EP0424474B2 - Verfahren zum betrieb eines kaltdampfprozesses unter trans- oder überkritischen bedingungen - Google Patents

Verfahren zum betrieb eines kaltdampfprozesses unter trans- oder überkritischen bedingungen Download PDF

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Publication number
EP0424474B2
EP0424474B2 EP89910211A EP89910211A EP0424474B2 EP 0424474 B2 EP0424474 B2 EP 0424474B2 EP 89910211 A EP89910211 A EP 89910211A EP 89910211 A EP89910211 A EP 89910211A EP 0424474 B2 EP0424474 B2 EP 0424474B2
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Prior art keywords
refrigerant
pressure
evaporator
liquid
compressor
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EP89910211A
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English (en)
French (fr)
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EP0424474B1 (de
EP0424474A1 (de
Inventor
Gustav Lorentzen
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SINVENT A/S TE TRONDHEIM, NOORWEGEN.
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Sinvent AS
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B1/00—Compression machines, plants or systems with non-reversible cycle
    • 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
    • F25B45/00—Arrangements for charging or discharging 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
    • F25B40/00—Subcoolers, desuperheaters or superheaters
    • 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
    • F25B41/00—Fluid-circulation arrangements
    • F25B41/20—Disposition of valves, e.g. of on-off valves or flow control valves
    • 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
    • F25B2309/00—Gas cycle refrigeration machines
    • F25B2309/06—Compression machines, plants or systems characterised by the refrigerant being carbon dioxide
    • F25B2309/061—Compression machines, plants or systems characterised by the refrigerant being carbon dioxide with cycle highest pressure above the supercritical pressure
    • 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—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
    • F25B2400/04—Refrigeration circuit bypassing means
    • F25B2400/0411—Refrigeration circuit bypassing means for the expansion valve or capillary tube
    • 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—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
    • F25B2400/04—Refrigeration circuit bypassing means
    • F25B2400/0415—Refrigeration circuit bypassing means for the receiver
    • 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—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
    • F25B2400/16—Receivers
    • 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
    • F25B2600/00—Control issues
    • F25B2600/17—Control issues by controlling the pressure of the condenser
    • 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
    • F25B2600/00—Control issues
    • F25B2600/25—Control of valves
    • F25B2600/2501—Bypass valves

