EP0195704A1 - Verfahren zum Wärmeaustausch zwischen einer warmen und einer kalten Flüssigkeit mittels einer gemischten Flüssigkeit als Wärmeträger - Google Patents

Verfahren zum Wärmeaustausch zwischen einer warmen und einer kalten Flüssigkeit mittels einer gemischten Flüssigkeit als Wärmeträger Download PDF

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Publication number
EP0195704A1
EP0195704A1 EP86400439A EP86400439A EP0195704A1 EP 0195704 A1 EP0195704 A1 EP 0195704A1 EP 86400439 A EP86400439 A EP 86400439A EP 86400439 A EP86400439 A EP 86400439A EP 0195704 A1 EP0195704 A1 EP 0195704A1
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EP
European Patent Office
Prior art keywords
fluid
exchange
heat transfer
zone
transfer fluid
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Granted
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EP86400439A
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English (en)
French (fr)
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EP0195704B1 (de
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
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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 system comprises a reserve of liquid of the heat transfer fluid 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 situated at a level between the lowest level of the evaporator and the highest level of the evaporator, which makes it possible to impose the direction of circulation of the heat transfer fluid.
  • 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 external fluids and / or a variation in the flow rate of these fluids.
  • One of the objects of the invention is to describe a process allowing a high heat recovery rate without consumption of mechanical energy and which can be used even at low temperatures without carrying the risk of freezing provided that a fluid is chosen adapted coolant.
  • 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 the closest to the point (s) of entry of the fluid (A) to pass into the accumulation zone and reach the exchange zone (II) at the end closest to the outlet point (s) of the fluid (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 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 penetrates by l end closest to the outlet point (s) of the fluid (A).
  • the circuit is said to be substantially isobaric since it includes neither compression zone neither area expansion, the small pressure differences observed at various points in the circuit resulting mainly from pressure drops in the circuit
  • An essential characteristic of the process 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 I 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 A first exemplary embodiment of the method of the invention is shown diagrammatically in FIG. 1.
  • the non-azeotropic mixture which circulates in the continuous duct forming a looped circuit represented in FIG. 1 arrives at the state liquid through the conduit 1 at the end 7 of the exchange zone 1 called "evaporator" in which it is put in heat exchange relation by indirect contact generally against the current with a first external fluid which arrives by the conduit 2 at a temperature higher than that of the start of vaporization of said non-azeotropic mixture and leaves via line 3; said non-azeotropic mixture leaving the exchange zone 1 through its end 8 passes into a reserve (R), of liquid phase, placed at the outlet of the evaporator and passes through the conduit 4 connecting the reserve (R) to the end 9 of the If exchange zone.
  • R reserve
  • the vapor phase of the non-azeotropic mixture obtained at the end 8 of the exchange zone 1 passes into the reserve (R) and arrives via the conduit 4 at the end 9 of the exchange zone If, in which said mixture is brought into heat exchange relationship 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.
  • FIG. 2 A second embodiment of the process of the invention is shown diagrammatically in FIG. 2.
  • the operation of the process is generally similar to that described above for FIG. 1.
  • the exchange zones 1 and II are generally inclined with respect to the horizontal.
  • the end 7 of the exchange zone I into which the non-azeotropic mixture penetrates, in the liquid state, is at a level substantially lower than the end 8 of said zone through which said non-aseptic mixture exits.
  • azeotropic at least 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 leaves at least partially. condensed.
  • 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 advantageously from approximately 0.01 to approximately 1.75 and preferably from approximately 0.1 to 1.
  • non-azeotropic mixture and 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 - (CCI 3 F) 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 calorific transport between 22 and 31.5 times lower by sensible heat.
  • the operation of the process shown schematically in Figures 3 and 4 is broadly the same as that described above in relation to Figures 1 and 2. With the exception of the system (11) the other elements and arrangements of Figures 3 and 4 correspond respectively to the elements and arrangements of Figures 1 and 2.
  • the system (11) may for example be a valve made up of a device such as - shown diagrammatically in Figure 5 or in Figure 6, or for example a capillary type diaphragm creating a pressure drop associated with a liquid reserve creating a liquid buffer preventing rotation in the opposite direction of the non-azeotropic mixture.
  • the device shown in Figure 5 or in Figure 6 comprises a float 12 resting on a seat 15, said float having a density less than that of the condensate from the exchange zone II, said condensate flowing through the pipe 1 Said condensate cannot flow below the valve if the level of liquid 14 is too low to exert on the float an Archimedes thrust sufficient to cause pressure.
  • 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 exchange 1.
  • the height separating the level corresponding to the range of the float 12 on its seat 15 from the level of minimum liquid 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 oppose 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.
  • 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 3 or 4), that is to say to impose the direction of 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 1, with a rise in temperature which corresponds at least in part to the vaporization interval of said
  • 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 1.
  • 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 fluid relatively hot (A) circulating in the exchange zone (I) is 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 1 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 condensed progressively 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) a development substantially identical to the temperature evolution followed during the vaporization stage.
  • 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) by mole and preferably at least 10% by mole.
  • 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); among these fluids, there may be mentioned trifluoromethane CHF 3 (R23), chlorotrifluo-romethane CCIF 3 (R 1 3), trifluorobromomethane CF 3 Br (R13B1) 5 chlorodifluoro-romethane CHCIF 2 (R22), chloropentafluoroethane CCIF 2 -CF 3 - (R115), dichlorodifluoromethane CCl 2 F 2 (R12), difluoroethane CH 3 CHF 2 (R152a), chlorodifluoroethane CH 3 -CClF 2 (R142b), dichlorotetrafluoroethane CCIF 2 -CC 2 - (R114), dichlorofluoro-methane CHCI 2 F (R21
  • 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 only effective if the said non-azeotropic mixture is associated with the use of the generally counter-current modes of exchange.
