EP3329191B1 - Dispositif et procédé permettant la mise en uvre d'un processus de vaporisation à froid - Google Patents

Dispositif et procédé permettant la mise en uvre d'un processus de vaporisation à froid Download PDF

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Publication number
EP3329191B1
EP3329191B1 EP16748095.3A EP16748095A EP3329191B1 EP 3329191 B1 EP3329191 B1 EP 3329191B1 EP 16748095 A EP16748095 A EP 16748095A EP 3329191 B1 EP3329191 B1 EP 3329191B1
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EP
European Patent Office
Prior art keywords
high pressure
expander
fluid
mass flow
pressure level
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.)
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EP16748095.3A
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German (de)
English (en)
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EP3329191A1 (fr
Inventor
Joerg Nickl
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.)
Bitzer Kuehlmaschinenbau GmbH and Co KG
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Bitzer Kuehlmaschinenbau GmbH and Co KG
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/06—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point using expanders
    • 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
    • F25B11/00—Compression machines, plants or systems, using turbines, e.g. gas turbines
    • F25B11/02—Compression machines, plants or systems, using turbines, e.g. gas turbines as expanders
    • 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
    • F25B31/02—Compressor arrangements of motor-compressor units
    • F25B31/026—Compressor arrangements of motor-compressor units with compressor of rotary 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
    • 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
    • F25B43/006—Accumulators
    • 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
    • F25B9/008—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant being carbon dioxide
    • 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
    • F25B2400/00—Component parts or details not otherwise provided for in this subclass
    • F25B2400/06—Several compression cycles arranged in parallel
    • 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
    • F25B2400/00—Component parts or details not otherwise provided for in this subclass
    • F25B2400/13—Economisers
    • 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
    • F25B2400/00—Component parts or details not otherwise provided for in this subclass
    • F25B2400/23—Separators

Definitions

  • the present invention relates to a device and a method for
  • DE 10010864 shows a device according to the preamble of claim 1.
  • the present invention is therefore based on the object of proposing a device and a method for carrying out a cold steam process, with which a simplified control and regulation of the cold steam process is possible.
  • a device for carrying out a cold steam process has a motor-driven main compressor which is designed to suck in a mass flow of a fluid serving as a coolant which is at the evaporator pressure level and to compress this mass flow to a high pressure level.
  • a high pressure heat exchanger is provided in order to cool the mass flow of the fluid which is at the high pressure level, to increase its density and to reduce a temperature of the fluid by cooling.
  • the mass flow of the fluid coming from the high pressure heat exchanger is expanded to the evaporator pressure level in an expander and is fed to an evaporator.
  • the evaporator is designed to absorb heat so that the density of the fluid decreases as it passes through the evaporator and the temperature of the mass flow coming from the expander, which is at the evaporator pressure level and passes through the evaporator, increases.
  • a subcooler is provided downstream of the high pressure heat exchanger and upstream of the expander. After the subcooler and before the expander, a part of the mass flow of the fluid that is at high pressure level can be branched off and expanded to medium pressure level by means of a high pressure control valve, so that the fluid then absorbs heat at medium pressure level in countercurrent in the subcooler and thereby subcools the mass flow that is at high pressure level in the subcooler.
  • a high pressure compressor that is mechanically directly connected to the expander is designed to exclusively supply the fluid that is branched off between the subcooler and before the expander and in countercurrent to the To compress the mass flow of fluid passing through the subcooler, which is at high pressure level, from medium pressure level to high pressure level and to mix it with the mass flow of fluid coming from the motor-driven main compressor upstream of the high pressure heat exchanger.
  • the device described enables efficient control of the high pressure that is typically present at the high pressure heat exchanger, the high pressure compressor and partly at the subcooler. Because the high pressure compressor, which is also directly driven by the expander, only compresses a separate mass flow of the fluid, the medium pressure mass flow, the mass flow that is guided through the expander and comes from the high pressure heat exchanger can be additionally subcooled. The exergy of the expansion is thus ultimately used for additional subcooling at high pressure, or the output of the expander is used to compress the medium pressure mass flow in the high pressure compressor.
  • a collector can be arranged after the expander (and thus before the evaporator). This is designed to separate a liquid phase of the fluid and a vapor phase of the fluid.