Definitions

  • the invention relates to a method of operating a vapour compression cycle ; in particular, the invention relates to a method of operating a vapour compression cycle as e.g. employed in refrigerators, air-conditioning units and heat pumps, using a refrigerant operating in a dosed circuit under supercritical high-side conditions.
  • a conventional vapour compression cycle device for refrigeration, air-conditioning or heat pump purposes is shown in principle in Fig. 1.
  • the device consists of a compressor (1), a condensing heat exchanger (2), a throttling valve (3) and a evaporating heat exchanger (4). These components are connected in a closed flow circuit, in which a refrigerant is circulated.
  • the operating principle of a vapour compression cycle device is as follows: The pressure and temperature of the refrigerant vapour is increased by the compressor (1), before it enters the condenser (2) where it is cooled and condensed, giving off heat to a secondary coolant, The high-pressure liquid is then throttled to the evaporator pressure and temperature by means of the expansion valve (3). In the evaporator (4), the refrigerant boils and absorbs heat from its surroundings. The vapour at the evaporator outlet is drawn into the compressor, completing the cycle.
  • refrigerants as for instance R-12, CF 2 Cl 2
  • refrigerant A number of different substances or mixtures of substances may be used as a refrigerant.
  • the choice of refrigerant is among others influenced by the condensation temperature, as the critical temperature of the fluid sets the upper limit for the condensation to occur. In order to maintain a reasonable efficiency, it is normally desirable to use a refrigerant with critical temperature at least 20-30K above the condensation temperature. Near-critical temperatures are normally avoided in design and operation of conventional systems.
  • US-A-4205532 discloses a heatpump or refrigeration apparatus, where the refrigerant on the high pressure side is at supercritical pressure. However, no regulation of the pressure is disclosed.
  • Capacity control of the conventional vapour compression cycle device is achieved mainly by regulating the mass flow of refrigerant passing through the evaporator. This is done e.g. by controlling the compressor capacity, throttling or bypassing. These methods involve more complicated flow circuit and components, need for additional equipment and accesories, reduced part-load efficiency and other complications.
  • a common type of liquid regulation device is a thermostatic expansion valve, which is controlled by the superheat at the evaporator outlet, Proper valve operation under varying operating conditions is achieved by using a considerable part of the evaporator to superheat the refrigerant, resulting in a low heat transfer coefficient.
  • thermodynamic losses occur due to large temperature differences when giving off heat to a secondary coolant with large temperature increase, as in heat pump applications or when the avalable secondary coolant flow is small.
  • Another object of the present invention is to provide a vapour compression cycle avoiding use of CFC refrigerants, and at the same time offering possibility to apply several attractive refrigerants with respect to safety, environmental hazards and price.
  • Further object of the present invention is to provide a new method of capacity control, which involves operation at mainly constant refrigerant mass flow rate and simple capacity modulation by valve operation.
  • Still another object of the present invention is to provide a cycle rejecting heat at gilding temperature, reducing heat-exchange losses in applications where secondary coolant flow is small or when the secondary coolant is to be heated to a relatively high temperature.
  • the vapour compression cycle operates normally at trans-critical conditions (i.e. super-critical high-side pressure, sub-critical low-side pressure) where the thermodynamic properties in the super-critical state are utilized to control the refrigerating and heating capacity of the device.
  • the present invention involves the regulation of specific enthalpy at evaporator inlet by deliberate use of the pressure before throttling for capacity control. Capacity is controlled by varying the refrigerant enthalpy difference in the evaporator, by changing the specific enthalpy of the refrigerant before throttling, In the supercritical state this can be done by varying the pressure and temperature independently. According to the present invention this modulation of specific enthalpy is done by varying the pressure before throttling, The refrigerant is cooled down as far as it is feasible by means of the avalable cooling medium, and the pressure regulated to give the required enthalpy.
  • Fig. 1 is a schematic representation of a conventional (sub-critical) vapour compression cycle device.
  • Fig. 2 is a schematic representation of a trans-critical vapour compression cycle device for use in connection with with a preferred embodiment of the invention.
