EP0195704B1 - Procédé de transfert de chaleur d'un fluide chaud à un fluide froid utilisant un fluide mixte comme agent caloporteur - Google Patents

Procédé de transfert de chaleur d'un fluide chaud à un fluide froid utilisant un fluide mixte comme agent caloporteur Download PDF

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Publication number
EP0195704B1
EP0195704B1 EP86400439A EP86400439A EP0195704B1 EP 0195704 B1 EP0195704 B1 EP 0195704B1 EP 86400439 A EP86400439 A EP 86400439A EP 86400439 A EP86400439 A EP 86400439A EP 0195704 B1 EP0195704 B1 EP 0195704B1
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EP
European Patent Office
Prior art keywords
fluid
heat
exchange
zone
exchange zone
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EP86400439A
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German (de)
English (en)
French (fr)
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EP0195704A1 (fr
Inventor
Alexandre Rojey
Alain Grehier
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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Priority to AT86400439T priority Critical patent/ATE33710T1/de
Publication of EP0195704A1 publication Critical patent/EP0195704A1/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F1/00—Tubular elements; Assemblies of tubular elements
    • F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
    • F28F1/12—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element
    • F28F1/24—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element and extending transversely
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
    • F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
    • F28D15/0266—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with separate evaporating and condensing chambers connected by at least one conduit; Loop-type heat pipes; with multiple or common evaporating or condensing chambers

Definitions

  • the purpose of the process according to the invention is to allow the transfer of heat from a hot fluid (A) to a cold fluid (B), and more particularly to allow the recovery of available heat from a hot fluid to transmit it to a cold fluid that needs to be heated.
  • This system includes an evaporator, a condenser and a central collector connected together by a circuit forming a loop ( Figure 2 of this patent).
  • the fluid leaving the evaporator is mixed in the central manifold with the fluid leaving the condenser, which results in the temperature of the fluid leaving the evaporator being lowered while the temperature of the fluid leaving the condenser is increased, thus the inlet temperatures of the evaporator and the condenser are respectively higher and lower than those of the outlet of the condenser and the evaporator.
  • US-A-4216903 describes a heat exchange system comprising an exchange loop, using as heat transfer fluid, for example, a halogenated hydrocarbon or a mixture of halogenated hydrocarbons.
  • the exchange of heat with an external fluid at the level of the condenser, making it possible to heat water, takes place globally against the current, while the heat exchange at the level of the condenser, making it possible to heat air, generally takes place at cross currents and the exchange of heat with an external fluid at the level of the evaporator takes place generally at cocurrent.
  • the system comprises a liquid coolant reserve located between the outlet of the condenser and the inlet of the evaporator and at least one U-shaped tube, the highest part of which is located at the highest level of the evaporator, which allows the direction of circulation of the heat transfer fluid to be imposed.
  • non-azeotropic mixtures such as for example those described in patent application EP-A-57120, in the system described above will not allow the system to be able to respond correctly to a variation in inlet temperature of the external fluids and / or a variation in the flow rate of these fluids.
  • non-azeotropic mixtures for a compression heat pump, comprising means of compression, condensation, expansion, evaporation and a reserve of liquid located at the outlet of the evaporation means, said liquid reserve being equipped with a “J” tube comprising a capillary opening, said tube allowing the reintroduction of the liquid working fluid into the active circuit of the heat pump, when as a result of a change in the external conditions the heaviest component of the working fluid has accumulated in the reserve, following the cooperation of the preset expansion means for a given modification of the external conditions.
  • One of the objects of the invention is to describe a process allowing a recovery rate of high heat without mechanical energy consumption and which can be used even at low temperatures without the risk of freezing provided you choose a suitable heat transfer fluid.
  • the invention describes a method of transferring heat from a hot fluid to a cold fluid which makes it possible to be able to work with partial recovery of the ranges of evolution of the temperature of the hot fluid and of the cold fluid, therefore with better heat recovery rate, as well as being able to work with relatively large variations either of the inlet temperatures of the hot and / or cold fluids, or of the flow rates of said fluids.
  • the heat transfer agent evaporates at least in part and leaves in the gaseous state the exchange zone (I) by its hottest end (that which is closest to the entry point (s) of the fluid (A)) to pass into the accumulation zone and reach the exchange zone (II) at the end closest to the ) fluid outlet point (s) (B).