  • the liquid phase of the fluid can be stored in the collector and expanded to evaporator pressure via an injection valve arranged between the collector and the evaporator.
  • the vapor phase of the fluid can be expanded via a pressure-maintaining valve.
  • the expanded liquid phase can be fed to the evaporator in the mass flow, while the expanded vapor phase after the evaporator can be mixed into the mass flow of the fluid coming from the evaporator.
  • the expander and the high-pressure compressor are arranged in a common housing and form a unit, which is also referred to as an "expander-compressor unit".
  • the arrangement in a single housing enables a space-saving design in which the expander and the high-pressure compressor can be mechanically connected directly to one another, in particular in a pressure-tight manner.
  • the displacement ratio between the expander and the high-pressure compressor should preferably be between 0.5 and 0.75 to ensure optimum cold steam processing.
  • the displacement ratio is particularly preferably 0.6. In principle, lower values are sensible for high recooling temperatures at the outlet of the high-pressure heat exchanger.
  • the working spaces of the expander can be controlled via a main slide and an auxiliary slide.
  • the main slide and the auxiliary slide are arranged centrally between the working spaces of the expander, which are usually located on the inside and therefore face each other.
  • the main slide valve and/or the auxiliary slide valve are designed as flat slide valves in order to ensure simple and particularly tight operation with only a small space requirement.
  • auxiliary slide of the working piston is movable by two pins.
  • a piston rod that keeps the working pistons at a distance is detachably connected to the working pistons, i.e. not permanently connected to them.
  • This is simple in terms of manufacturing and yet functional, as the internal piston rod only experiences compressive forces and therefore does not have to be permanently connected to the piston or pistons. This means that small misalignments of housing parts can be accepted and production is made easier.
  • a main slide unit consisting of the main slide, a slide rod and a slide piston can be constructed in the same way.
  • An auxiliary slide unit consisting of the auxiliary slide and the pins can also be constructed in the same way.
  • a high pressure level between 50 bar and 100 bar
  • a medium pressure level between 40 bar and 65 bar
  • a collector pressure level between 30 bar and 35 bar
  • an evaporator pressure level between 25 bar and 30 bar.
  • a method for carrying out a cold vapor process has a method step in which a mass flow of a fluid serving as a refrigerant, which is at evaporator pressure level, is compressed to high pressure level by a motor-driven main compressor. This mass flow of the fluid, which is at high pressure level, is cooled in a high pressure heat exchanger, whereby a density is increased and a temperature of the fluid is reduced. The fluid coming from the high pressure heat exchanger is expanded to evaporator pressure level in an expander, whereby the expander is mechanically connected directly to a high pressure compressor.
  • the fluid coming from the expander is led into an evaporator and absorbs heat there, so that the density of the fluid decreases and the temperature of the mass flow of the fluid coming from the expander, which is at evaporator pressure level, increases.
  • the fluid is led through a subcooler, whereby between the subcooler and before the expander, part of the fluid is branched off from the mass flow at high pressure level and expanded to medium pressure level by means of a high-pressure control valve.
  • the fluid is then led through the subcooler at medium pressure level in countercurrent to the mass flow led through the subcooler, which is at high pressure level, where it absorbs heat and the mass flow, which is at high pressure level, is subcooled.
  • the fluid in the branched medium-pressure mass flow reaches the high-pressure compressor, which exclusively compresses the countercurrent fluid from medium-pressure level to high-pressure level and mixes it with the mass flow coming from the motor-driven main compressor before the high-pressure heat exchanger.
  • the fluid is led into a collector after the expander, in which a liquid phase of the fluid is separated from a vapor phase of the fluid.
  • the liquid phase is expanded to evaporator pressure via an injection valve.
  • the vapor phase of the fluid is expanded via a pressure-maintaining valve and, after the evaporator, is mixed into the mass flow of the fluid coming from the evaporator.
  • Carbon dioxide, C0 2 can be used as a fluid, which is also referred to as a coolant in this context, because carbon dioxide is non-explosive and non-flammable, but thermally stable.
  • a coolant As a coolant, its advantages include a low specific volume and a high heat transfer coefficient as well as low pressure losses when flowing through heat exchangers.
  • the described method can be carried out with the described device or the described device is configured to carry out the described method.
  • FIG. 1 shows a schematic representation of a cold steam process.
