EP3555544B1 - Heat exchanger with a liquid/gas mixing device with improved channel geometry - Google Patents

Heat exchanger with a liquid/gas mixing device with improved channel geometry Download PDF

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Publication number
EP3555544B1
EP3555544B1 EP17822398.8A EP17822398A EP3555544B1 EP 3555544 B1 EP3555544 B1 EP 3555544B1 EP 17822398 A EP17822398 A EP 17822398A EP 3555544 B1 EP3555544 B1 EP 3555544B1
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EP
European Patent Office
Prior art keywords
channel
plate
mixing device
exchanger according
passages
Prior art date
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EP17822398.8A
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German (de)
French (fr)
Other versions
EP3555544A1 (en
Inventor
Philippe Grigoletto
Natacha Haik-Beraud
Sophie LAZZARINI
Jean-Marc Peyron
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP3555544A1 publication Critical patent/EP3555544A1/en
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/02—Header boxes; End plates
    • F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
    • F28F9/0263—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by varying the geometry or cross-section of header box
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • 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
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0062—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements
    • F28D9/0068—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements with means for changing flow direction of one heat exchange medium, e.g. using deflecting zones
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
    • F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/22—Arrangements for directing heat-exchange media into successive compartments, e.g. arrangements of guide plates
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0033—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for cryogenic applications
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F2250/00—Arrangements for modifying the flow of the heat exchange media, e.g. flow guiding means; Particular flow patterns
    • F28F2250/10—Particular pattern of flow of the heat exchange media
    • F28F2250/108—Particular pattern of flow of the heat exchange media with combined cross flow and parallel flow