  • zone (II) the gaseous heat transfer fluid gradually condenses in whole or in part, yielding its heat of condensation to the fluid (B).
  • the condensed heat transfer fluid leaves in the liquid state, by the end of the zone (II) closest to the point (s) of entry of the fluid (B), and descends by gravity towards the zone (I) where it enters through the end closest to the point (s) of fluid outlet (A).
  • the circuit is said to be substantially isobaric due to the fact that it includes neither compression zone nor expansion zone, the small pressure differences observed at various points of the circuit resulting mainly from pressure drops in the circuit.
  • An essential characteristic of the method according to the invention resides in the fact that no mechanical device is necessary, the transfer of the mixture between the exchange zones I and II taking place naturally by itself, under the sole effect of the heat transfers in exchange zones 1 and II and differences in density between the vapor phase and the liquid phase of the heat transfer fluid. This characteristic makes it possible to easily produce a sealed circuit without the risk of leakage of the mixture and to avoid maintenance and reliability problems linked to the use of a compressor or a pump.
  • FIG. 1 represents a first embodiment not in accordance with the invention comprising horizontal heat exchangers.
  • FIG. 2 represents an embodiment of the invention in which the exchange zones I and II are formed by heat exchangers generally inclined with respect to the horizontal. This embodiment allows easier starting of the process.
  • Figures 3 and 4 show embodiments similar to those of Figures 1 and 2. These embodiments comprising a system (11) for imposing a direction of flow on the heat transfer fluid and possibly limit and / or regulate the flow of the liquid phase.
  • the embodiment of Figure 3 comprising horizontal heat exchangers is not in accordance with the invention.
  • Figures 5 and 6 show one of the systems (11) capable of being used to impose the direction of circulation of the heat transfer fluid and possibly to limit and / or regulate the flow of the liquid phase.
  • FIG. 7 illustrates the application of the method of the invention to the air conditioning of premises, for example computer premises; for reasons of simplification of the diagram the reserve R has not been shown in this figure.
  • FIGS 8 to 11 illustrate the devices for implementing the method of the invention.
  • a first exemplary embodiment of the method of the invention is shown diagrammatically in FIG. 2.
  • the non-azeotropic mixture which circulates in the continuous duct forming a looped circuit represented in FIG. 2 arrives in the liquid state by the duct 1 at the end 7 of the exchange zone I called “evaporator” in which it is put into heat exchange relation by indirect contact generally against the current with a first external fluid which arrives via the conduit 2 at a temperature higher than that of beginning of vaporization of said non-azeotropic mixture and leaves via line 3; said non-azeotropic mixture leaving the exchange zone I via its end 8 passes into a reserve (R), of liquid phase, placed at the outlet of the evaporator and passes into the conduit 4 connecting the reserve (R) to the end 9 of the exchange zone II.
  • R reserve
  • the vapor phase of the non-azeotropic mixture obtained at the end 8 of the exchange zone I passes into the reserve (R) and arrives via the conduit 4 at the end 9 of the exchange zone II, in which the said mixture is put into heat exchange relation by indirect contact generally against the current with a second external fluid which arrives via line 5 at a temperature lower than that of the start of condensation of said non-azeotropic mixture and leaves via line 6; said non-azeotropic mixture leaving the exchange zone II via its end 10 in the conduit 1 connecting the end 10 of the exchange zone II to the end 7 of the exchange zone 1.
  • the exchange zones 1 and II are generally inclined relative to the horizontal.
  • the end 7 of the exchange zone I into which the non-azeotropic mixture enters, in the liquid state, is at a level substantially lower than the level of the end 8 of said zone through which said non-azeotropic mixture exits at less partially vaporized.
  • said non-azeotropic mixture penetrating into the exchange zone 1 at the end 7 rises generally continuously up to the level of the end 8; the slope of this exchange zone can be generally constant.
  • the end 9 of the exchange zone II into which the vapor phase of the non-azeotropic mixture penetrates is at a level substantially higher than the end 10 of said zone through which said non-azeotropic mixture at least partially condensed exits.