  • a low-pressure circuit in which a fluid, in the illustrated embodiment carbon dioxide, comes from a collector S through an injection valve TV and passes through an evaporator V to a motor-driven main compressor CI.
  • the fluid compressed by the main compressor CI mixes with a medium-pressure mass flow of the fluid compressed by a high-pressure compressor C2 in front of the high-pressure heat exchanger H, in which a higher pressure is maintained than in the collector S. From the high-pressure heat exchanger H, the fluid passes through a subcooler U and the expander E back into the collector S.
  • a separate medium-pressure mass flow is compressed by the high-pressure compressor C2, which is directly driven by the expander E, before it reaches the high-pressure heat exchanger H.
  • the high-pressure compressor C2 only compresses this medium-pressure mass flow, i.e. no fluid that is guided outside the medium-pressure mass flow.
  • the high-pressure heat exchanger H which is also referred to as a gas cooler or condenser
  • the fluid just coming from the high-pressure heat exchanger H is transferred to a high-pressure heat exchanger H between the high-pressure heat exchanger H and the high-pressure heat exchanger H. and the expander E is divided after passing through the subcooler U.
  • the branched fluid then absorbs heat in the subcooler U in countercurrent and reaches the high-pressure compressor C2. This additionally subcools the high-pressure mass flow of the fluid. The exergy of the expansion is thus used for additional subcooling at high pressure.
  • the medium-pressure mass flow compressed to high pressure by the high-pressure compressor C2 is mixed with the fluid coming from the main compressor CI upstream of the high-pressure heat exchanger H.
  • a pressure difference and a suction volume flow can be freely adjusted on the high-pressure compressor C2 according to what is available on the expander side. If the high-pressure control valve or throttle TH is closed, the pressure difference increases until the expander-compressor unit shown stops and there is no more expander mass flow. The result is an increasing high pressure. If the high-pressure control valve TH is now slowly opened, the medium pressure increases again until the expander E is running and the desired expander mass flow, high pressure and expander inlet temperature are set. However, the high pressure should only be increased to such an extent that a minimal temperature difference remains on the "hot side" of the subcooler U, i.e. on the high-pressure compressor side. This is another control principle. The expander mass flow is thus regulated without throttling it, which would be equivalent to a loss of exergy.
  • the collector pressure in the collector S is only selected to be high enough to ensure sufficient controllability of the injection valve TV and a pressure holding valve TS, which is arranged in a line connected between a vapor space of the collector S and after the evaporator V and before the main compressor CI. With a constant evaporator pressure, this allows a constantly low collector pressure, regardless of the high pressure.
  • a coefficient of performance at an evaporation temperature of -10 °C and an ambient temperature of 20 °C can be increased by around 15 percent compared to a simple cold steam process in which only a compressor, a high-pressure gas cooler or condenser, a throttle valve, a collector and an evaporator are used in a known manner.
  • the high pressure remains at comparable values.
  • further exergy losses can be reduced by a two-stage compression with intermediate cooling, whereby the rest of the process control or the rest of the structure remains the same.
  • expander E in several stages, ie to allow the expansion of the fluid to take place in several stages.
  • several individual expanders E can be arranged one behind the other.
  • FIG 2 shows in a Figure 1
  • the corresponding view shows the described process without the collector S.
  • Recurring features are provided with identical reference numerals in this figure as well as in the following figures.
  • the expander E thus leads the fluid directly to the evaporator V without the fluid first passing through the collector S. Accordingly, the injection valve TV and the pressure holding valve TS are also obsolete.
  • Figure 3 shows a side view of a cross-section through an expander-compressor unit consisting of the expander E and the high-pressure compressor C2, which are arranged in a common housing 10 and thus form the expander-compressor unit.
  • Two pistons 1 and 2 are kept at a distance by a piston rod 3 and spatially separated from one another by a central part 4 of the unit.
  • the working space 5.1 and the working space 5.2 are each one of two expander working spaces, while the working spaces 6.1 and 6.2 are each one of two compressor working spaces.
  • a value between 0.5 and 0.75 has proven to be the optimal displacement ratio for the unit shown.
  • the internal expander working spaces 5.1 and 5.2 are controlled by an auxiliary slide 9 or a main slide 8 arranged in the middle part 4.
  • the auxiliary slide 9 is moved directly by the working pistons 1 and 2 by pins 7.