  • the exchange zone 1 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 It 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 conduit 1.
  • the exchange zones and It 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 zone 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 working fluid being condensed in said exchange zone (II) formed by at least said hollow element or tube, the liquid phase obtained during said condensation step 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 - (1), the vapor formed in said zone (1) returning after having crossed the reserve (R) by at 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 1 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 the zone I is carried out from top to bottom and that the circulation of the cold gas with which the mixture is put in heat exchange relation in the zone takes place from bottom to top so that the mixture and the gas circulate generally against current in the two exchange zones.
  • exchanger 8 comprises a set of exchanger elements preferably formed by finned tubes of approximately equal length, arranged one under the other so that for each set of tubes corresponding to each of the zones their longitudinal axes are approximately parallel, located approximately in the same vertical plane and these exchanger elements 20, 21 and 22 of zone 1 on the one hand and 23, 24 and 25 of zone II on the other hand are hydraulically connected "in series" by approximately vertical joints or conduits, such as junctions 26 and 27 for the exchanger elements of zone 1 and junctions 28 and 29 for the exchanger elements of zone II.
  • the left free end of the exchanger element located at the lowest level of zone 1 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 1 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.
  • thermosiphon effect causes the circulation of the mixture in the exchange devices according to the direction indicated by the arrows in Figure 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 1 is at a level lower than that of l 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.
  • 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 sheets 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 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 1 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 zone 1 ply.
  • the connection between the tube constituting a ply of zone 1 and the tube constituting the homologous ply of zone II is effected by placing in communication 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 1 via the portions of tubes 46 and 47, all of the plies being contained in a box 48 , the plies of zone 1 being separated from the plies of zone II by a wall 49 through which pass the parts of tubes (such as 46 and 47 connecting the plies 40 and 45) which communicate the pairs of homologous plies.
  • the constituent tubes preferably the layers as they are shown schematically in Figure 10 are preferably provided with external fins 50, as shown diagrammatically in the section along the axis AA - ( Figure 10A), 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 so that the spaces left free around the layers are reduced to the minimum possible, the vertical walls, parallel to the linear sections of the tubes constituting the layers having openings allowing the horizontal passage of the hot gas in the zone 1 and cold gas in zone II; the paths of said gases in zones 1 and II being generally in the same direction but oriented in opposite directions.
  • a particularly advantageous and preferred arrangement according to the invention of the plies in zones 1 and It consists in producing inclined plies so that the linear protections 42 and 55 of the hottest tube of a ply, that is to say say located near the hot air inlet and the 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 at near the hot air outlet and the cold air inlet.
  • the condenser arranged in the exchange zone It comprises the generally horizontal layers 60, 61 and 62 similar or identical to those described in connection with FIG. 10, including the extreme linear portions 63, 65 and 67 located in the vicinity of the outlet of the cold air communicates with a vertical manifold 69, which can for example be a tube of sufficiently large diameter compared to the diameter of the tubes of the exchanger, and the extreme linear portions 64, 66 and 68 located in the vicinity of the inlet cold air communicates with a vertical collector 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 or equal to 2 times and preferably at least 3 times the diameter of the tubes used to make the exchangers.
  • the evaporator located in the exchange zone I 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 and the constituents 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 collector 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 of zone II 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 the area I being located at a level below the mean level of the plane of the sheet 62 and below the level of the junction 75.
  • FIG. 11A 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 of internal diameter from 4 to 50 mm and preferably of 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.
  • Those skilled in the art are able to provide all the means necessary for the smooth running 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 the transfers to be carried out.
  • 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 1; 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 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; the latter 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 profiles fluid temperature (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 expansion valve (D).
  • the evaporator E is placed in the computing center 17 which includes the computing units 16a, 16b and 16c.
  • FIG. 7 shows an outdoor temperature sensor (S), which controls, as a function of this temperature, the closing of two solenoid valves (EV,) and (EV 2 ) placed respectively at the outlet of the evaporator (E1) and at the condenser outlet - (E 2 ); when the outside temperature falls below a selected value, the solenoid valves (EV,) and (EV 2 ) controlled by the temperature probe (S) close, thus avoiding the compressor (K) and the expansion valve - (D) via lines 18 and 19 respectively.
  • S outdoor 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,) 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 range of the order of 10 ° C; under the conditions of the example, this evaporation will take place between 6.5 ° C and 16.5 ° C.
  • the conditions may change, for example, in the following way thanks to the judicious choice of the fluid mixture and to the reserve disposed downstream of the evaporator - (outlet of the evaporator): the air in the room to be conditioned is cooled by permanence from 18 ° C to 6 ° C with a flow rate of 200 m 3 / h; the power taken from the evaporator (E1) 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 common fluids, for example: R23, R13, R31, R32, R 115 , R 5 0 2 , R22, R 5 0 1 , R 1 2, R 152 a, R 13 B 1 , R 5 00, 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 MPa 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 is located at a level higher than the level of vaporization start in zone 1.
  • this level of liquid interface can be located inside from the condenser, the liquid phase leaving sub-cooled from the condenser, which allows gravity flow of the liquid phase 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 Verfahren zum Wärmeaustausch zwischen einer warmen und einer kalten Flüssigkeit mittels einer gemischten Flüssigkeit als Wärmeträger Expired EP0195704B1 (de)