  • This embodiment includes a volume as an integral part of the evaporator system, holding refrigerant in the liquid state.
  • Fig. 3 is a schematic representation of a trans-critical vapour compression cycle device. This embodiment includes an intermediate pressure receiver connected directly into the flow circuit between two valves.
  • Fig. 4 is schematic representation of a trans-critical vapour compression cycle device. This embodiment includes a special receiver to hold refrigerant as liquid or in the super-critical state.
  • Fig. 5 is a graph illustrating the relationship of pressure versus enthalpy of the trans-critical vapour compression cycle device of Fig. 2, 3 or 4, at different operating conditions.
  • Fig. 6 is a collection of graphs illustrating the control of refrigerating capacity by the method of pressure control in accordance with the present invention. The results shown are measured in a laboratory demonstration system built according to a preferred embodiment of the invention.
  • Fig. 7 is test results showing the relationship of temperature versus entropy of the trans-critical vapour compression cycle device of Fig. 2, operating at different highside pressures, employing carbon dioxide as refrigerant.
  • a trans-critical vapour compression cycle for use in the present invention includes a refrigerant, of which critical temperature is between the temperature of the heat inlet and the mean temperature of heat submittal, and a closed working fluid circuit where the refrigerant is circulated.
  • Suitable working fluids may be by the way of examples: ethyten (C 2 H 4 ), diborane (B 2 H 6 ), carbon dioxide (CO 2 ), ethane (C 2 H 6 ) and nitrogen oxide (N 2 O).
  • the dosed working fluid circuit consists of a refrigerant flow loop with an integrated storage segment
  • Fig. 2 shows a preferred embodiment of the invention where the storage segment is an integral part of the evaporator system.
  • the flow circuit includes a compressor 10 connected in series to a heat exchanger 11, a counterflow heat exchanger 12 and a throttling valve 13.
  • the throttling valve can be replaced by an optional expansion device.
  • An evaporating heat exchanger 14, a liquid separator/receiver 16 and the low-pressure side of the counterflow heat exchanger 12 are connected in flow communication intermediate the throttling valve 13 and the inlet 19 of the compressor 10.
  • the liquid receiver 16 is connected to the evaporator outlet 15, and the gas phase outlet of the receiver 16 is connected to the counterflow heat exchanger 12.
  • the counterflow heat exchanger 12 is not absolutely necessary for the functioning of the device but improves its efficiency, in particular its rate of response to a capacity increase requirement It also serves to return oil to the compressor.
  • a liquid phase line from the receiver (16) (shown with broken line in Fig. 2) is connected to the suction line either before the counterflow heat exchanger (12) at 17 or after it at 18, or anywhere between these points.
  • the liquid flow i.e. refrigerant and oil, is controlled by a suitable conventional liquid flow restricting device (not shown in the figure). By allowing some excess liquid refrigerant to enter the vapour line, a liquid surplus at the evaporator outlet is obtained.
  • the storage segment of the working fluid circuit includes a receiver 22 integrated in the flow circuit between a valve 21 and the throttling valve 13.
  • the other components 10-14 of the flow circuit are identical to the components of the previous embodiment, although the heat exchanger 12 can be omitted without any great consequence.
  • the pressure in the receiver 22 is kept intermediate the high-side and low-side pressures of the flow circuit
  • the storage segment of the working fluid circuit includes a special receiver 25, where the pressure is kept between the high-side pressure and the low-side pressure of the flow circuit,
  • the storage segment further consists of the valves 23 and 24 which are connected to the high pressure and low pressure part of the flow circuit respectively.
  • the refrigerant is compressed to a suitable supercritical pressure in the compressor 10, the compressor outlet 20 is shown as state “a” in Fig. 5.
  • the refrigerant is circulated through the heat exchanger 11 where it is cooled to state "b", giving off heat to a suitable cooling agent e.g. cooling air or water.
  • a suitable cooling agent e.g. cooling air or water.
  • the refrigerant can be further cooled to state “c" in the counterflow heat exchanger 12, before throttling to state "d".
  • a two-phase gas/liquid mixture is formed, shown as state “d” in Fig. 3.
  • the refrigerant absorbs heat in the evaporator 14 by evaporation of the liquid phase.
  • the refrigerant vapour can be superheated in the counterflow heat exchanger 12 to state “f” before it enters the compressor inlet 19, making the cycle complete.