  • the vapor phase of the non-azeotropic mixture entering the exchange zone II at the end 9 generally descends continuously to the level of the end 10; the slope of this exchange zone can be generally constant; said slope (tangent of the angle formed by the axis of the exchange zone with the horizontal plane) being before approximately 0.01 to approximately 1.75 and preferably approximately 0.1 to 1.
  • non-azeotropic mixture and of the reserve thus allows the adaptation of the difference, bubble temperature-dew temperature, to the external conditions while retaining the advantage of ensuring the exchange of heat by latent heat: all evaporation takes place in the evaporator.
  • halogenated fluids R11 (CCI3F) and R12 (CCI 2 F 2 ) the respective specific heats of the gases are, at 30 ° C, 565 J / kg - K for R11 and 607 J / kg ⁇ K for R12 and the latent heats of vaporization of liquids are, at 30 ° C, 177,970 J / kg for R11 and 135,020 J / kg for R12, i.e. for a thermal difference of 10 ° C a mass capacity of heat transport between 22 and 31.5 times lower by sensible heat.
  • the operation of the process shown diagrammatically in FIGS. 3 and 4 is generally the same as that described above in relation to FIGS. 1 and 2.
  • the system (11) the other elements and arrangements of FIGS. 3 and 4 correspond respectively to the elements and arrangements of FIGS. 1 and 2.
  • the system (11) can for example be a valve made up of a device as shown diagrammatically in FIG. 5 or in FIG.
  • the device represented in FIG. 5 or in FIG. 6 comprises a float 12 resting on a seat 15, said float having a density lower than that of the condensate coming from the exchange zone II, said condensate flowing through the pipe 1 Said condensate cannot flow below the valve if the liquid level 14 is too low to exert on the float a sufficient Archimedes thrust to cause said float to rise due to the contact of said float on the seat 15 which creates the obturation of the duct 1 (this is the case shown in Figure 5).
  • the level 14 of the liquid rises and reaches a height such that the buoyancy exerted on the float 12 is sufficient to cause said float to rise, which does not resting more on its seat 15, allows the condensate to pass through the pipe 1, towards the exchange zone 1 (this is the case shown in FIG. 6). If the flow rate of the condensate from the exchange zone II is greater than the flow flow in the pipe 1 towards the exchange zone 1, the level 14 of the liquid rises and the float 12 also rises up to at the stop 13 which prevents said float from continuing to rise, but is arranged in such a way that it allows the level 14 of the liquid to continue its rise in line 1.
  • the mass of the float 12 will for example be greater than or equal to a value such that it is sufficient, without a liquid buffer in the valve 11, to oppose the passage of the non-azeotropic mixture from the exchange zone II in the zone of exchange I.
  • the height separating the level corresponding to the range of the float 12 on its seat 15 from the minimum liquid level 14 corresponding to the start of lifting of the float 12 will be such that the hydrostatic pressure of the condensate column between these two levels is sufficient to s '' opposing the passage of the non-azeotropic mixture from the exchange zone II into the exchange zone I.
  • the choice of mass and other characteristics of the float 12 depends in particular on the choice of the non-azeotropic mixture and in particular its density.
  • a system (11) such as that shown in FIGS. 5 and 6 is particularly well suited to the case where the transfer of heat between the relatively hot fluid (A) and the relatively cold fluid (B) has a or several transient regimes, said system (11) additionally ensuring, in this case, a certain regulation of the circulation of the heat transfer fluid.
  • the system (11) must be located at a level such that, before the process is put into operation, the hydrostatic pressure of the column of liquid existing at rest and / or the mass of the float is sufficient to oppose during from the start to the passage of the non-azeotropic mixture from the exchange zone (I) to the exchange zone (II) via line 1 (see Figure 4), that is to say to impose the direction circulation of the heat transfer fluid.
  • the non-azeotropic mixture arrives in the liquid state via the pipe 1 and enters the exchange zone 1 via its end 7.
  • the mixture is gradually vaporized, at least in part as it progresses between the ends 7 and 8 of the exchange zone I, with a rise in temperature which corresponds at least in part to the vaporization interval of said mixed.
  • the temperature of the mixture can change according to a temperature profile parallel to the change in temperature of the external fluid which cools between inlet 2 and outlet 3 of the exchange zone I.