  • the auxiliary slide 9 then applies pressure to the main slide 8, which then moves and controls an inflow opening and an outflow opening for the working spaces 5.1 and 5.2 of the expander E by opening and closing.
  • the main slide 8 and the auxiliary slide 9 are advantageously designed as flat slides.
  • Simple ball valves are arranged in the compressor working chambers 6.1 and 6.2. Since the piston rod 3 in the illustrated embodiment only experiences pressure forces, the piston rod 3 is not firmly connected to the pistons 1 and 2, but is detachably connected, in that the pistons 1 and 2 only touch the piston rod 3 at the front or across its surface.
  • Figure 4 shown in a side view, in which the working pistons 1 and 2 are separated from the piston rod 3. In other embodiments, however, a fixed connection can of course also be present. The construction shown thus also allows the use of O-rings in places that would otherwise be difficult to seal.
  • Figure 5 represents a sectional view along the line BB of Figure 3 by an end piece of the expander-compressor unit.
  • a compressor valve designed as a ball valve is connected to an upper connection on the high-pressure side and to its lower connection to the medium-pressure level of the subcooler U.
  • FIG 6 is a sectional view of the middle part 4 of the Figure 3 shown expander-compressor unit along the line AA.
  • An upper connection leads the fluid from the high pressure level of the subcooler U, while the lower connection leads to the collector S.
  • the main slide 8 is connected to a slide piston 12 via a slide rod 11, this connection being detachable. This is shown in a side view in Figure 7 also shown, in which the main slide 8, the slide rod 11 and the slide piston 12 are shown as separate and distinct components.
  • auxiliary slide 9 together with the pins 7 used for its actuation by the working pistons 1 and 2 is in Figure 8 along a line DD from Figure 3 shown.
  • Figure 9 shows in a Figure 4 corresponding view the auxiliary slide 9 and the two pins 7 in a separate manner, by means of which the auxiliary slide 9 can be moved.
  • Figure 10 shows a top view of a sealing frame 13 with two O-rings 14 and 15 for the auxiliary slide 9, which are arranged in openings in the sealing frame 13 during installation.
  • the main slide 8 including slide rod 11 and slide piston 12 in plan view along the line CC from Figure 3
  • Figure 12 a further sealing frame 16 with O-ring 17 for the main slide 8.
  • the described construction allows the use of O-rings on surfaces that are difficult to seal (namely around the main slide 8 and the auxiliary slide 9), so that pocket milling is avoided by appropriate support frames.

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Claims (11)

  1. Dispositif de mise en œuvre d'un processus de vaporisation à froid, avec
    un compresseur principal à moteur (CI), qui est mis au point pour aspirer un flux massique d'un fluide faisant office d'agent de refroidissement, qui se trouve à un niveau de pression d'évaporation, et pour comprimer ledit flux massique à un niveau de haute pression,
    un échangeur de chaleur haute pression (H), qui est mis au point pour refroidir le flux massique du fluide, qui se trouve à niveau de haute pression, pour augmenter la densité et pour réduire la température du fluide,
    un détendeur (E), qui est mis au point pour détendre en produisant un travail le flux massique du fluide provenant de l'échangeur de chaleur haute pression (H) à un niveau de pression d'évaporation,
    un évaporateur (V), qui est mis au point pour absorber de la chaleur de telle sorte que la densité du fluide diminue lors du passage lorsqu'il traverse l'évaporateur (V), et pour augmenter la température du flux massique provenant du détendeur (E), qui se trouve à un niveau de pression d'évaporation, et du fluide guidé à travers l'évaporateur (V),
    un sous-refroidisseur (U) monté en aval de l'échangeur de chaleur haute pression (H) et en amont du détendeur (E),