  • the evaporator outlet condition "e” will be in the two-phase region due to the liquid surplus at the evaporator outlet.
  • Modulation of the trans-critical cycle device capacity is accomplished by varying the refrigerant state at the evaporator inlet, i.e. point "d” in Fig. 5.
  • the refrigerating capacity per unit of refrigerant mass flow corresponds to the enthalpy difference between state "d” and state "e”. This enthalpy difference is found as a horizontal distance in the enthalpy-pressure diagram, Fig. 5.
  • Throttling is a constant enthalpy process, thus the enthalpy in point “d” is equal to the enthalpy in point "c".
  • the refrigerating capacity (in kW) at constant refrigerant mass flow can be controlled by varying the enthalpy at point "c".
  • the high-pressure single-phase refrigerant vapour is not condensed but reduced in temperature in the heat exchanger 11.
  • the terminal temperature of the refrigerant in the heat exchanger (point "b") will be some degrees above the entering cooling air or water temperature, if counterflow is used.
  • the high-pressure vapour can then be cooled a few degrees lower, to point "c", in the counterflow heat exchanger 12.
  • the result is, however, that at constant cooling air or water inlet temperature, the temperature at point "c" will be mainly constant, independent of the pressure level in the high side.
  • modulation of device capacity is accomplished by varying the pressure in the highside, while the temperature in point "c" is mainly constant.
  • the curvature of the isotherms near the critical point result in a variation of enthalpy with pressure, as shown in Fig. 5.
  • the figure shows a reference cycle (a-b-c-d-e-f), a cycle with reduced capacity due to reduced high side pressure (a'-b'-c'-d'-e-f) and a cycle with increased capacity due to higher pressure in the high side (a"-b"-c"-d"-e-f).
  • the evaporator pressure is assumed to be constant.
  • the pressure in the high-pressure side is independent of temperature, because it is filed with a single phase fluid.
  • the refrigerant mass in the high side is increased by temporarily reducing the opening of the throttling valve 13. Due to the incidentally reduced refrigerant flow to the evaporator, the excess liquid fraction at the evaporator outlet (15) will be reduced.
  • the liquid refrigerant flow from the receiver 16 into the suction line is however constant Consequently, the balance between the liquid flow entering and leaving the receiver 16 is shifted, resulting in a net reduction in receiver liquid content and a corresponding accumulation of refrigerant in the high pressure side of the flow circuit.
  • Opening of the throttling valve 13 will increase the excess liquid fraction at the evaporator outlet 15, because the evaporated amount of refrigerant is mainly constant The difference between this liquid flow entering the receiver and the liquid flow from the receiver into the suction line, will accumulate. The result is a net transport of refrigerant charge from the high side to the low side of the flow circuit, with the reduction in the high side charge stored in liquid state in the receiver. By reducing the high-side charge and thereby pressure, the capacity of the device is reduced, until balance is found.
  • the refrigerant mass in the high side can be increased by simultaneously shutting the valve 21 and modulating the throttling valve 13 to provide the evaporator with sufficient liquid flow. This will reduce the refrigerant flow from the high side into the receiver through valve 21, while refrigerant mass is transferred from the low side to the high side by the compressor.
  • Reduction of high-side charge is obtained by opening the valve 21 while keeping the flow through the throttling valve 13 mainly constant. This will transfer mass from the highside of the flow circuit to the receiver 22.
  • the refrigerant mass in the high side can be increased by opening the valve 24 and simultaneously reducing the flow through the throttling valve 13.
  • refrigerant charge is accumulated in the high-pressure side due to reduced flow through the throttling valve 13.
  • Sufficient liquid flow to the evaporator is obtained by opening the valve 24.
  • a reduction in the high side charge can be accomplished by opening the valve 23 to transfer some refrigerant charge from the high side to the receiver. Capacity control of the device is thus accomplished by modulation of the valves 23 and 24, and simultaneously operating the throttling valve 13.
  • the preferred embodiment as indicated in fig. 2 has the advantage of simplicity, with capacity control by operation of one valve only. Furthermore, the trans-critical vapour compression cycle device built according to this embodiment has a certain self-regulating capability by adapting to changes in cooling load through changes in liquid content in the receiver 16, involving changes in highside charge and thus cooling capacity. In addition, the operation with liquid surplus at evaporator outlet gives favourable heat transfer characteristics.