  • the mixture forming the heat transfer fluid will advantageously be chosen so that the ratio delta T / delta T 'of the vaporization interval (delta T) of said heat transfer fluid to the temperature variation interval (delta T') of the relatively hot fluid (A) circulating in the exchange zone (1) either from 0.6: 1 to 1.5: 1 and preferably from 0.8: 1 to 1.2: 1.
  • the exchange battery will preferably be designed to allow a mixed exchange mode against the current / cross currents.
  • the vapor phase of non-azeotropic mixture obtained at the end 8 of the exchange zone I tends to move from bottom to top, due to its relatively low density; it crosses the reserve (R) and passes through the conduit 4 to reach the end 9 of the exchange zone II in which the non-azeotropic mixture is gradually condensed at least in part, as it progresses between the ends 9 and 10 of the exchange zone II; with a lowering of temperature which corresponds at least in part to the condensation interval of said mixture.
  • the entire circuit is substantially isobaric, the pressure variations being only linked to the pressure losses due to the circulation of the mixture and induced by the reserve (R), and / or induced by the presence of the system (11).
  • the condensation interval is the same as the vaporization interval and during the condensation stage the mixture follows in the opposite direction (lowering instead of raising the temperature) an evolution substantially identical to the evolution temperature monitored during the vaporization step.
  • the mixture cools while the external fluid heats up. It is also advantageous to carry out this exchange under conditions as close as possible to the exchange against the current.
  • the non-azeotropic mixture used must comprise at least two constituents which do not form an azeotrope therebetween, characterized by boiling temperatures differing by at least 15 ° C (under working pressure) and preferably by at least 30 ° C.
  • Each of said constituents being present in a proportion of at least 5% (for example 5 to 95% and 95 to 5% in the case of two constituents) in moles and preferably at least 10% in moles.
  • the mixtures used can be mixtures of two, three (or more) constituents (separate chemical compounds).
  • At least one of the constituents of the mixture can be a hydrocarbon, the molecule of which comprises, for example, from 3 to 8 carbon atoms, such as propane, normal butane, isobutane, normal pentane, isopentane, neopentane , normal hexane, isohexane, normal heptane, isoheptane, normal octane and isooctane as well as an aromatic hydrocarbon such as benzene and toluene or a cyclic hydrocarbon such as cyclopentane and cyclohexane.
  • a hydrocarbon the molecule of which comprises, for example, from 3 to 8 carbon atoms, such as propane, normal butane, isobutane, normal pentane, isopentane, neopentane , normal hexane
  • the mixture used may contain a halogenated fluid of the “freon” type (CFC) or be formed by a mixture of halogenated fluids of the “freon” type (CFC); these fluids include trifluoromethane CHF 3 (R23), chlorotrifluoromethane CCIF 3 (R13), trifluorobromomethane CF 3 Br (R13B1), chlorodifluoromethane CHClF 2 (R22), chloropentafluoroethane CCIF 1 -CF 3 ( R115), dichlorodifluoromethane CCI 2 F 2 (R12), difluoroethane CH 3 CHF 2 (R152a) CH 3 chlorodifluoroethane -CClF 2 (R142b), dichlorotetrafluoroethane CCIF 2 -CCIF 2 (R114), dichlorofluoromethane CHCl 2 F (R21), trichlorofluoromethane CC
  • mixtures comprising water and at least one second component miscible with water such as mixtures formed of water and ammonia, mixtures formed of water and an amine such as methylamine or ethylamine, mixtures formed from water and a ketone such as acetone.
  • non-azeotropic mixtures of particular composition so that the vaporization / condensation interval is adjusted according to the temperature intervals on the external fluids.
  • the advantages resulting from the choice of these compositions are effective only if the said non-azeotropic mixture is associated with the use of the generally counter-current exchange modes.
  • the exchange zone I through which the hot fluid passes is located below the exchange zone II through which the cold fluid passes. Under these conditions, the condensed liquid phase at the outlet of the exchange zone II flows by gravity to the exchange zone 1.
  • An important criterion for selecting the non-azeotropic mixture will be the density of the liquid phase in the duct 1 .
  • the exchange zones I and II generally consist of exchangers of the conventional type in which the heat exchanges are carried out generally against the current.