Definitions

  • the present invention relates to a heat exchanger comprising series of passages for each of the fluids to be placed in a heat exchange relationship, the exchanger comprising at least one mixing device configured to distribute at least one two-phase liquid / gas mixture in a series of passages
  • An exchanger according to the preamble of claim 1 is known from the document FR 2 563 620 A1 .
  • the present invention can be applied to a heat exchanger which vaporizes at least one flow of liquid-gas mixture, in particular a flow of mixture with several constituents, for example a mixture of hydrocarbons, by heat exchange with at least one other fluid, for example natural gas.
  • the technology commonly used for an exchanger is that of brazed aluminum plate and fin exchangers, which make it possible to obtain very compact devices offering a large exchange surface.
  • These exchangers comprise plates between which are inserted heat exchange waves, formed of a succession of fins or wave legs, thus constituting a stack of vaporization passages and condensation passages, some intended to vaporize refrigerant and the like to condense a circulating gas. Heat exchange between fluids can take place with or without phase change.
  • the sizing of the exchanger is calculated by assuming a uniform distribution of the phases, and therefore a single end of vaporization temperature of the liquid phase, equal to the dew point temperature of the mixture.
  • the end of vaporization temperature will depend on the proportion of liquid phase and gas phase in the passages.
  • the temperature profile of the refrigerant will therefore vary according to the passages, or even vary within the same passage. Due to this non-uniform distribution, it may then happen that the circulating fluid (s) in exchange relation with the two-phase mixture have a temperature at the outlet of the exchanger higher than that expected, which consequently degrades the performance. of the heat exchanger.
  • the document FR-A-2563620 describes such an exchanger in which a grooved bar is inserted in the series of passages intended to channel the two-phase mixture.
  • This mixing device has separate inlets for a liquid phase and a gas phase opening into a common mixing volume provided with an outlet for distributing the liquid-gas mixture to the heat exchange zone.
  • the liquid phase supplying the mixing device is then inevitably in a heat exchange situation with the circulating fluid (s) circulating in the adjacent passages of the other series of passages. This can cause the start of vaporization of the liquid phase even within the corresponding inlets, thereby leading to an unequal distribution of the two phases of the mixture in certain passages of the series as well as in certain zones within the same passage.
  • one solution would be to install the mixing device in a zone of the exchanger in which no other fluid is circulating. It would then be necessary to place the mixing device at one end of the exchanger, free of any means of discharge or supply of fluid, which would require restructuring the exchanger as a whole and would necessarily lead to an increase in its size. In addition, such a solution does not allow the introduction of the two-phase mixture in the middle of the exchanger, which may be desirable in cases where the specificities of the process require it.
  • the object of the present invention is to resolve all or part of the above-mentioned problems, in particular by proposing a heat exchanger in which the distribution of the liquid and gas phases of a mixture is as uniform as possible, and this without complicating any excessively the structure of the exchanger, nor increase its size.
  • the present invention can be applied to a heat exchanger which vaporizes at least one flow of liquid-gas mixture, in particular a flow of mixture with several constituents, for example a mixture of hydrocarbons, by heat exchange with at least one. other fluid, for example natural gas.
  • natural gas refers to any composition containing hydrocarbons including at least methane. This includes a "crude” composition (prior to any treatment or washing), as well as any composition that has been partially, substantially or fully treated for the reduction and / or elimination of one or more compounds, including, but not limited to. limit, sulfur, carbon dioxide, water, mercury and some heavy and aromatic hydrocarbons.
  • FIGS. 1 and 2 illustrate a heat exchanger 1 according to an embodiment of the invention comprising a stack of plates 2a, 2b, 2c ... which extend in two dimensions, in a longitudinal direction z and a lateral direction y.
  • the plates 2a, 2b, 2c ... are arranged parallel one above the other with spacing and thus form a plurality of passages for fluids in indirect heat exchange relation via said plates.
  • the lateral direction is represented therein orthogonal to the longitudinal direction z and parallel to the plates 2a, 2b, 2c ....
  • each passage has a parallelepipedal and flat shape.
  • the gap between two successive plates is small compared to the length and width of each successive plate.
  • the exchanger 1 may include a number of plates greater than 20, or even greater than 100, defining between them a first series of passages 10 for channeling at least one refrigerant F1, and a second series of passages 20 (not visible on the Figure 1 ) to channel at least one circulating fluid F2, the flow of said fluids taking place generally in the longitudinal direction z.
  • the passages 10 of the first series can be arranged, in whole or in part, alternating or adjacent to all or part of the passages 20 of the second series.
  • the exchanger 1 comprises distribution and evacuation means 43, 52 configured to distribute the various fluids selectively in the passages 10, 20, as well as to evacuate said fluids from said passages 10, 20.
  • the sealing of the passages 10, 20 along the edges of the plates 2a, .. is generally ensured by lateral and longitudinal sealing strips 4 fixed to the plates 2a, ...
  • the lateral sealing strips 4 do not block off not completely the passages 10, 20 but advantageously leave fluid inlet and outlet openings located in the diagonally opposite corners of the passages.
  • the openings of the passages 10 of the first series are arranged in coincidence one above the other, while the openings of the passages 20 of the second series are arranged at the opposite corners.
  • the openings placed one above the other are united respectively in semi-tubular collectors 40, 45, 50, 55, through which the distribution and evacuation of the fluids take place.
  • the semi-tubular collectors 50, 45 are used for the introduction of fluids into the exchanger 1 and the semi-tubular collectors 40, 55 are used for the evacuation of these fluids out of the exchanger 1.
  • the supply manifold of one of the fluids and the discharge manifold of the other fluid are located at the same end of the exchanger, the fluids F1, F2 thus circulating in counter-current in exchanger 1.
  • the refrigerant and circulating fluids can also circulate in co-current, the means for supplying one of the fluids and the means for discharging the other fluid then being located at opposite ends of the 'exchanger 1.
  • the longitudinal direction is oriented vertically when the exchanger 1 is in operation.
  • the refrigerant F1 flows generally vertically and in the upward direction.
  • Other directions and direction of flow of the fluids F1, F2 can of course be envisaged, without departing from the scope of the present invention.
  • one or more refrigerants F1 and one or more circulating fluids F2 of different types can flow within passages 10, 20 of the first and second series of the same exchanger.
  • the distribution and evacuation means 43, 52 advantageously comprise distribution waves 44, 51, 54, arranged between two successive plates 2a, 2b, ... in the form of corrugated sheets, which extend from the openings d entry and exit.
  • the distribution waves 44, 51, 54 ensure the uniform distribution and the recovery of the fluids over the entire width of the passages 10, 20.
  • the passages 10, 20 advantageously comprise heat exchange structures arranged between the plates 2a, 2b, .... These structures have the function of increasing the heat exchange surface area of the exchanger.
  • the heat exchange structures are in contact with the fluids circulating in the passages and transfer heat flows by conduction to the adjacent plates, to which they can be fixed by brazing, which increases the mechanical resistance of the exchanger.
  • the heat exchange structures also have a function of spacers between the plates, in particular during assembly by brazing the exchanger and to prevent any deformation of the plates during the use of fluids under pressure. They also ensure the guidance of the fluid flows in the passages of the exchanger.
  • these structures comprise heat exchange waves 11 which advantageously extend along the width and the length of the passages 10, 20, parallel to the plates, in the extension of the distribution waves 44, 51, 54 along the length of the passages 10, 20.
  • the passages 10, 20 of the exchanger thus have a main part of their length constituting the actual heat exchange part, which is lined with a heat exchange structure, said main part being bordered by distribution parts furnished with distribution waves 44, 51, 54.
  • the Figure 1 illustrates a passage 10 of the first series 1 configured to distribute a refrigerant F1 in the form of a two-phase liquid-gas mixture.
  • the refrigerant F1 is separated in a separator device 6 into a gas phase 61 and a liquid phase 62 introduced separately into the exchanger 1 via a side manifold 30 and the manifold 50.
  • the two phases 61, 62 are then mixed with each other by means of a mixing device 3 arranged in the passage 10 and shown schematically on the Figure 1 .
  • several passages 10, or even all of the passages 10 of the first series include a mixing device 3.
  • the Figure 2 is a schematic sectional view, in a plane parallel to the longitudinal direction z and perpendicular to the lateral direction y, of the heat exchanger of the Figure 1 . It shows a stack of passages 10, 20 of the first and second series, mixing devices 3 being arranged in two passages 10.
  • the mixing device 3 advantageously consists of a bar, or rod, housed in a passage 10 and which preferably extends in the section of passage 10 over almost all, if not all, of the height of passage 10, so that the mixing device is in contact with each plate 2a, 2b forming passage 10.
  • the mixing device 3 is advantageously fixed to the adjacent plates 2a and 2b by brazing.
  • the mixing device 3 may have, parallel to the longitudinal direction z, a first dimension comprised between 20 and 200 mm and, parallel to the lateral direction y, a second dimension comprised between 100 and 1,400 mm.
  • the mixing device 3 is delimited in particular by a first surface 3a arranged facing a first plate 2a of the exchanger and a second surface 3b arranged facing a second plate 2b.
  • the second plate 2b forms, with a third plate 2c, the adjacent passage 20.
  • the first and second surfaces 3a, 3b preferably extend generally parallel, that is to say parallel or almost parallel, to the first and second plates 2a and 2b respectively.
  • the mixing device 3 is advantageously of generally parallelepipedal shape.
  • the first and second surfaces 3a, 3b are generally planar but can locally have recesses forming fluid channels, as explained below.
  • the mixer device 3 comprises at least a first channel 31 for channeling a gas phase 61 of the refrigerant F1, the direction of flow of the fluid being symbolized by the arrow 61.
  • the longitudinal section of the second channel 32 decreases towards the second surface 3b.
  • the longitudinal section of the second channel 32, or of an opening of said channel means the section of the channel measured parallel to the second surface 3b, that is to say according to section planes of said channel parallel to the second plate 3b.
  • the first channel 31 extends in the longitudinal direction z and the second channel 32 extends in the lateral direction y.
  • the longitudinal section of the second channel 32 then decreases in the direction represented by the arrow x.
  • the contact surface between the liquid phase 62 and the part of the second plate 2b extending at the level of the mixing device 3 is reduced, which makes it possible to greatly reduce the heat exchanges that can take place between the circulating fluid F2 flowing in the adjacent passage 20 and the liquid phase 62 of the refrigerant F1.
  • the two phases of the mixture are thus distributed as homogeneously as possible within the passages for the two-phase mixture, as well as between the different passages for the two-phase mixture.
  • This solution has the advantages of being easy to implement, of not modifying the size of the exchanger and of not complicating its structure.
  • the longitudinal channel 31 and the second channel 32 are in fluid communication via at least one orifice 34 arranged between the first channel 31 and the second channel 32.
  • the orifice 34 comprises an inlet 342 opening into the second channel 32 and a outlet 341 opening into the first channel 31.
  • One or more orifices 34 may be arranged along the y direction.
  • the longitudinal section of the second channel 32 decreases from the inlet 342 of the orifice 34 towards the second surface 3b.
  • the mixing of the liquid 62 and gas 61 phases takes place generally downstream of the outlet 341 and the two-phase liquid / gas mixture is distributed out of the mixing device through one or more passages 33.
  • the channels 31, 32 and / or the passages 33 may open out at the level of the end faces 35, 36 of the mixing device 3, or recessed towards the interior of the device 3 with respect to said faces 35, 36.
  • the first and second channels 31, 32 are of elongate shape, their length being great compared to their width.
  • the first and second channels 31, 32 pass through the mixing device 3 right through.
  • the second channel 32 extends over almost all, or even all of the width of the passage 10, measured in the lateral direction y.
  • At least one passage 10 of the first series is defined between a first plate 2a and a second plate 2b, the first plate 2a also defining an adjacent passage 20 of the second series immediately adjacent to the passage 10 considered.
  • a mixing device 3 is arranged in the passage 10 of the first series considered.
  • the first channel 31 is formed from a recess formed within the mixing device 3.
  • the first channel 31 may be formed from a recess formed within the mixing device 3 and opening out at the level of the first surface 3a.
  • the second channel 32 is formed from a recess formed within the mixing device 3.
  • the recess forming the second channel 32 opens at the level of the second surface 3b.
  • the second channel 32 then comprises a second open end 321 located at the level of the second surface 3b.
  • the second channel 32 is formed by a blind internal recess.
  • the Figures 3A to 6 illustrate mixing devices 3 comprising a single second channel 32.
  • the device 3 can also advantageously comprise several lateral channels 32 following one another along the longitudinal direction z.
  • the mixing device 3 can comprise one or more longitudinal channels 31.
  • the Figure 3B illustrates a device 3 comprising a row of longitudinal channels 31 succeeding one another along the lateral direction y.
  • the longitudinal channels 31 extend substantially parallel to each other.
  • the first longitudinal channels 31 are advantageously arranged between the second channel 32 and the first surface 3a.
  • the second channel 32 advantageously comprises a first end 322 located at the level of the inlet 342 of the orifice 34 and a second end 321 located on the side of the second surface 3b.
  • the longitudinal section of the second channel 32 decreases so that the ratio between the longitudinal section of the second channel 32 measured at the level of the second end 321 and the longitudinal section of the second channel 32 measured at level of the first end 322 is between 0 and 0.8, preferably between 0.2 and 0.8.
  • Such dimensioning makes it possible to minimize the heat exchanges between the liquid circulating in the second channel 32 and the adjacent fluids.
  • a ratio of longitudinal sections of second channel 32 equal to 0 corresponds to a second channel 32 whose cross section is triangular in shape.
  • the ratio between the longitudinal section of the opening 321 and the width of the second channel 32 measured at the level of the first end 322, or bottom 322, is between 0.2 and 0 , 8.
  • the longitudinal section of the second channel 32 can gradually decrease towards the second surface 3b.
  • the cross section of the second channel 32 is at least partly of frustoconical shape converging towards the second surface 3b.
  • the reduction in the longitudinal section of the second channel 32 can be caused by a lateral constriction 324 of said second channel 32 towards the second surface 3b.
  • the term “constriction” is understood to mean a sudden reduction in the width of the second channel 32, typically a reduction such as the section ratio. longitudinal values defined above is between 0.2 and 0.8, this reduction occurring over a distance typically less than 4 mm, in the direction of the second surface 3b.
  • the constriction 324 takes place in a substantially symmetrical fashion.
  • the constriction is such that the second channel 32 has an inverted T-shaped section, as illustrated in the figures.
  • the second channel 32 can comprise side walls 323 arranged perpendicularly to the bottom 322 and said bottom 322 can be arranged parallel to the longitudinal direction z.
  • Figure 3B remains applicable for a representation of the mixing device 3 in a plane perpendicular to that of the Figures 5 or 6 .
  • the mixing device 3 further comprises a third channel 37 for channeling the gas phase 61 of the refrigerant F1, said third channel 37 extending in the longitudinal direction z, between the second channel 32 and the second surface 3b.
  • this third channel 37 makes it possible to further minimize the heat exchanges between the liquid circulating in the second channel 32 and the fluids circulating in the adjacent passages. This in fact makes it possible to create a gas barrier which acts as a thermal insulator between the second channel and the second plate 2b.
  • the first channel 31 and the third channel 37 may be of distinct or identical shape and number.
  • the opening 321 of the second channel 32 advantageously opens into the third channel 37.
  • the mixing device 3 comprises at least two passages 33 for the two-phase liquid / gas mixture.
  • the exchanger according to the invention is mainly described in the case where the passages 10, 20 extend in the longitudinal direction z, the first channel 31 extending in the longitudinal direction z and the second channel 32 s' extending in a lateral direction y orthogonal to the longitudinal direction z.
  • the reverse is also possible, that is to say a first channel 31 extending in the lateral direction y and a second channel 32 extending in the longitudinal direction z.
  • the lateral y and longitudinal z directions may also not be mutually orthogonal.