  • the device of figure 3 has the advantage of simplified valve operation.
  • Valve 21 only regulates the pressure in the high side of the device, and the thrittling valve 13 only assures that the evaporator is fed sufficiently.
  • a conventional thermostatic valve can thus be used for throttling. Oil return to the compressor is easily achieved by allowing the refrigerant to flow through the receiver.
  • This embodiment however does not offer the capacity control function at high-side pressures below the critical pressure.
  • the volume of the receiver 22 must be relatively large since it is only operating between the discharge pressure and the liquid line pressure.
  • the device figure 4 has the advantage of operating as a conventional vapour compression cycle device, when it is running at stable conditions.
  • the valves 23 and 24, connecting the receiver 25 to the flow circuit, are activated only during capacity control. This embodiment requires use of three different valves during periods of capacity change.
  • Trans-critical vapour compression cycle devices built according to the described embodiments can be applied in several areas.
  • the technology is well suitable in small and medium-sized stationary and mobile air-conditioning units, small and medium-sized refrigerators/freezers and in smaller heat pump units.
  • One of the most promising applications is in automotive air-conditioning, where the present need for a new, non-CFC, lightweight and efficient alternative to R12-systems is urgent.
  • the laboratory test device uses water as heat source, i.e. the water is refrigerated by heat exchange with boiling CO 2 in the evaporator 14. Water is also used as cooling agent, being heated by CO 2 in the heat exchanger 11.
  • the test device includes a 61 ccm reciprocating compressor (10) and a receiver (16) with total volume of 4 liters.
  • the system also includes a counterflow heat exchanger (12) and liquid line connection from the receiver to point 17, as indicated in Fig. 2.
  • the throttling valve 13 is operated manually.
  • This example shows how control of refrigerating capacity is obtained by varying the position of the throttling valve 13, thereby varying the pressure in the high-side of the flow circuit.
  • the specific refrigerant enthalpy at the evaporator inlet is controlled, resulting in modulation of refrigerating capacity at constant mass flow.
  • the water inlet temperature to the evaporator 14 is kept constant at 20°C, and the water inlet temperature to the heat exchanger 11 is kept constant at 35°C. Water circulation is constant both in the evaporator 14 and the heat exchanger 11.
  • the compressor is running at constant speed.
  • Fig. 6 shows the variation of refrigerating capacity (Q), compressor shaft work (W), highside pressure (p H ), CO 2 mass flow (m), CO 2 temperature at evaporator outlet (t e ), CO 2 temperature at the outlet of heat exchanger 11 (t b ) and liquid level in the receiver (h) when the throttling valve 13 is operated as indicated at the top of the figure.
  • the adjustment of throttling valve position is the only manipulation.
  • capacity (Q) is easily controlled by operating the throttling valve (13). It is further clear from the figure that at stable conditions, the circulating mass flow of CO 2 (m) is mainly constant and independent of the cooling capacity. The CO 2 temperature at the outlet of heat exchanger 11 (t b ) is also mainly constant. The graphs show that the variation of capacity is a result of varying high side pressure (p H ) only.
  • the transient period during capacity increase is not involving any significant superheating at the evaporator outlet, i.e. only small fluctuations in t e .
  • Table 1 shows results from tests run at different water inlet temperature to heat exchanger 11 (t w ).
  • the water inlet temperature to the evaporator is kept constant at 20°C, and the compressor is running at constant speed.
  • the cooling capacity can be kept mainly constant when the ambient temperature is rising, by increasing the high side pressure.
  • the refrigerant mass flow is mainly constant, as shown.
  • Increased high-side pressures involve a reduction in receiver liquid content, as indicated by the liquid level readings.
  • Table 1 Inlet temperature (t w ) 35.1 45.9 57.3 °C Refrigerating capacity (Q) 2.4 2.2 2.2 kW High side pressure (p H ) 84.9 94.3 114.1 bar
  • Mass flow 0.026 0.024 0.020 kg/s Liquid level (h) 171 166 115 mm
  • Fig. 8 is a graphic representation of trans critical cycles in the entropy/temperature diagram. The cycles shown in the diagram are based on measurements on the laboratory test device, during operation at five different high-side pressures. The evaporator pressure is kept constant. refrigerant is CO 2 .
  • the diagram gives a good impression of the capacity control principle, indicating the changes in specific enthalpy (h) at evaporator inlet caused by variation of the high-side pressure (p).