  • Heat exchange devices for implementing the method according to the invention, in particular those relating to heat exchange between two gas streams, one relatively hot in the exchange zone (I) and the other relatively cold in the exchange zone (II) comprise in each of the zones at least one exchanger element making it possible to carry out a heat exchange generally against the current, the said exchanger element (s) being advantageously formed by at least one hollow element or tube, advantageously provided with fins; the non-azeotropic mixture forming the working fluid being at least partly vaporized in said exchange zone (I) formed by at least said hollow element or tube and preferably formed by a set of hollow elements or tubes, and said fluid being condensed in said exchange zone (II) formed by at least said hollow element or tube, the liquid phase obtained during said stage of condensation in said exchange zone (II) returning by at least one conduit or a junction connecting said exchange zones (I) and (II) by gravity to said exchange zone (I), the vapor formed in said zone (I) returning after having crossed the reserve (R) by at least a second conduit or
  • FIGS. 8 to 11 Various devices for implementing the invention are described below in conjunction with FIGS. 8 to 11.
  • the exchange zone 1 corresponding to the evaporator is located below the exchange zone II corresponding to the condenser, the circulation of the non-azeotropic mixture takes place overall from bottom to top in zone I and from top to bottom in zone II, while the circulation of the hot gas with which the mixture is put in heat exchange relation in zone I takes place from top to bottom and the circulation of the cold gas with which the mixture is put in heat exchange relation in zone II takes place from bottom to top so that the mixture and the gas circulate generally against current in the two exchange zones.
  • the left free end of the exchanger element located at the lowest level of zone I being connected to the left free end of the exchanger element located at the lowest level of zone II by a junction or conduit element 31 and the end left free of the exchanger element located at the highest level of zone I being connected to the end left free of the exchanger element located at the highest level of zone II by a junction element or conduit 30.
  • thermosyphon effect causes the circulation of the mixture in the exchange devices according to the direction indicated by the arrows in Figure 8.
  • FIG. 9 A device similar to that of FIG. 8 is represented in FIG. 9.
  • the reference numbers mentioned in FIG. 9 designate the same elements as in FIG. 8.
  • FIG. 9 designate the same elements as in FIG. 8.
  • said tubes have their longitudinal axes inclined with respect to each other and inclined with respect to the horizontal so that the end left free of the finned tube situated at the generally lowest level of zone I is at a level below that of the other end of said tube and the end left free of the tube situated at the generally lowest level of the zone II being at a level lower than that of the other end of said tube.
  • the ends left free of these two tubes 20 and 23 being interconnected by the junction tube 31.
  • the end left free of the tube located at the generally highest level of zone I being at a level higher than that of the other end of said tube and the end left free of the tube located at the generally highest level of zone It is at a level higher than that of the other end of said tube.
  • the ends left free of these two tubes 22 and 25 being interconnected by the junction tube 30.
  • FIGS. 10 and 11 Another example of a device for implementing the method according to the invention is shown in FIGS. 10 and 11.
  • the exchangers are batteries formed from plies which correspond as in the case of FIG. 10 ply by ply with an offset in the vertical direction between the set of layers forming the battery corresponding to the exchange zone 1 and to that corresponding to the exchange zone II.
  • Each of said plies can, like the ply 40 shown in Figure 10, for example consist of a single bent tube, as shown schematically in Figure 10, so that the linear sections 41 of said tube disposed between the elbows 43 and 44 , and the extreme linear sections 42 and 56 are approximately parallel, said linear sections 42 and 56 being connected to sections 41 by the elbows 43, said linear sections being approximately of the same length and their longitudinal axes being approximately in the same horizontal plane.
  • the approximately horizontal planes corresponding to each of the layers laid out in each of zones I and II are preferably substantially equidistant and each layer of zone 1 is connected to a homologous layer of zone II situated on a substantially horizontal plane lying at a level generally greater than the level of the substantially horizontal plane of said ply of zone I.
  • the connection between the tube constituting a ply of zone I and the tube constituting the homologous ply of zone It is effected by communication of the linear sections located at the ends of each of the two homologous plies, the longitudinal axes of said linear sections placed at the ends of each of the two homologous plies being preferably located two by two in the same vertical planes; this communication can for example be carried out continuously by the same tube or conduit constituting said layers.