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
FR8503410 1985-03-08
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

Publications (2)

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

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EP86400439A Expired EP0195704B1 (de) 1985-03-08 1986-03-03 Verfahren zum Wärmeaustausch zwischen einer warmen und einer kalten Flüssigkeit mittels einer gemischten Flüssigkeit als Wärmeträger

Country Status (6)

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

Cited By (3)

* Cited by examiner, † Cited by third party
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EP0335707A2 (de) * 1988-03-30 1989-10-04 Alcan International Limited Verfahren zur Uebertragung von Wärme zwischen flüssigen Prozessströmen
FR2642154A1 (fr) * 1989-01-25 1990-07-27 Const Aero Navales Procede pour le refroidissement d'un fluide chaud par un fluide froid sans surface d'echange commune en contact avec ces fluides et echangeur pour sa mise en oeuvre
FR2687464A1 (fr) * 1992-02-19 1993-08-20 Bernier Jacques Caloducs a melange zeotropique de fluides.

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DE10221639B4 (de) * 2002-05-15 2004-06-03 Siemens Ag Einrichtung der Supraleitungstechnik mit einem supraleitenden Magneten und einer Kälteeinheit
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US20090020263A1 (en) * 2006-01-26 2009-01-22 Akihiro Ohsawa Cooling Apparatus for Fluid
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DE102010033169A1 (de) * 2010-08-03 2012-02-09 Khs Gmbh Verfahren sowie Anlage zum Füllen von Behältern mit einem flüssigen Füllgut
FR2979981B1 (fr) * 2011-09-14 2016-09-09 Euro Heat Pipes Dispositif de transport de chaleur a pompage capillaire
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JP2012026723A (ja) * 2011-11-10 2012-02-09 Tai-Her Yang 自然サーモキャリアの熱作動で対流する放熱システム
US9117991B1 (en) 2012-02-10 2015-08-25 Flextronics Ap, Llc Use of flexible circuits incorporating a heat spreading layer and the rigidizing specific areas within such a construction by creating stiffening structures within said circuits by either folding, bending, forming or combinations thereof
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Publication number Priority date Publication date Assignee Title
EP0335707A2 (de) * 1988-03-30 1989-10-04 Alcan International Limited Verfahren zur Uebertragung von Wärme zwischen flüssigen Prozessströmen
EP0335707A3 (de) * 1988-03-30 1991-07-03 Alcan International Limited Verfahren zur Uebertragung von Wärme zwischen flüssigen Prozessströmen
FR2642154A1 (fr) * 1989-01-25 1990-07-27 Const Aero Navales Procede pour le refroidissement d'un fluide chaud par un fluide froid sans surface d'echange commune en contact avec ces fluides et echangeur pour sa mise en oeuvre
FR2687464A1 (fr) * 1992-02-19 1993-08-20 Bernier Jacques Caloducs a melange zeotropique de fluides.

Also Published As

Publication number Publication date
ATE33710T1 (de) 1988-05-15
FR2578638B1 (fr) 1989-08-18
FR2578638A1 (fr) 1986-09-12
US4771824A (en) 1988-09-20
JPS61208490A (ja) 1986-09-16
DE3660140D1 (en) 1988-05-26
EP0195704B1 (de) 1988-04-20

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