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Chemical & Material Sciences (AREA)
  • Compression-Type Refrigeration Machines With Reversible Cycles (AREA)
  • Devices That Are Associated With Refrigeration Equipment (AREA)
  • Heating, Cooling, Or Curing Plastics Or The Like In General (AREA)
  • Air-Conditioning For Vehicles (AREA)
  • Treatments Of Macromolecular Shaped Articles (AREA)
  • Common Detailed Techniques For Electron Tubes Or Discharge Tubes (AREA)
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  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)

Claims (3)

  1. Verfahren zum Betreiben eines Dampfkompressionskreises mit einem Kompressor (10), einem Kühler (11), einer Drosseleinrichtung (13) und einem Verdampfer (14), die seriell miteinander verbunden sind, um einen integralen geschlossenen Kreis zu bilden, der mit überkritischem Druck auf der Hochdruckseite des Kreises arbeitet, wobei der Druck auf der Hochdruckseite durch Veränderung der jeweiligen Kältemittelfüllung auf der Hochdruckseite des Kreises durch Veränderung des Inhalts eines in dem Kreis angeordneten Kältemittel-Pufferbehälters reguliert wird, wobei der Druck durch Verringern des Inhalts erhöht wird, und umgekehrt, wodurch die spezifische Kapazität des Kreises beeinflußt wird, und wobei die Regulierung des überkritschen Drucks durch Veränderung des Flüssigkeitsinhalts eines Niederdruckkältemittelbehälters (16) ausgeführt wird, der zwischen dem Verdampfer (14) und dem Kompressor (10) liegt, und zwar unter Verwendung nur der Drosseleinrichtung (13) als Steuereinrichtung.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der Zustand des Verdampferauslasses als eine Zwei-Phasen-Mischung von Dampf und Flüssigkeit gehalten wird, und zwar unter Schaffung eines Flüssigkeitsüberschusses an dem Niederdruckeinlaß eines zusätzlichen Wärmetauschers (12), wo das Niederdruckkältemittel durch Wärme von dem Hochdruckkältemittel vor dem Einlaß in den Kompressor Verdampfung und Überhitzung unterworfen wird.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß das Kältemittel Kohlendioxid ist.
EP89910211A 1989-01-09 1989-09-06 Verfahren zum betrieb eines kaltdampfprozesses unter trans- oder überkritischen bedingungen Expired - Lifetime EP0424474B2 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
NO890076A NO890076D0 (no) 1989-01-09 1989-01-09 Luftkondisjonering.
NO890076 1989-01-09
PCT/NO1989/000089 WO1990007683A1 (en) 1989-01-09 1989-09-06 Trans-critical vapour compression cycle device

Publications (3)

Publication Number Publication Date
EP0424474A1 EP0424474A1 (de) 1991-05-02
EP0424474B1 EP0424474B1 (de) 1993-08-04
EP0424474B2 true EP0424474B2 (de) 1997-11-19

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EP (1) EP0424474B2 (de)
JP (1) JPH0718602B2 (de)
KR (1) KR0126550B1 (de)
DE (2) DE68908181T3 (de)
DK (1) DK167985B1 (de)
NO (2) NO890076D0 (de)
PL (1) PL285966A1 (de)
RU (1) RU2039914C1 (de)
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EP0424474B1 (de) 1993-08-04
DK214690A (da) 1990-11-06
KR0126550B1 (ko) 1998-04-03
RU2039914C1 (ru) 1995-07-20
KR910700437A (ko) 1991-03-15
DE68908181T2 (de) 1994-04-14
DK214690D0 (da) 1990-09-07
PL285966A1 (en) 1991-03-25
JPH0718602B2 (ja) 1995-03-06
NO903903L (no) 1990-09-07
NO171810C (no) 1993-05-05
JPH03503206A (ja) 1991-07-18
EP0424474A1 (de) 1991-05-02
DK167985B1 (da) 1994-01-10
WO1990007683A1 (en) 1990-07-12
NO171810B (no) 1993-01-25
DE68908181D1 (de) 1993-09-09
DE68908181T4 (de) 1995-06-14
NO903903D0 (no) 1990-09-07
DE68908181T3 (de) 1998-06-18
UA27758C2 (uk) 2000-10-16
NO890076D0 (no) 1989-01-09

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