  • the ply 40 of zone II is in communication with the ply 45 of zone I via the portions of tubes 46 and 47, all of the plies being contained in a box 48, the sheets of zone I being separated from the sheets of zone II by a wall 49 through which the parts of tubes pass (such as 46 and 47 connecting the sheets 40 and 45) which connect the pairs of homologous layers.
  • the tubes preferably constituting the layers as they are shown diagrammatically in FIG. 10 are preferably provided with external fins 50, as shown diagrammatically in the section along the axis AA (FIG. 1 OA), in order to develop the exchange surface between the gas and the walls of each of the exchanger elements.
  • the walls of the box 48 are advantageously arranged in such a way that the spaces left free around the sheets are reduced to the minimum possible, the vertical walls, parallel to the linear sections of the tubes constituting the sheets having openings allowing the horizontal passage of the hot gas in the zone I and cold gas in zone II; the paths of said gases in zones I and II being generally in the same direction but oriented in opposite directions.
  • the plies in zones I and II are plies inclined so that the linear portions 42 and 55 of the hottest tube of a ply, that is to say located near the entry hot air and cold air outlet, are located respectively at higher levels than the linear portions 56 and 57 of the coldest tube of the corresponding layers 40 and 45 located near the air outlet hot and cold air inlet.
  • the condenser placed in the exchange zone II comprises the generally horizontal layers 60, 61 and 62 similar or identical to those described in conjunction with FIG. 10, the extreme linear portions 63, 65 and 67 of which are located in the vicinity of the outlet of the cold air communicate with a vertical manifold 69, which can for example be a tube of sufficiently large diameter relative to the diameter of the exchanger tubes, and the extreme linear portions 64, 66 and 68 located in the vicinity of the cold air inlet communicate with a vertical manifold 70 which can also be, for example, a tube, for example identical to that forming the collector 69.
  • the diameter of these tubes is advantageously greater than or equal to 2 times and preferably at least 3 times the diameter of the tubes used for r create the exchangers.
  • the evaporator located in the exchange zone 1 comprises the plies 71, 72 and 73 having the same configuration as the plies described in connection with FIG. 10 but whose longitudinal axes of the tubes constituting them are placed in generally vertical planes.
  • the three plies 71, 72 and 73 are hydraulically connected "in series", the highest linear portion of the ply 73 located near the outlet of the relatively hot air being in communication with the lowest linear portion of the ply 72, said ply 72 being in communication by its highest linear portion with the lowest linear portion of ply 71 located near the inlet of the hot air.
  • the extreme plies 71 and 73 of zone I are connected respectively to the collectors 69 and 70, the highest linear portion 78 of the ply 71 communicating with the highest end 77 of the collector 69, and the lowest linear portion of the ply 73 communicating with the lowest end 74 of the manifold 70, said bottom end 74 being at a level sufficiently below the mean horizontal plane of the lowest ply 62 of zone II so that the upper level of the liquid formed by the condensates from the sheets in the zone It preferably does not reach, during operation, the level of the junction 75 of the sheet 62 with the collector 70 and the lowest linear portion 76 of the sheet 73 of zone 1 being situated at a level below the mean level of the plane of the ply 62 and below the level of the junction 75.
  • FIG. 11 A represents a section along the axis AA of the device shown in FIG. 11 in the case where the tubes of the sheets of zone II are provided with external fins 80.
  • the elements used for the production of the exchangers are advantageously tubes with an internal diameter of 4 to 50 mm and preferably from 6 to 30 mm, the distance between the approximately parallel planes of the layers is preferably between 20 and 300 mm and the fins (50, 80) can have any shape, they can be for example round, square or rectangular, the distance between the planes of two successive fins is advantageously from 1.8 to 25 mm.
  • the fins can also be helical, the pitch of the uniform or variable propeller preferably being from 1.8 to 25 mm.
  • the elements used for the production of the exchangers can also be hollow elements of square, rectangular or arbitrary section allowing the circulation of the working fluid and an efficient heat exchange with the external fluids.
  • the materials used to make the exchangers are generally copper, steel, aluminum or metal alloys; but we can also consider the use of plastic.