    dans lequel fluide absorbe de la chaleur dans le sous-refroidisseur (U) à contre-courant à un niveau de moyenne pression et sous-refroidit ce faisant le flux massique traversant le sous-refroidisseur, qui se trouve à un niveau de haute pression,
    un compresseur haute pression (C2), qui est mis au point pour comprimer le flux massique guidé à contre-courant vers le flux massique du fluide traversant le sous-refroidisseur (U) et se trouvant à haute pression, qui se trouve à un niveau de moyenne pression et pour le mélanger au flux massique provenant du compresseur principal à moteur (CI) en amont de l'échangeur de chaleur haute pression (H),
    caractérisé en ce que la partie du flux massique du fluide, guidée à contre-courant à travers le sous-refroidisseur (U), laquelle se trouve à un niveau de haute pression, peut être dérivée en aval du sous-refroidisseur (U) et en amont du détendeur (E) et peut être détendue à un niveau de moyenne pression au moyen d'une soupape de régulation haute pression (TH), que le compresseur haute pression (C2) est directement relié de manière mécanique au détendeur (E) pour comprimer exclusivement le flux massique dérivé en amont du détendeur (E), et qu'un flux massique de détendeur peut être régulé au moyen de la soupape de régulation haute pression (TH), dans lequel une différence de pression et un volume d'aspiration peuvent être réglés sur le compresseur haute pression (C2) de manière à correspondre à une offre sur le côté de détendeur en ce que lors d'une fermeture de la soupape de régulation haute pression (TH), sa différence de pression augmente lentement jusqu'à ce que l'unité composée du détendeur (E) et du compresseur (C2) relié directement de manière mécanique s'arrête si bien qu'aucun flux massique de détendeur n'est plus présent ce qui provoque l'augmentation de la haute pression, et que la moyenne pression augmente lors d'une ouverture de la soupape de régulation haute pression (TH) jusqu'à ce que le détendeur (E) fonctionne et le flux massique de détendeur souhaité, la haute pression et la température d'entrée de détendeur soient réglés.
  2. Dispositif selon la revendication 1, caractérisé en ce qu'est disposé en aval du détendeur (E) un collecteur (S), qui est mis au point pour séparer une phase liquide du fluide et une phase vapeur du fluide, dans lequel la phase liquide peut être stockée, peut être détendue sur la pression d'évaporation par l'intermédiaire d'une soupape d'injection (TV) et la phase vapeur du fluide peut être détendue par l'intermédiaire d'une soupape de maintien de pression (TS), dans lequel la phase liquide détendue peut être amenée à l'évaporateur (V) et la phase vapeur détendue peut être mélangée en aval de l'évaporateur (V) au flux massique provenant de l'évaporateur.
  3. Dispositif selon la revendication 1 ou la revendication 2, caractérisé en ce que le détendeur (E) et le compresseur haute pression (C2) sont disposés dans un boîtier (10) commun.
  4. Dispositif selon l'une quelconque des revendications précédentes, caractérisé en ce qu'un rapport de cylindrée entre le détendeur (E) et le compresseur haute pression (C2) est maintenu entre 0,5 et 0,75.
  5. Dispositif selon l'une quelconque des revendications précédentes, caractérisé en ce que des espaces de travail (5.1, 5.2) du détendeur (E) peuvent être commandés par l'intermédiaire d'un coulisseau principal (8) et d'un coulisseau auxiliaire (9), qui sont disposés au centre entre les espaces de travail (5.1, 5.2).
  6. Dispositif selon la revendication 5, caractérisé en ce que le coulisseau principal (8) et/ou le coulisseau auxiliaire (9) sont réalisés en tant que coulisseaux plats.
  7. Dispositif selon la revendication 5 ou la revendication 6, caractérisé en ce que le coulisseau auxiliaire (9) peut être déplacé par des pistons de travail (1, 2) par au moins deux broches (7).
  8. Dispositif selon la revendication 7, caractérisé en ce qu'une tige de piston (3) est reliée de manière amovible aux pistons de travail (1, 2).