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Description

La présente invention concerne un échangeur de chaleur comprenant des séries de passages pour chacun des fluides à mettre en relation d'échange thermique, l'échangeur comprenant au moins un dispositif mélangeur configuré pour distribuer au moins un mélange à deux phases liquide/gaz dans une des séries de passages Un échangeur selon le préambule de la revendication 1 est connu du document FR 2 563 620 A1 .The present invention relates to a heat exchanger comprising series of passages for each of the fluids to be placed in a heat exchange relationship, the exchanger comprising at least one mixing device configured to distribute at least one two-phase liquid / gas mixture in a series of passages An exchanger according to the preamble of claim 1 is known from the document FR 2 563 620 A1 .

En particulier, la présente invention peut s'appliquer à un échangeur de chaleur qui vaporise au moins un débit de mélange liquide-gaz, en particulier un débit de mélange à plusieurs constituants, par exemple un mélange d'hydrocarbures, par échange de chaleur avec au moins un autre fluide, par exemple du gaz naturel.In particular, the present invention can be applied to a heat exchanger which vaporizes at least one flow of liquid-gas mixture, in particular a flow of mixture with several constituents, for example a mixture of hydrocarbons, by heat exchange with at least one other fluid, for example natural gas.

La technologie couramment utilisée pour un échangeur est celle des échangeurs en aluminium à plaques et à ailettes brasés, qui permettent d'obtenir des dispositifs très compacts offrant une grande surface d'échange.The technology commonly used for an exchanger is that of brazed aluminum plate and fin exchangers, which make it possible to obtain very compact devices offering a large exchange surface.

Ces échangeurs comprennent des plaques entre lesquelles sont insérées des ondes d'échange thermique, formées d'une succession d'ailettes ou jambes d'onde, constituant ainsi un empilage de passages de vaporisation et de passages de condensation, les uns destinés à vaporiser du liquide frigorigène et les autres à condenser un gaz calorigène. Les échanges de chaleur entre les fluides peuvent avoir lieu avec ou sans changement de phase.These exchangers comprise plates between which are inserted heat exchange waves, formed of a succession of fins or wave legs, thus constituting a stack of vaporization passages and condensation passages, some intended to vaporize refrigerant and the like to condense a circulating gas. Heat exchange between fluids can take place with or without phase change.

Afin d'assurer le bon fonctionnement d'un échangeur mettant en œuvre un mélange liquide-gaz, la proportion de phase liquide et de phase gazeuse doit être la même dans tous les passages et doit être uniforme au sein d'un même passage.In order to ensure the correct operation of an exchanger using a liquid-gas mixture, the proportion of liquid phase and gas phase must be the same in all the passages and must be uniform within the same passage.

Le dimensionnement de l'échangeur est calculé en supposant une répartition uniforme des phases, et donc une seule température de fin de vaporisation de la phase liquide, égale à la température de rosée du mélange.The sizing of the exchanger is calculated by assuming a uniform distribution of the phases, and therefore a single end of vaporization temperature of the liquid phase, equal to the dew point temperature of the mixture.

Pour un mélange à plusieurs constituants, la température de fin de vaporisation va dépendre de la proportion de phase liquide et de phase gazeuse dans les passages.For a mixture with several constituents, the end of vaporization temperature will depend on the proportion of liquid phase and gas phase in the passages.

Dans le cas d'une répartition inégale des deux phases, le profil de température du fluide frigorigène va donc varier selon les passages, voire varier au sein d'un même passage. Du fait de cette répartition non uniforme, il peut alors arriver que le ou les fluides calorigènes en relation d'échange avec le mélange à deux phases aient une température en sortie de l'échangeur supérieure à celle prévue, ce qui dégrade en conséquence les performances de l'échangeur de chaleur.In the case of an unequal distribution of the two phases, the temperature profile of the refrigerant will therefore vary according to the passages, or even vary within the same passage. Due to this non-uniform distribution, it may then happen that the circulating fluid (s) in exchange relation with the two-phase mixture have a temperature at the outlet of the exchanger higher than that expected, which consequently degrades the performance. of the heat exchanger.

Une solution pour répartir le plus uniformément possible les phases liquide et gazeuse du mélange consiste à les introduire séparément dans l'échangeur, puis à les mélanger entre elles seulement à l'intérieur de l'échangeur.One solution for distributing the liquid and gas phases of the mixture as uniformly as possible consists of introducing them separately into the exchanger, then mixing them together only inside the exchanger.

Le document FR-A-2563620 décrit un tel échangeur dans lequel une barre rainurée est insérée dans la série de passages destinée à canaliser le mélange à deux phases. Ce dispositif mélangeur comporte des entrées séparées pour une phase liquide et une phase gazeuse débouchant dans un volume mélangeur commun muni d'une sortie pour distribuer le mélange liquide-gaz vers la zone d'échange thermique.The document FR-A-2563620 describes such an exchanger in which a grooved bar is inserted in the series of passages intended to channel the two-phase mixture. This mixing device has separate inlets for a liquid phase and a gas phase opening into a common mixing volume provided with an outlet for distributing the liquid-gas mixture to the heat exchange zone.

Cependant, la phase liquide alimentant le dispositif mélangeur se trouve alors inévitablement en situation d'échange thermique avec le ou les fluides calorigènes circulant dans les passages adjacents de l'autre série de passages. Ceci peut engendrer un début de vaporisation de la phase liquide au sein même des entrées correspondantes, entraînant de ce fait une répartition inégale des deux phases du mélange dans certains passages de la série ainsi que dans certaines zones au sein d'un même passage.However, the liquid phase supplying the mixing device is then inevitably in a heat exchange situation with the circulating fluid (s) circulating in the adjacent passages of the other series of passages. This can cause the start of vaporization of the liquid phase even within the corresponding inlets, thereby leading to an unequal distribution of the two phases of the mixture in certain passages of the series as well as in certain zones within the same passage.

Afin de minimiser les échanges de chaleur pouvant se produire au niveau du dispositif mélangeur, une solution serait d'installer la dispositif mélangeur dans une zone de l'échangeur dans laquelle aucun autre fluide ne circule. Il faudrait alors placer le dispositif mélangeur à une extrémité de l'échangeur, exempte de tout moyen d'évacuation ou d'amenée de fluide, ce qui imposerait de restructurer l'échangeur dans sa globalité et conduirait nécessairement à en augmenter l'encombrement. En outre, une telle solution ne permet pas l'introduction du mélange à deux phases au milieu de l'échangeur, ce qui peut être souhaitable dans des cas où les spécificités du procédé l'imposent.In order to minimize the heat exchanges that can occur at the mixing device, one solution would be to install the mixing device in a zone of the exchanger in which no other fluid is circulating. It would then be necessary to place the mixing device at one end of the exchanger, free of any means of discharge or supply of fluid, which would require restructuring the exchanger as a whole and would necessarily lead to an increase in its size. In addition, such a solution does not allow the introduction of the two-phase mixture in the middle of the exchanger, which may be desirable in cases where the specificities of the process require it.

La présente invention a pour but de résoudre en tout ou partie les problèmes mentionnés ci-avant, notamment en proposant un échangeur de chaleur dans lequel la répartition des phases liquide et gazeuse d'un mélange est la plus uniforme possible, et ce sans complexifier de façon excessive la structure de l'échangeur, ni en augmenter l'encombrement.The object of the present invention is to resolve all or part of the above-mentioned problems, in particular by proposing a heat exchanger in which the distribution of the liquid and gas phases of a mixture is as uniform as possible, and this without complicating any excessively the structure of the exchanger, nor increase its size.

La solution selon l'invention est alors un échangeur de chaleur selon la revendication 1.The solution according to the invention is then a heat exchanger according to claim 1.