  • a person skilled in the art is able to foresee all necessary means to ensure the proper functioning of the installations and not shown in the figures, such as for example purging and emptying means, as well as to envisage various modifications of the devices described above allowing their optimal operation under the particular conditions of transfers to achieve.
  • the devices described above also include means for circulating the hot fluid (A) and means for circulating the cold fluid (B) such as for example fans when the two fluids are gases, in particular of the air.
  • the fluid (A) consists of water which passes through the exchange zone I; it enters via line 2 at an initial temperature of 40 ° C and is discharged through line 3, at a final temperature of 25 ° C (conditions 1).
  • the heat transfer fluid is a binary mixture consisting of 80% in moles of dichlorodifluoromethane R12 and 20% in moles of trichlorofluoromethane R11.
  • the fluid initially contained in the reserve (R) is a binary mixture consisting of R12 and R11 of respective concentration in moles 52% and 48%.
  • the mixture is vaporized in the transfer zone I, by exchange against the current with the fluid (A); it enters the exchanger, at the bottom of the pipe 1, at a temperature of 20 ° C, under a pressure of 4.82 bars; it is completely vaporized and leaves the exchange zone (I) at a temperature of 35 ° C, under a pressure of 4.72 bars passes into the reserve and then into the pipe 4.
  • the pressure drops and the thermal leaks of the vapor phase along the pipe 4 are neglected; the mixture, suggested in the example, is then condensed between 35 ° C and 20 ° C, bubble temperature, corresponding to a pressure of 4.82 bars.
  • the condensation of the mixture is ensured by exchange against the current with the cold fluid (B), consisting of water; it enters through the tube 5 and exits the exchanger II through the tube 6; it is assumed to be warmed from 10 ° C to 25 ° C; the hydrostatic height required is 0.90 m, taking into account the density of the condensed liquid and the pressure losses of the fluid in the circuit.
  • the non-azeotropic mixture chosen for this example, can allow partial overlap between the temperature profiles of the fluids (A) and (B).
  • the fluid (A) changes and its inlet temperature through line 2 is established at 35 ° C, its outlet temperature through line 3 at 23.2 ° C (conditions 2).
  • the composition of the gas mixture at the outlet of the reserve is in moles of 84.5% of R12 and 15.5% of R11, the composition of the mixture in the reserve is of 47% in R12 and 53% in R11 (molar).
  • the mixture enters the exchange zone I at 18.2 ° C under a pressure of 4.55 bars and leaves completely vaporized at a temperature of 30 ° C under a pressure of 4.50 bars.
  • the mixture is then condensed between 30 ° C and 18.2 ° C, bubble temperature corresponding to a pressure of 4.55 bars.
  • the condensation of the mixture is ensured by exchange against the current with the cold fluid (B), consisting of water, which is assumed to be heated from 13.2 ° C to 25 ° C; the hydrostatic height required is in this case 0.45 m.
  • the evaporator outlet temperature is no longer sufficient to vaporize all the mixture in circulation: the non-vaporized part, richer in heavy component (R11) pours out then in the reserve, the concentration of heavy component (R11) of which increases from 48% to 53% in moles.
  • the vaporized mixture is enriched in light component (R12) which passes in molar percentage from 80% to 84.5%.
  • Data centers require a controlled temperature of around 18 ° C; generally, an air / air or water / air cold machine is used by removing the calories from the room to be conditioned, the condenser rejecting the heat on the terrace; the cold loop shown in Figure 7 then includes the evaporator (E,), the compressor (K), the condenser (E 2 ) and the regulator (D).
  • the evaporator (E 1 ) is placed in the computing center 17 which includes the computing units 16a, 16b and 16c.
  • FIG. 7 shows an outside temperature sensor (S), which controls, as a function of this temperature, the closing of two solenoid valves (EV,) and (EV z ) placed respectively at the outlet of the evaporator (E 1 ) and at the outlet of the condenser (E Z ); when the outside temperature falls below a chosen value, the solenoid valves (EV,) and (EV z ) controlled by the temperature probe (S) close, thus avoiding the compressor (K) and the expansion valve (D) via lines 18 and 19 respectively.