  9. Procédé de mise en œuvre d'un processus de vaporisation à froid, dans lequel
    un flux massique d'un fluide faisant office d'agent de refroidissement, qui se trouve à un niveau de pression d'évaporation, est aspiré par un compresseur principal à moteur (CI) et est comprimé à un niveau de haute pression,
    le flux massique du fluide, qui se trouve à un niveau de haute pression, est refroidi dans un échangeur de chaleur haute pression (H), dans lequel une densité est augmentée et une température du fluide est diminuée,
    le fluide provenant de l'échangeur de chaleur haute pression (H) est détendu tout en produisant un travail à un niveau de pression d'évaporation dans un détendeur (E),
    le fluide provenant du détendeur (E) est guidé dans un évaporateur (V) et absorbe de la chaleur de sorte que la densité baisse et la température du flux massique provenant du détendeur (E), qui se trouve à un niveau de pression d'évaporation, augmente,
    dans lequel le fluide est guidé à travers un sous-refroidisseur (U) en aval de l'échangeur de chaleur haute pression (H),
    et une partie du fluide est dérivée et est détendue à une moyenne pression et est guidée vers le flux massique s'écoulant à un niveau de haute pression à contre-courant dans le sous-refroidisseur (U), absorbe de la chaleur et le flux massique dans le sous-refroidisseur, qui se trouve à un niveau de haute pression, est sous-refroidi ce faisant,
    et le fluide détendu à la moyenne pression après avoir traversé le sous-refroidisseur (U) traverse un compresseur haute pression (C2), dans lequel exclusivement le fluide guidé à contre-courant est compressé à un niveau de haute pression par le compresseur haute pression (C2) et est mélangé au flux massique provenant du compresseur principal à moteur (CI) en amont de l'échangeur de chaleur haute pression (H),
    caractérisé en ce qu'entre le sous-refroidisseur (U) et en amont du détendeur (E), la partie du fluide guidée à contre-courant à travers le sous-refroidisseur (U) est dérivée du flux massique guidé à travers le sous-refroidisseur (U), qui se trouve à un niveau de haute pression et est détendu à un niveau de moyenne pression au moyen d'une soupape de régulation haute pression (TH), dans lequel le détendeur (E) est relié directement de manière mécanique au compresseur haute pression (C2) pour comprimer exclusivement le flux massique dérivé en amont du détendeur (E) de sorte qu'un flux massique de détendeur est régulé au moyen de la soupape de régulation haute pression (TH), et une différence de pression et un volume d'aspiration peuvent être réglés sur le compresseur haute pression (C2) de manière à correspondre à une offre sur le côté de détendeur en ce que lors d'une fermeture de la soupape de régulation haute pression (TH), sa différence de pression augmente lentement jusqu'à ce que l'unité composée du détendeur (E) et du compresseur (C2) relié directement de manière mécanique s'arrête de sorte qu'aucun flux massique de détendeur n'est plus présent, ce qui provoque l'augmentation de la haute pression, et que lors d'une ouverture de la soupape de régulation haute pression (TH), la moyenne pression augmente jusqu'à ce que le détendeur (E) fonctionne et que le flux massique de détendeur souhaité, la haute pression et la température d'entrée de détendeur soient réglés.
  10. Procédé selon la revendication 9, caractérisé en ce que le fluide est guidé en aval du détendeur (E) dans un collecteur (S), dans lequel une phase liquide du fluide est séparée d'une phase vapeur du fluide et la phase liquide est détendue sur une pression d'évaporation par l'intermédiaire d'une soupape d'injection (TV) et la phase vapeur du fluide est détendue par l'intermédiaire d'une soupape de maintien de pression (TS) et sont mélangées au flux massique du fluide provenant de l'évaporateur (V) en aval de l'évaporateur (V).
  11. Procédé selon la revendication 9 ou la revendication 10, caractérisé en ce que du dioxyde de carbone est utilisé en tant que fluide.
EP16748095.3A 2015-07-31 2016-07-29 Dispositif et procédé permettant la mise en uvre d'un processus de vaporisation à froid Active EP3329191B1 (fr)

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DE102017124643B4 (de) 2017-10-23 2021-03-04 Technische Universität Dresden Kälteanlage und Verfahren zum Betreiben der Kälteanlage
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DE102021125108A1 (de) 2021-09-28 2023-03-30 Technische Universität Dresden, Körperschaft des öffentlichen Rechts Expansions-Kompressionsmaschine für Kältekreisläufe

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JP2018521295A (ja) 2018-08-02
WO2017021293A1 (fr) 2017-02-09
BR112018002125A2 (pt) 2018-09-11
US20180149391A1 (en) 2018-05-31
AU2016302538B2 (en) 2020-04-02
CN107949756A (zh) 2018-04-20
EP3329191A1 (fr) 2018-06-06
JP6998298B2 (ja) 2022-01-18
DE102015214705A1 (de) 2017-02-02
US10254018B2 (en) 2019-04-09
AU2016302538A1 (en) 2018-02-22
BR112018002125B1 (pt) 2023-04-18

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