Selon le cas, l'échangeur de l'invention peut comprendre l'une ou plusieurs des caractéristiques techniques suivantes :

  • les passages s'étendent suivant une direction longitudinale, le premier canal s'étendant suivant la direction longitudinale et le deuxième canal s'étendant suivant une direction latérale orthogonale à la direction longitudinale.
  • le premier canal est formé d'un premier évidement ménagé au sein du dispositif mélangeur.
  • le dispositif mélangeur comprend une première surface agencée en regard de la première plaque et une deuxième surface agencée en regard de la deuxième plaque, le premier évidement débouchant au niveau de la première surface.
  • le deuxième canal est formé d'un deuxième évidement ménagé au sein du dispositif mélangeur.
  • le deuxième évidement débouche au niveau de la deuxième surface.
  • le dispositif mélangeur comprend plusieurs premiers canaux longitudinaux se succédant suivant la direction latérale.
  • le deuxième canal comprend une première extrémité située au niveau de l'entrée de l'orifice et une deuxième extrémité située du côté de la deuxième plaque, le rapport entre la section longitudinale du deuxième canal mesurée au niveau de la deuxième extrémité et la section longitudinale du deuxième canal mesurée au niveau de la première extrémité étant compris entre 0 et 0,8, de préférence entre 0,2 et 0,8.
  • la section longitudinale du deuxième canal (32) diminue progressivement vers la deuxième plaque (2b).
  • le deuxième canal s'étend suivant la direction latérale, le section transversale du deuxième canal étant, dans un plan perpendiculaire à la direction latérale, au moins en partie de forme tronconique convergente vers la deuxième plaque.
  • la diminution de la section longitudinale du deuxième canal est provoquée par un étranglement latéral dudit deuxième canal se produisant en direction de la deuxième plaque.
  • le dispositif mélangeur comporte en outre au moins un troisième canal s'étendant parallèlement au premier canal, ledit troisième canal étant agencé entre le deuxième canal et la deuxième plaque.
Depending on the case, the exchanger of the invention may comprise one or more of the following technical characteristics:
  • the passages extend in a longitudinal direction, the first channel extending in the longitudinal direction and the second channel extending in a lateral direction orthogonal to the longitudinal direction.
  • the first channel is formed from a first recess formed within the mixing device.
  • the mixing device comprises a first surface arranged facing the first plate and a second surface arranged facing the second plate, the first recess opening out at the level of the first surface.
  • the second channel is formed by a second recess formed within the mixing device.
  • the second recess opens out at the second surface.
  • the mixing device comprises several first longitudinal channels following one another in the lateral direction.
  • the second channel comprises a first end located at the level of the entry of the orifice and a second end located on the side of the second plate, the ratio between the longitudinal section of the second channel measured at the level of the second end and the longitudinal section of the second channel measured at the first end being between 0 and 0.8, preferably between 0.2 and 0.8.
  • the longitudinal section of the second channel (32) gradually decreases towards the second plate (2b).
  • the second channel extends in the lateral direction, the cross section of the second channel being, in a plane perpendicular to the lateral direction, at least partly of frustoconical shape converging towards the second plate.
  • the reduction in the longitudinal section of the second channel is caused by a lateral constriction of said second channel occurring in the direction of the second plate.
  • the mixer device further comprises at least one third channel extending parallel to the first channel, said third channel being arranged between the second channel and the second plate.

La présente invention peut s'appliquer à un échangeur de chaleur qui vaporise au moins un débit de mélange liquide-gaz, en particulier un débit de mélange à plusieurs constituants, par exemple un mélange d'hydrocarbures , par échange de chaleur avec au moins un autre fluide, par exemple du gaz naturel.The present invention can be applied to a heat exchanger which vaporizes at least one flow of liquid-gas mixture, in particular a flow of mixture with several constituents, for example a mixture of hydrocarbons, by heat exchange with at least one. other fluid, for example natural gas.

L'expression "gaz naturel" se rapporte à toute composition contenant des hydrocarbures dont au moins du méthane. Cela comprend une composition « brute » (préalablement à tout traitement ou lavage), ainsi que toute composition ayant été partiellement, substantiellement ou entièrement traitée pour la réduction et/ou élimination d'un ou plusieurs composés, y compris, mais sans s'y limiter, le soufre, le dioxyde de carbone, l'eau, le mercure et certains hydrocarbures lourds et aromatiques.The expression “natural gas” refers to any composition containing hydrocarbons including at least methane. This includes a "crude" composition (prior to any treatment or washing), as well as any composition that has been partially, substantially or fully treated for the reduction and / or elimination of one or more compounds, including, but not limited to. limit, sulfur, carbon dioxide, water, mercury and some heavy and aromatic hydrocarbons.

La présente invention va maintenant être mieux comprise grâce à la description suivante, donnée uniquement à titre d'exemple non limitatif et faite en référence aux schémas ci-annexés, parmi lesquels :

  • la Figure 1 est une vue schématique en coupe, dans un plan parallèle aux directions longitudinale et latérale, d'une partie d'un passage de l'échangeur de chaleur alimenté en mélange à deux phases liquide-gaz conformément à un mode de réalisation de l'invention ;
  • la Figure 2 est une vue schématique en coupe, dans un plan parallèle à la direction longitudinale et perpendiculaire à la direction latérale, de séries de passages de l'échangeur de la Figure 1 ;
  • les Figures 3A et 3B sont des vues schématiques en coupe, suivant deux plans perpendiculaires à celui de la Figure 1, illustrant un mode de réalisation d'un dispositif mélangeur équipant un échangeur selon l'invention ;
  • les Figures 4A et 4B sont des vues partielles du dispositif mélangeur des Figures 3A et 3B et d'une variante d'un tel dispositif ;
  • les Figures 5 et 6 sont des vues schématiques en coupe de dispositifs mélangeurs selon d'autres modes de réalisation de l'invention.
The present invention will now be better understood by virtue of the following description, given solely by way of non-limiting example and made with reference to the attached diagrams, among which:
  • the Figure 1 is a schematic sectional view, in a plane parallel to the longitudinal and lateral directions, of a part of a passage of the heat exchanger supplied with a two-phase liquid-gas mixture according to an embodiment of the invention ;
  • the Figure 2 is a schematic sectional view, in a plane parallel to the longitudinal direction and perpendicular to the lateral direction, of a series of passages of the exchanger of the Figure 1 ;
  • the Figures 3A and 3B are schematic sectional views, following two planes perpendicular to that of the Figure 1 , illustrating an embodiment of a mixing device fitted to an exchanger according to the invention;
  • the Figures 4A and 4B are partial views of the mixing device of the Figures 3A and 3B and a variant of such a device;
  • the Figures 5 and 6 are schematic sectional views of mixing devices according to other embodiments of the invention.

Les Figures 1 et 2 illustrent un échangeur de chaleur 1 selon un mode de réalisation de l'invention comprenant un empilement de plaques 2a, 2b, 2c... qui s'étendent suivant deux dimensions, suivant une direction longitudinale z et une direction latérale y. Les plaques 2a, 2b, 2c... sont disposées parallèlement l'une au-dessus de l'autre avec espacement et forment ainsi une pluralité de passages pour des fluides en relation d'échange de chaleur indirect via lesdites plaques. La direction latérale y est représentée orthogonale à la direction longitudinale z et parallèle aux plaques 2a, 2b, 2c....The Figures 1 and 2 illustrate a heat exchanger 1 according to an embodiment of the invention comprising a stack of plates 2a, 2b, 2c ... which extend in two dimensions, in a longitudinal direction z and a lateral direction y. The plates 2a, 2b, 2c ... are arranged parallel one above the other with spacing and thus form a plurality of passages for fluids in indirect heat exchange relation via said plates. The lateral direction is represented therein orthogonal to the longitudinal direction z and parallel to the plates 2a, 2b, 2c ....

De préférence, chaque passage a une forme parallélépipédique et plate. L'écart entre deux plaques successives est petit devant la longueur et la largeur de chaque plaque successive.Preferably, each passage has a parallelepipedal and flat shape. The gap between two successive plates is small compared to the length and width of each successive plate.

L'échangeur 1 peut comprendre un nombre de plaques supérieur à 20, voire supérieur à 100, définissant entre elles une première série de passages 10 pour canaliser au moins un fluide frigorigène F1, et une deuxième série de passages 20 (non visible sur la Figure 1) pour canaliser au moins un fluide calorigène F2, l'écoulement desdits fluides ayant lieu globalement suivant la direction longitudinale z. Les passages 10 de la première série peuvent être agencés, en tout ou partie, en alternance ou de façon adjacente avec tout ou partie des passages 20 de la deuxième série.The exchanger 1 may include a number of plates greater than 20, or even greater than 100, defining between them a first series of passages 10 for channeling at least one refrigerant F1, and a second series of passages 20 (not visible on the Figure 1 ) to channel at least one circulating fluid F2, the flow of said fluids taking place generally in the longitudinal direction z. The passages 10 of the first series can be arranged, in whole or in part, alternating or adjacent to all or part of the passages 20 of the second series.

De façon connue en soi, l'échangeur 1 comprend des moyens de distribution et d'évacuation 43, 52 configurés pour distribuer les différents fluides sélectivement dans les passages 10, 20, ainsi que pour évacuer lesdits fluides desdits passages 10, 20.In a manner known per se, the exchanger 1 comprises distribution and evacuation means 43, 52 configured to distribute the various fluids selectively in the passages 10, 20, as well as to evacuate said fluids from said passages 10, 20.