  • S outside temperature sensor
  • the air in the room to be conditioned is continuously cooled from 18 ° C to 8 ° C with a flow rate of 200 m 3 / h; the power taken from the evaporator (E 1 ) is 720 W and compensates for the thermal losses caused by the operation of the computers or computers.
  • the outside air will be heated, for example, from 5 ° C to 15 ° C; a non-azeotropic mixture of fluids will be selected to have a total evaporation and condensation interval of the order of 10 ° C; under the conditions of the example, this evaporation will take place between 6.5 ° and 16.5 ° C.
  • Conditions may change, for example, as follows, thanks to the judicious choice of fluid mixture and the reserve located downstream of the evaporator (outlet of the evaporator): the air in the room to be conditioned is continuously cooled from 18 ° C to 6 ° C with a flow rate of 200 m 3 / h; the power taken from the evaporator (E,) goes to 864 W. The outside air will then be heated, for example from 8 ° C to 20 ° C; the mixture will then evaporate between 7 and 19 ° C.
  • the mixture used is a binary or a ternary of CFCs chosen from the following usual fluids, for example: R23, R13, R31, R32, R115, R502, R22, R501, R12, R152a, R13 B1, R500, R142b, R133a, R114, R11, R216 or R113; more generally, the mixture will comprise at least two chlorofluorocarbon derivatives of methane or ethane, the molar concentration of each component will be at least 5%.
  • halogenated hydrocarbons have the advantage of having a density greater than that of water; in the process according to the invention, it is recommended to select a non-azeotropic mixture whose liquid density is greater than 1, preferably 1.2, in order to limit the size of the installation.
  • the heat exchanges are carried out according to a generally counter-current exchange mode; however, when the heat exchange is carried out with air, the realization of a pure countercurrent exchange mode is hardly feasible; in these cases, the use of exchange batteries allowing a mixed cross current / counter current exchange will be preferable.
  • the operating pressure of the system will preferably be higher than atmospheric pressure, in order to avoid the entry of air into the circuit. It will be less than 3 MPa (megapascals) and, preferably, between 0.1 and 1.5 M Pa absolute (1 to 15 bars absolute).
  • the two exchangers can be located at the same level.
  • the interface of the continuous liquid phase formed by condensation in zone II be located at a level higher than the level at the start of vaporization in zone I.
  • this level of liquid interface can be located inside the condenser, the liquid phase leaving sub-cooled from the condenser, which makes it possible to carry out a flow by gravity of the phase liquid from the condenser to the evaporator while the evaporator and the condenser are located at the same level.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Geometry (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Lubricants (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
EP86400439A 1985-03-08 1986-03-03 Procédé de transfert de chaleur d'un fluide chaud à un fluide froid utilisant un fluide mixte comme agent caloporteur Expired EP0195704B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT86400439T ATE33710T1 (de) 1985-03-08 1986-03-03 Verfahren zum waermeaustausch zwischen einer warmen und einer kalten fluessigkeit mittels einer gemischten fluessigkeit als waermetraeger.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8503410A FR2578638B1 (fr) 1985-03-08 1985-03-08 Procede de transfert de chaleur d'un fluide chaud a un fluide froid utilisant un fluide mixte comme agent caloporteur
FR8503410 1985-03-08

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Publication Number Publication Date
EP0195704A1 EP0195704A1 (fr) 1986-09-24
EP0195704B1 true EP0195704B1 (fr) 1988-04-20

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EP86400439A Expired EP0195704B1 (fr) 1985-03-08 1986-03-03 Procédé de transfert de chaleur d'un fluide chaud à un fluide froid utilisant un fluide mixte comme agent caloporteur

Country Status (6)

Country Link
US (1) US4771824A (ja)
EP (1) EP0195704B1 (ja)
JP (1) JPS61208490A (ja)
AT (1) ATE33710T1 (ja)
DE (1) DE3660140D1 (ja)
FR (1) FR2578638B1 (ja)

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Also Published As

Publication number Publication date
JPS61208490A (ja) 1986-09-16
DE3660140D1 (en) 1988-05-26
EP0195704A1 (fr) 1986-09-24
ATE33710T1 (de) 1988-05-15
FR2578638B1 (fr) 1989-08-18
US4771824A (en) 1988-09-20
FR2578638A1 (fr) 1986-09-12

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