à peu de frais, dans un tel procédé de réfrigération par absorption, un sorbant (36) est acheminé sous pression négative à travers un conduit de sorbant (37) d'au moins un module de changement de phase se présentant sous la forme d'un absorbeur (2, 30) et/ou d'un désorbeur (3) pour l'absorption et/ou la désorption d'un réfrigérant (33), le sorbant (40) étant acheminé sous pression négative à travers un conduit de fluide caloporteur (39) de l'au moins un module de changement de phase pour absorber de la chaleur d'absorption et/ou délivrer de la chaleur de désorption, et le sorbant (40) délivrant au moins partiellement la chaleur d'absorption à un fluide caloporteur et/ou absorbant la chaleur de désorption au moins partiellement du fluide caloporteur, dans au moins un échangeur de chaleur (17, 23).
EP14780467.8A 2013-10-02 2014-10-01 Procédé de réfrigération par absorption et machine de réfrigération par absorption Withdrawn EP3052869A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013110960.8A DE102013110960A1 (de) 2013-10-02 2013-10-02 Absorptionskälteprozess und Absorptionskältemaschine
PCT/EP2014/071045 WO2015049288A1 (fr) 2013-10-02 2014-10-01 Procédé de réfrigération par absorption et machine de réfrigération par absorption

Publications (1)

Publication Number Publication Date
EP3052869A1 true EP3052869A1 (fr) 2016-08-10

Family

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EP14780467.8A Withdrawn EP3052869A1 (fr) 2013-10-02 2014-10-01 Procédé de réfrigération par absorption et machine de réfrigération par absorption

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EP (1) EP3052869A1 (fr)
DE (1) DE102013110960A1 (fr)
WO (1) WO2015049288A1 (fr)

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Publication number Priority date Publication date Assignee Title
US4333515A (en) * 1980-08-13 1982-06-08 Battelle Development Corp. Process and system for boosting the temperature of sensible waste heat sources
DE3408193C2 (de) * 1984-03-06 1987-04-23 Markus 8058 Erding Rothmeyer Verfahren zum Erhöhen der Temperatur von Wärme durch einen Wärmepumpenprozeß
US4748830A (en) * 1986-02-28 1988-06-07 Hitachi, Ltd. Air-cooled absorption heating and cooling system
US5077986A (en) * 1990-02-09 1992-01-07 Columbia Gas System Service Corp. Energy recovery system for absorption heat pumps

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DE102013110960A1 (de) 2015-04-02
WO2015049288A1 (fr) 2015-04-09

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