L'étanchéité des passages 10, 20 le long des bords des plaques 2a,.. est généralement assurée par des bandes d'étanchéité latérales et longitudinales 4 fixées sur les plaques 2a,... Les bandes d'étanchéité latérales 4 n'obturent pas complétement les passages 10, 20 mais laissent avantageusement des ouvertures d'entrée et de sortie de fluide situées dans les coins diagonalement opposés des passages.The sealing of the passages 10, 20 along the edges of the plates 2a, .. is generally ensured by lateral and longitudinal sealing strips 4 fixed to the plates 2a, ... The lateral sealing strips 4 do not block off not completely the passages 10, 20 but advantageously leave fluid inlet and outlet openings located in the diagonally opposite corners of the passages.

Les ouvertures des passages 10 de la première série sont disposées en coïncidence l'une au-dessus de l'autre, tandis que les ouvertures des passages 20 de la deuxième série sont disposées dans les coins opposés. Les ouvertures placées l'une au-dessus de l'autre sont réunies respectivement dans des collecteurs de forme semi-tubulaire 40, 45, 50, 55, par lesquels s'effectuent la distribution et l'évacuation des fluides.The openings of the passages 10 of the first series are arranged in coincidence one above the other, while the openings of the passages 20 of the second series are arranged at the opposite corners. The openings placed one above the other are united respectively in semi-tubular collectors 40, 45, 50, 55, through which the distribution and evacuation of the fluids take place.

Dans les représentations des Figures 1 et 2, les collecteurs semi-tubulaires 50, 45 servent à l'introduction des fluides dans l'échangeur 1 et les collecteurs semi-tubulaires 40, 55 servent à l'évacuation de ces fluides hors de l'échangeur 1.In the representations of Figures 1 and 2 , the semi-tubular collectors 50, 45 are used for the introduction of fluids into the exchanger 1 and the semi-tubular collectors 40, 55 are used for the evacuation of these fluids out of the exchanger 1.

Dans cette variante de réalisation, le collecteur d'alimentation d'un des fluides et le collecteur d'évacuation de l'autre fluide sont situés à une même extrémité de l'échangeur, les fluides F1, F2 circulant ainsi à contre-courant dans l'échangeur 1.In this variant embodiment, the supply manifold of one of the fluids and the discharge manifold of the other fluid are located at the same end of the exchanger, the fluids F1, F2 thus circulating in counter-current in exchanger 1.

Selon une autre variante de réalisation, les fluides frigorigène et calorigène peuvent également circuler à co-courant, les moyens d'alimentation d'un des fluides et les moyens d'évacuation de l'autre fluide étant alors situés à des extrémités opposées de l'échangeur 1.According to another variant embodiment, the refrigerant and circulating fluids can also circulate in co-current, the means for supplying one of the fluids and the means for discharging the other fluid then being located at opposite ends of the 'exchanger 1.

De préférence, la direction longitudinale est orientée verticalement lorsque l'échangeur 1 est en fonctionnement. Le fluide frigorigène F1 s'écoule globalement verticalement et dans le sens ascendant. D'autres directions et sens d'écoulement des fluides F1, F2 sont bien entendu envisageables, sans sortir du cadre de la présente invention.Preferably, the longitudinal direction is oriented vertically when the exchanger 1 is in operation. The refrigerant F1 flows generally vertically and in the upward direction. Other directions and direction of flow of the fluids F1, F2 can of course be envisaged, without departing from the scope of the present invention.

A noter que dans le cadre de l'invention, un ou plusieurs fluides frigorigènes F1 et un ou plusieurs fluides calorigènes F2 de natures différentes peuvent s'écouler au sein des passages 10, 20 des première et deuxième séries d'un même échangeur.It should be noted that in the context of the invention, one or more refrigerants F1 and one or more circulating fluids F2 of different types can flow within passages 10, 20 of the first and second series of the same exchanger.

Les moyens de distribution et d'évacuation 43, 52 comprennent avantageusement des ondes de distribution 44, 51, 54, agencées entre deux plaques 2a, 2b,... successives sous forme de tôles ondulées, qui s'étendent à partir des ouvertures d'entrée et de sortie. Les ondes de distribution 44, 51, 54 assurent la répartition uniforme et la récupération des fluides sur toute la largeur des passages 10, 20.The distribution and evacuation means 43, 52 advantageously comprise distribution waves 44, 51, 54, arranged between two successive plates 2a, 2b, ... in the form of corrugated sheets, which extend from the openings d entry and exit. The distribution waves 44, 51, 54 ensure the uniform distribution and the recovery of the fluids over the entire width of the passages 10, 20.

En outre, les passages 10, 20 comprennent avantageusement des structures d'échange thermique disposées entre les plaques 2a, 2b,.... Ces structures ont pour fonction d'augmenter la surface d'échange thermique de l'échangeur. En effet, les structures d'échange thermique sont en contact avec les fluides circulant dans les passages et transferrent des flux thermiques par conduction jusqu'aux plaques adajcentes, auxquelles elles peuvent être fixées par brasage, ce qui augmente la résistance mécanique de l'échangeur.In addition, the passages 10, 20 advantageously comprise heat exchange structures arranged between the plates 2a, 2b, .... These structures have the function of increasing the heat exchange surface area of the exchanger. Indeed, the heat exchange structures are in contact with the fluids circulating in the passages and transfer heat flows by conduction to the adjacent plates, to which they can be fixed by brazing, which increases the mechanical resistance of the exchanger.

Les structures d'échange thermique ont aussi une fonction d'entretoises entre les plaques, notamment lors de l'assemblage par brasage de l'échangeur et pour éviter toute déformation des plaques lors de la mise en oeuvre des fluides sous pression. Elles assurent également le guidage des écoulements de fluide dans les passages de l'échangeur.The heat exchange structures also have a function of spacers between the plates, in particular during assembly by brazing the exchanger and to prevent any deformation of the plates during the use of fluids under pressure. They also ensure the guidance of the fluid flows in the passages of the exchanger.

De préférence, ces structures comprennent des ondes d'échange thermique 11 qui s'étendent avantageusement suivant la largeur et la longueur des passages 10, 20, parallélement aux plaques, dans le prolongement des ondes de distribution 44, 51, 54 selon la longueur des passages 10, 20. Les passages 10, 20 de l'échangeur présente ainsi une partie principale de leur longueur constituant la partie d'échange thermique proprement dite, qui est garnie d'une structure d'échange thermique, ladite partie principale étant bordée par des parties de distribution garnies des ondes de distribution 44, 51, 54.Preferably, these structures comprise heat exchange waves 11 which advantageously extend along the width and the length of the passages 10, 20, parallel to the plates, in the extension of the distribution waves 44, 51, 54 along the length of the passages 10, 20. The passages 10, 20 of the exchanger thus have a main part of their length constituting the actual heat exchange part, which is lined with a heat exchange structure, said main part being bordered by distribution parts furnished with distribution waves 44, 51, 54.

La Figure 1 illustre un passage 10 de la première série 1 configuré pour distribuer un fluide frigorigène F1 se présentant sous la forme d'un mélange liquide-gaz à deux phases. Le fluide frigorigène F1 est séparé dans un dispositif séparateur 6 en une phase gazeuse 61 et une phase liquide 62 introduites séparément dans l'échangeur 1 par l'intermédiaire d'un collecteur latéral 30 et du collecteur 50. Les deux phases 61, 62 sont ensuite mélangées l'une avec l'autre au moyen d'un dispositif mélangeur 3 agencé dans le passage 10 et représentée de façon schématique sur la Figure 1. Avantageusement, plusieurs passages 10, voire la totalité des passages 10 de la première série comporte un dispositif mélangeur 3.The Figure 1 illustrates a passage 10 of the first series 1 configured to distribute a refrigerant F1 in the form of a two-phase liquid-gas mixture. The refrigerant F1 is separated in a separator device 6 into a gas phase 61 and a liquid phase 62 introduced separately into the exchanger 1 via a side manifold 30 and the manifold 50. The two phases 61, 62 are then mixed with each other by means of a mixing device 3 arranged in the passage 10 and shown schematically on the Figure 1 . Advantageously, several passages 10, or even all of the passages 10 of the first series include a mixing device 3.

La Figure 2 est une vue schématique en coupe, dans un plan parallèle à la direction longitudinale z et perpendiculaire à la direction latérale y, de l'échangeur de la Figure 1. On y voit un empilement de passages 10, 20 des première et deuxième séries, des dispositifs mélangeurs 3 étant agencés dans deux passages 10.The Figure 2 is a schematic sectional view, in a plane parallel to the longitudinal direction z and perpendicular to the lateral direction y, of the heat exchanger of the Figure 1 . It shows a stack of passages 10, 20 of the first and second series, mixing devices 3 being arranged in two passages 10.

Le dispositif mélangeur 3 selon l'invention se compose avantageusement d'une barre, ou baguette, logée dans un passage 10 et qui s'étend de préférence dans la section du passage 10 sur la quasi-totalité, voire la totalité, de la hauteur du passage 10, de sorte que le dispositif mélangeur est en contact avec chaque plaque 2a, 2b formant le passage 10.The mixing device 3 according to the invention advantageously consists of a bar, or rod, housed in a passage 10 and which preferably extends in the section of passage 10 over almost all, if not all, of the height of passage 10, so that the mixing device is in contact with each plate 2a, 2b forming passage 10.

Le dispositif mélangeur 3 est avantageusement fixé aux plaques adjacentes 2a et 2b par brasage.The mixing device 3 is advantageously fixed to the adjacent plates 2a and 2b by brazing.

Le dispositif mélangeur 3 peut présenter, parallèlement à la direction longitudinale z, une première dimension comprise entre 20 et 200 mm et, parallèlement à la direction latérale y, une deuxième dimension comprise entre 100 et 1400 mm.The mixing device 3 may have, parallel to the longitudinal direction z, a first dimension comprised between 20 and 200 mm and, parallel to the lateral direction y, a second dimension comprised between 100 and 1,400 mm.

Comme on le voit sur les Figures 3A et 3B, le dispositif mélangeur 3 est délimité notamment par une première surface 3a agencée en regard d'une première plaque 2a de l'échangeur et une deuxième surface 3b agencée en regard d'une deuxième plaque 2b. La deuxième plaque 2b forme, avec une troisième plaque 2c, le passage 20 adjacent. Les premières et deuxième surfaces 3a, 3b s'étendent de préférence globalement parallèlement, c'est-à-dire parallèlement ou quasi-parallèlement, aux première et deuxième plaques 2a et 2b respectivement.As seen on Figures 3A and 3B , the mixing device 3 is delimited in particular by a first surface 3a arranged facing a first plate 2a of the exchanger and a second surface 3b arranged facing a second plate 2b. The second plate 2b forms, with a third plate 2c, the adjacent passage 20. The first and second surfaces 3a, 3b preferably extend generally parallel, that is to say parallel or almost parallel, to the first and second plates 2a and 2b respectively.

Le dispositif mélangeur 3 est avantageusement de forme générale parallélépipédique. Les première et deuxième surfaces 3a, 3b sont globalement planes mais peuvent présenter localement des évidements formant des canaux de fluide, comme expliqué ci-après.The mixing device 3 is advantageously of generally parallelepipedal shape. The first and second surfaces 3a, 3b are generally planar but can locally have recesses forming fluid channels, as explained below.

Le dispositif mélangeur 3 comprend au moins un premier canal 31 pour canaliser une phase gazeuse 61 du fluide frigorigène F1, la direction d'écoulement du fluide étant symbolisée par la flèche 61.The mixer device 3 comprises at least a first channel 31 for channeling a gas phase 61 of the refrigerant F1, the direction of flow of the fluid being symbolized by the arrow 61.

En outre, au moins un deuxième canal 32 pour canaliser une phase liquide 62 du fluide frigorigène F1.In addition, at least a second channel 32 for channeling a liquid phase 62 of the refrigerant F1.

Selon l'invention, la section longitudinale du deuxième canal 32 diminue en direction de la deuxième surface 3b.According to the invention, the longitudinal section of the second channel 32 decreases towards the second surface 3b.

A noter que dans le cadre de l'invention, la section longitudinale du deuxième canal 32, ou d'une ouverture dudit canal, s'entend de la section du canal mesurée parallèlement à la deuxième surface 3b, c'est-à-dire selon des plans de coupe dudit canal parallèles à la deuxième plaque 3b.Note that in the context of the invention, the longitudinal section of the second channel 32, or of an opening of said channel, means the section of the channel measured parallel to the second surface 3b, that is to say according to section planes of said channel parallel to the second plate 3b.

Ainsi, dans le mode de réalisation illustré par la Figure 3A, le premier canal 31 s'étend suivant la direction longitudinale z et le deuxième canal 32 s'étend suivant la direction latérale y. La section longitudinale du deuxième canal 32 diminue alors suivant la direction représentée par la flèche x.Thus, in the embodiment illustrated by Figure 3A , the first channel 31 extends in the longitudinal direction z and the second channel 32 extends in the lateral direction y. The longitudinal section of the second channel 32 then decreases in the direction represented by the arrow x.

En réduisant la section longitudinale du deuxième canal 32 en direction de la deuxième plaque 2b, on réduit la surface de contact entre la phase liquide 62 et la partie de la deuxième plaque 2b s'étendant au niveau du dispositif mélangeur 3, ce qui permet de réduire grandement les échanges de chaleur pouvant avoir lieu entre le fluide calorigène F2 circulant dans le passage 20 adjacent et la phase liquide 62 du fluide frigorigène F1. Ceci permet de limiter, voire d'éviter une vaporisation de la phase liquide avant son mélange avec la phase gazeuse dudit fluide frigorigène F1. Les deux phases du mélange sont ainsi réparties de la façon la plus homogène possible au sein même des passages pour le mélange à deux phases, ainsi qu'entre les différents passages pour le mélange à deux phases.By reducing the longitudinal section of the second channel 32 in the direction of the second plate 2b, the contact surface between the liquid phase 62 and the part of the second plate 2b extending at the level of the mixing device 3 is reduced, which makes it possible to greatly reduce the heat exchanges that can take place between the circulating fluid F2 flowing in the adjacent passage 20 and the liquid phase 62 of the refrigerant F1. This makes it possible to limit or even avoid vaporization of the liquid phase before it is mixed with the gas phase of said refrigerant F1. The two phases of the mixture are thus distributed as homogeneously as possible within the passages for the two-phase mixture, as well as between the different passages for the two-phase mixture.

Cette solution présente les avantages d'être simple de mise en œuvre, de ne pas modifier l'encombrement de l'échangeur et de ne pas complexifier sa structure.This solution has the advantages of being easy to implement, of not modifying the size of the exchanger and of not complicating its structure.

Avantageusement, le canal longitudinal 31 et le deuxième canal 32 sont en communication fluidique via un au moins un orifice 34 agencé entre le premier canal 31 et le deuxième canal 32. L'orifice 34 comprend une entrée 342 débouchant dans le deuxième canal 32 et une sortie 341 débouchant dans le premier canal 31. Un ou plusieurs orifices 34 peuvent être disposés le long de la direction y.Advantageously, the longitudinal channel 31 and the second channel 32 are in fluid communication via at least one orifice 34 arranged between the first channel 31 and the second channel 32. The orifice 34 comprises an inlet 342 opening into the second channel 32 and a outlet 341 opening into the first channel 31. One or more orifices 34 may be arranged along the y direction.

La section longitudinale du deuxième canal 32, diminue depuis l'entrée 342 de l'orifice 34 vers la deuxième surface 3b.The longitudinal section of the second channel 32 decreases from the inlet 342 of the orifice 34 towards the second surface 3b.

En fonctionnement, le mélange des phases liquide 62 et gazeuse 61 s'effectue globalement en aval de la sortie 341 et le mélange à deux phases liquide/gaz est distribué hors du dispositif de mélange par une ou plusieurs passages 33.In operation, the mixing of the liquid 62 and gas 61 phases takes place generally downstream of the outlet 341 and the two-phase liquid / gas mixture is distributed out of the mixing device through one or more passages 33.

Les canaux 31, 32 et/ou les passages 33 peuvent déboucher au niveau des faces extrêmes 35, 36 du dispositif mélangeur 3, ou en retrait vers l'intérieur du dispositif 3 par rapport audites faces 35, 36.The channels 31, 32 and / or the passages 33 may open out at the level of the end faces 35, 36 of the mixing device 3, or recessed towards the interior of the device 3 with respect to said faces 35, 36.

De préférence, les premier et deuxième canaux 31, 32 sont de forme longiligne, leur longueur étant grande devant leur largeur.Preferably, the first and second channels 31, 32 are of elongate shape, their length being great compared to their width.

Avantageusement, les premier et deuxième canaux 31, 32 traversent le dispositif mélangeur 3 de part en part. Ainsi, le deuxième canal 32 s'étend sur la quasi-totalité, voire la totalité de la largeur du passage 10, mesurée selon la direction latérale y.Advantageously, the first and second channels 31, 32 pass through the mixing device 3 right through. Thus, the second channel 32 extends over almost all, or even all of the width of the passage 10, measured in the lateral direction y.

Dans le cadre de l'invention, au moins un passage 10 de la première série est défini entre une première plaque 2a et une deuxième plaque 2b, la première plaque 2a définissant également un passage adjacent 20 de la deuxième série immédiatement adjacent au passage 10 considéré. Un dispositif mélangeur 3 est agencé dans le passage 10 de la première série considéré.In the context of the invention, at least one passage 10 of the first series is defined between a first plate 2a and a second plate 2b, the first plate 2a also defining an adjacent passage 20 of the second series immediately adjacent to the passage 10 considered. . A mixing device 3 is arranged in the passage 10 of the first series considered.

Avantageusement, le premier canal 31 est formé d'un évidement ménagé au sein du dispositif mélangeur 3.Advantageously, the first channel 31 is formed from a recess formed within the mixing device 3.

Selon une variante illustrée sur les Figures 3A à 6, le premier canal 31 peut être formé d'un évidement ménagé au sein du dispositif mélangeur 3 et débouchant au niveau de la première surface 3a. De préférence, le deuxième canal 32 est formé d'un évidement ménagé au sein du dispositif mélangeur 3.According to a variant illustrated on Figures 3A to 6 , the first channel 31 may be formed from a recess formed within the mixing device 3 and opening out at the level of the first surface 3a. Preferably, the second channel 32 is formed from a recess formed within the mixing device 3.

Dans une forme de réalisation illustrée notamment sur la Figure 4A, l'évidemment formant le deuxième canal 32 débouche au niveau de la deuxième surface 3b. Le deuxième canal 32 comporte alors une deuxième extrémité 321 ouverte située au niveau de la deuxième surface 3b.In one embodiment illustrated in particular on the Figure 4A , the recess forming the second channel 32 opens at the level of the second surface 3b. The second channel 32 then comprises a second open end 321 located at the level of the second surface 3b.

Selon une variante, illustrée sur la Figure 4B, le deuxième canal 32 est formé par un évidemment interne non débouchant.According to a variant, illustrated on Figure 4B , the second channel 32 is formed by a blind internal recess.

Les Figures 3A à 6 illustrent des dispositifs de mélange 3 comprenant un seul deuxième canal 32. Le dispositif 3 peut aussi comprendre, de manière avantageuse, plusieurs canaux latéraux 32 se succédant le long de la direction longitudinale z.The Figures 3A to 6 illustrate mixing devices 3 comprising a single second channel 32. The device 3 can also advantageously comprise several lateral channels 32 following one another along the longitudinal direction z.

De même, le dispositif de mélange 3 peut comprendre un ou plusieurs canaux longitudinaux 31. La Figure 3B illustre un dispositif 3 comportant une rangée de canaux longitudinaux 31 se succédant le long de la direction latérale y. De préférence, les canaux longitudinaux 31 s'étendent sensiblement parallèlement les uns aux autres. Les premiers canaux longitudinaux 31 sont avantageusement agencés entre le deuxième canal 32 et la première surface 3a.Likewise, the mixing device 3 can comprise one or more longitudinal channels 31. The Figure 3B illustrates a device 3 comprising a row of longitudinal channels 31 succeeding one another along the lateral direction y. Preferably, the longitudinal channels 31 extend substantially parallel to each other. The first longitudinal channels 31 are advantageously arranged between the second channel 32 and the first surface 3a.

Plus précisément, le deuxième canal 32 comprend avantageusement une première extrémité 322 située au niveau de l'entrée 342 de l'orifice 34 et une deuxième extrémité 321 située du côté de la deuxième surface 3b.More precisely, the second channel 32 advantageously comprises a first end 322 located at the level of the inlet 342 of the orifice 34 and a second end 321 located on the side of the second surface 3b.

Selon un mode de réalisation avantageux de l'invention, la section longitudinale du deuxième canal 32 diminue de sorte que le rapport entre la section longitudinale du deuxième canal 32 mesurée au niveau de la deuxième extrémité 321 et la section longitudinale du deuxième canal 32 mesurée au niveau de la première extrémité 322 est compris entre 0 et 0,8, de préférence entre 0,2 et 0,8.According to an advantageous embodiment of the invention, the longitudinal section of the second channel 32 decreases so that the ratio between the longitudinal section of the second channel 32 measured at the level of the second end 321 and the longitudinal section of the second channel 32 measured at level of the first end 322 is between 0 and 0.8, preferably between 0.2 and 0.8.

Un tel dimensionnement permet de minimiser les échanges thermiques entre le liquide circulant dans le deuxième canal 32 et les fluides adjacents.Such dimensioning makes it possible to minimize the heat exchanges between the liquid circulating in the second channel 32 and the adjacent fluids.

A titre d'exemple, dans la configuration illustrée sur les Figures 4A ou 4B, un rapport de sections longitudinales de deuxième canal 32 égal à 0 correspond à un deuxième canal 32 dont la section transversale est de forme triangulaire.By way of example, in the configuration illustrated on the Figures 4A or 4B , a ratio of longitudinal sections of second channel 32 equal to 0 corresponds to a second channel 32 whose cross section is triangular in shape.

Dans le cas d'un deuxième canal 32 débouchant, le rapport entre la section longitudinale de l'ouverture 321 et la largeur du deuxième canal 32 mesurée au niveau de la première extrémité 322, ou fond 322, est compris entre 0,2 et 0,8.In the case of a second opening channel 32, the ratio between the longitudinal section of the opening 321 and the width of the second channel 32 measured at the level of the first end 322, or bottom 322, is between 0.2 and 0 , 8.

En particulier, comme illustré sur les Figures 3A, 4A et 4B, la section longitudinale du deuxième canal 32 peut diminuer progressivement vers la deuxième surface 3b.In particular, as illustrated on Figures 3A , 4A and 4B , the longitudinal section of the second channel 32 can gradually decrease towards the second surface 3b.

Selon une forme de réalisation avantageuse de l'invention, et comme visible sur les Figures 3A, 4A et 4B, la section transversale du deuxième canal 32 est au moins en partie de forme tronconique convergente vers la deuxième surface 3b.According to an advantageous embodiment of the invention, and as visible on the Figures 3A , 4A and 4B , the cross section of the second channel 32 is at least partly of frustoconical shape converging towards the second surface 3b.

De façon alternative, la diminution de la section longitudinale du deuxième canal 32 peut être provoquée par un étranglement latéral 324 dudit deuxième canal 32 en direction de la deuxième surface 3b. Par « étranglement », on entend une diminution brusque de la largeur du deuxième canal 32, typiquement une diminution telle que le rapport de sections longitudinales défini précédemment est compris entre 0,2 et 0,8, cette diminution se produisant sur une distance typiquement inférieure à 4 mm, en direction de la deuxième surface 3b.Alternatively, the reduction in the longitudinal section of the second channel 32 can be caused by a lateral constriction 324 of said second channel 32 towards the second surface 3b. The term “constriction” is understood to mean a sudden reduction in the width of the second channel 32, typically a reduction such as the section ratio. longitudinal values defined above is between 0.2 and 0.8, this reduction occurring over a distance typically less than 4 mm, in the direction of the second surface 3b.

Ainsi, on réduit encore plus les échanges de chaleur pouvant avoir lieu entre le fluide calorigène F2 circulant dans le passage 20 adjacent et la phase liquide du fluide frigorigène F1 avant son mélange avec la phase gazeuse.Thus, the heat exchanges that can take place between the circulating fluid F2 circulating in the adjacent passage 20 and the liquid phase of the refrigerant F1 before its mixing with the gas phase are further reduced.

De préférence, l'étranglement 324 a lieu de façon sensiblement symétrique.Preferably, the constriction 324 takes place in a substantially symmetrical fashion.

Avantageusement, l'étranglement est tel que le deuxième canal 32 a une section en forme de T inversé, comme illustré sur les Figures 5 et 6 Advantageously, the constriction is such that the second channel 32 has an inverted T-shaped section, as illustrated in the figures. Figures 5 and 6

Plus précisément, le deuxième canal 32 peut comprendre des parois latérales 323 disposées perpendiculairement au fond 322 et ledit fond 322 peut être disposé parallèlement à la direction longitudinale z.More precisely, the second channel 32 can comprise side walls 323 arranged perpendicularly to the bottom 322 and said bottom 322 can be arranged parallel to the longitudinal direction z.

La représentation de la Figure 3B reste applicable pour une représentation du dispositif mélangeur 3 dans un plan perpendiculaire à celui des Figures 5 ou 6.The representation of Figure 3B remains applicable for a representation of the mixing device 3 in a plane perpendicular to that of the Figures 5 or 6 .

Selon un mode de réalisation particulier de l'invention, illustré sur la Figure 6, le dispositif mélangeur 3 comporte en outre un troisième canal 37 pour canaliser la phase gazeuse 61 du fluide frigorigène F1, ledit troisième canal 37 s'étendant suivant la direction longitudinale z, entre le deuxième canal 32 et la deuxième surface 3b.According to a particular embodiment of the invention, illustrated in Figure 6 , the mixing device 3 further comprises a third channel 37 for channeling the gas phase 61 of the refrigerant F1, said third channel 37 extending in the longitudinal direction z, between the second channel 32 and the second surface 3b.

La présence de ce troisième canal 37 permet de minimiser encore plus les échanges thermiques entre le liquide circulant dans le deuxième canal 32 et les fluides circulant dans les passages adjacents. Ceci permet en effet de créer une barrière de gaz qui joue le rôle d'isolant thermique entre le deuxième canal et la deuxième plaque 2b.The presence of this third channel 37 makes it possible to further minimize the heat exchanges between the liquid circulating in the second channel 32 and the fluids circulating in the adjacent passages. This in fact makes it possible to create a gas barrier which acts as a thermal insulator between the second channel and the second plate 2b.

Etant précisé que le premier canal 31 et le troisième canal 37 peuvent être de forme et en nombre distincts ou identiques. Comme montré sur la Figure 6, l'ouverture 321 du deuxième canal 32 débouche avantageusement dans le troisième canal 37. Dans ce mode de réalisation, le dispositif mélangeur 3 comprend au moins deux passages 33 pour le mélange à deux phases liquide/gaz.It being specified that the first channel 31 and the third channel 37 may be of distinct or identical shape and number. As shown on the Figure 6 , the opening 321 of the second channel 32 advantageously opens into the third channel 37. In this embodiment, the mixing device 3 comprises at least two passages 33 for the two-phase liquid / gas mixture.

Bien entendu, l'invention n'est pas limitée aux exemples particuliers décrits et illustrés dans la présente demande. D'autres variantes ou modes de réalisation à la portée de l'homme du métier peuvent aussi être envisagés sans sortir du cadre de l'invention.Of course, the invention is not limited to the specific examples described and illustrated in the present application. Other variants or embodiments within the reach of a person skilled in the art can also be envisaged without departing from the scope of the invention.

Par exemple, l'échangeur selon l'invention est principalement décrit dans le cas où les passages 10, 20 s'étendent suivant la direction longitudinale z, le premier canal 31 s'étendant suivant la direction longitudinale z et le deuxième canal 32 s'étendant suivant une direction latérale y orthogonale à la direction longitudinale z. L'inverse est aussi envisageable, c'est-à-dire un premier canal 31 s'étendant suivant la direction latérale y et un deuxième canal 32 s'étendant suivant la direction longitudinale z. Les directions latérale y et longitudinale z peuvent aussi ne pas être orthogonales entre elles.For example, the exchanger according to the invention is mainly described in the case where the passages 10, 20 extend in the longitudinal direction z, the first channel 31 extending in the longitudinal direction z and the second channel 32 s' extending in a lateral direction y orthogonal to the longitudinal direction z. The reverse is also possible, that is to say a first channel 31 extending in the lateral direction y and a second channel 32 extending in the longitudinal direction z. The lateral y and longitudinal z directions may also not be mutually orthogonal.

Claims (13)

  1. Heat exchanger (1) comprising a plurality of plates (2a, 2b, 2c, ...) arranged parallel to each other so as to define a first series of passages (10) for channelling at least one refrigerating fluid (F1) and a second series of passages (20) for channelling at least one calorigenic fluid (F2) to be put in heat-exchange relationship with at least said refrigerating fluid (F1), at least one passage (10) in the first series being defined between a second plate (2b) defining an adjacent passage (20) in the second series and a first plate (2a), a mixing device (3) furthermore being arranged in said at least one passage (10) in the first series and comprising:
    - at least one first channel (31) for channelling a gaseous phase (61) of the refrigerating fluid (F1),
    - at least one second channel (32) for channelling a liquid phase (62) of the refrigerating fluid (F1), the first channel (31) being arranged between the second channel (32) and the first plate (2a),
    wherein at least one orifice (34) is arranged between the first channel (31) and the second channel (32), said orifice (34) comprises an inlet (342) emerging in the second channel (32) and an outlet (341) emerging in the first channel (31),
    characterised in that the longitudinal section of the second channel (32), measured parallel to the second plate (3b), decreases from the inlet (342) of the orifice (34) towards said second plate (2b).
  2. Exchanger according to claim 1, characterised in that the first channel (31) and the second channel (32) extend parallel to the first and second plates (2a, 2b).
  3. Exchanger according to one of the preceding claims, characterised in that the passages (10, 20) extend in a longitudinal direction (z), the first channel (31) extending in the longitudinal direction (z) and the second channel (32) extending in a lateral direction (y) orthogonal to the longitudinal direction (z).
  4. Exchanger according to one of the preceding claims, characterised in that the first channel (31) is formed by a first recess provided in the mixing device (3).
  5. Exchanger according to claim 4, characterised in that the mixing device (3) comprises a first surface (3a) arranged opposite the first plate (2a) and a second surface (3b) arranged opposite the second plate (2b), the first recess emerging at the first surface (3a).
  6. Exchanger according to one of the preceding claims, characterised in that the second channel (32) is formed by a second recess provided in the mixing device (3).
  7. Exchanger according to claim 6, characterised in that the second recess provided in the mixing device (3) emerges at the second surface (3b).
  8. Exchanger according to one of the preceding claims, characterised in that the mixing device (3) comprises a plurality of first longitudinal channels (31) succeeding each other in the lateral direction (y).
  9. Exchanger according to one of the preceding claims, characterised in that the second channel (32) comprises a first end (322) situated at the inlet (342) of the orifice (34) and a second end (321) situated on the same side as the second plate (2b), the ratio between the longitudinal section of the second channel (32) measured at the second end (321) and the longitudinal section of the second channel (32) measured at the first end (322) being between 0 and 0.8, preferably between 0.2 and 0.8.
  10. Exchanger according to one of the preceding claims, characterised in that the longitudinal section of the second channel (32) decreases gradually towards the second plate (2b).
  11. Exchanger according to one of the preceding claims, characterised in that the second channel (32) extends in the lateral direction (y), the cross section of the second channel (32) being, in a plane perpendicular to the lateral direction (y), at least partly frustoconical in form converging towards the second plate (2b).
  12. Exchanger according to one of claims 1 to 9, characterised in that the decrease in the longitudinal section of the second channel (32) is caused by a lateral throttling (324) of said second channel (32) occurring in the direction of the second plate (2b).
  13. Exchanger according to claim 12, characterised in that the mixing device (3) further comprises at least one third channel (37) extending parallel to the first channel (31), said third channel (37) being arranged between the second channel (32) and the second plate (2b).
EP17822398.8A 2016-12-16 2017-12-12 Heat exchanger with a liquid/gas mixing device with improved channel geometry Active EP3555544B1 (en)

Applications Claiming Priority (2)

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FR1662581A FR3060721B1 (en) 2016-12-16 2016-12-16 HEAT EXCHANGER WITH LIQUID / GAS MIXER DEVICE WITH IMPROVED CHANNEL GEOMETRY
PCT/FR2017/053505 WO2018109352A1 (en) 2016-12-16 2017-12-12 Heat exchanger with a liquid/gas mixing device with improved channel geometry

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EP (1) EP3555544B1 (en)
JP (1) JP7019696B2 (en)
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DE3415807A1 (en) * 1984-04-27 1985-10-31 Linde Ag, 6200 Wiesbaden HEAT EXCHANGER
RU2005973C1 (en) * 1990-11-05 1994-01-15 Западно-Сибирский научно-исследовательский и проектно-конструкторский институт технологии глубокого разведочного бурения Heat exchanger
CN1236271C (en) * 2002-12-30 2006-01-11 西安交通大学 Low-temp. two-phase flow gas liquid homogeneous distribution board fin type phase change heat-exchanger
US9151540B2 (en) * 2010-06-29 2015-10-06 Johnson Controls Technology Company Multichannel heat exchanger tubes with flow path inlet sections
CN202382638U (en) * 2011-12-08 2012-08-15 杭州中泰深冷技术股份有限公司 Liquid uniform distribution device for aluminum plate-fin heat exchanger
CN103983138A (en) * 2014-05-16 2014-08-13 杭州杭氧股份有限公司 Large air flow two phase flow uniform distribution device of aluminum plate fin heat exchanger
CN203928851U (en) * 2014-05-16 2014-11-05 杭州杭氧股份有限公司 Aluminum plate-fin heat exchanger atm number two phase flow even distribution device
CN105486106A (en) * 2015-12-29 2016-04-13 无锡佳龙换热器股份有限公司 Gas-liquid uniform-distribution heat exchange device for natural gas
CN205784010U (en) * 2016-07-05 2016-12-07 天津商业大学 A kind of bleeder plate-fin heat exchanger

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US20200109894A1 (en) 2020-04-09
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RU2019120798A (en) 2021-01-11
JP7019696B2 (en) 2022-02-15
FR3060721B1 (en) 2019-08-16
FR3060721A1 (en) 2018-06-22
RU2019120798A3 (en) 2021-01-12
CN110234952A (en) 2019-09-13
JP2020514654A (en) 2020-05-21
WO2018109352A1 (en) 2018-06-21
RU2743818C2 (en) 2021-02-26

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