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    • 专利摘要:
    Plate heat exchanger (1) comprising a first series of passages (10) for channeling at least one refrigerant (F1) and a second series of passages (20) for channeling at least one heat-exchange fluid (F2), each passage ( 10, 20) being defined between two successive plates (2) and extending parallel to a longitudinal axis (z), at least one mixing device (3) arranged in at least one passage (10) of the first series, said device mixer (3) being configured to receive a liquid phase (61) and a gas phase (62) of the refrigerant (F1) and distribute a mixture of said phases (61, 62) in said at least one passage (10). According to the invention, at least one passage (20) of the second series adjacent to said at least one passage (10) of the first series comprises a heat exchange structure divided, along the longitudinal axis (z), into at least a first portion (100) and a second portion (200) juxtaposed along the longitudinal axis (z), the second portion (200) extending facing at least a portion of the mixing device (3) and being configured to have a heat exchange coefficient lower than the heat exchange coefficient of the first portion (100).
    公开号:FR3053452A1
    申请号:FR1656320
    申请日:2016-07-01
    公开日:2018-01-05
    发明作者:Ludovic Granados；Philippe Grigoletto；Natacha Haik-Beraud；Jean-Marc Peyron；Eduard Rosa；Sophie Lazzarini
    申请人:LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude；
    IPC主号:
    专利说明:

    Holder (s): AIR LIQUIDE, ANONYMOUS COMPANY FOR THE STUDY AND EXPLOITATION OF GEORGES CLAUDE PROCESSES Société anonyme.
    Extension request (s)
    Agent (s): AIR LIQUIDE.
    HEAT EXCHANGER COMPRISING A DEVICE FOR DISPENSING A LIQUID / GAS MIXTURE.
    FR 3 053 452 - A1 (57) Plate heat exchanger (1) comprising a first series of passages (10) for channeling at least one refrigerant (F1) and a second series of passages (20) for channeling at least one circulating fluid (F2), each passage (10, 20) being defined between two successive plates (2) and extending parallel to a longitudinal axis (z), at least one mixing device (3) arranged in at least one passage ( 10) of the first series, said mixing device (3) being configured to receive a liquid phase (61) and a gas phase (62) of the refrigerant (F1) and distribute a mixture of said phases (61,62) in said au minus one passage (10). According to the invention, at least one passage (20) of the second series adjacent to said at least one passage (10) of the first series comprises a heat exchange structure divided, along the longitudinal axis (z), into at least a first portion (100) and a second portion (200) juxtaposed along the longitudinal axis (z), the second portion (200) extending opposite at least part of the mixing device (3) and being configured to have a heat exchange coefficient lower than the heat exchange coefficient of the first portion (100).
    x
    i
    The present invention relates to a heat exchanger comprising series of passages for each of the fluids to be put into heat exchange relation, the exchanger comprising at least one mixing device configured to distribute at least one mixture with two liquid / gas phases in a series of passages.
    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.
    The technology commonly used for an exchanger is that of aluminum exchangers with brazed plates and fins, which make it possible to obtain very compact devices offering a large exchange surface.
    These exchangers include 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, each intended to vaporize refrigerant and others to condense circulating gas. Heat exchanges between fluids can take place with or without phase change.
    In order to ensure the proper functioning 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.
    The dimensioning of the exchanger is calculated by assuming a uniform distribution of the phases, and therefore a single temperature at the end of vaporization of the liquid phase, equal to the dew temperature of the mixture.
    For a mixture with several constituents, the temperature at the end of vaporization will depend on the proportion of liquid phase and gaseous phase in the passages.
    In the case of an uneven 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 relationship with the two-phase mixture have a temperature at the outlet of the exchanger higher than that provided, which consequently degrades the performance. of the heat exchanger.
    One solution for distributing the liquid and gaseous phases of the mixture as uniformly as possible consists in introducing them separately into the exchanger, then mixing them together only inside the exchanger.
    Document FR-A-2563620 describes such an exchanger in which a mixing device, such as a grooved bar, is inserted in the series of passages intended to channel the two-phase mixture. The mixing device has separate inputs 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.
    However, the liquid phase supplying the mixing device is then inevitably in a heat exchange situation with the circulating fluid or fluids circulating in the adjacent passages of the other series of passages. This can lead to the start of vaporization of the liquid phase within the corresponding inlets, thereby causing 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.
    In order to minimize the heat exchanges that may occur at the level of the mixing device, one solution would be to install the mixing device in an area of the exchanger in which no other fluid circulates. It would then be necessary to place the mixing device at one end of the exchanger, free from any means of evacuation or supply of fluid, which would mean restructuring the exchanger as a whole and would necessarily lead to increasing 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 specifics of the process require it.
    The object of the present invention is to solve all or part of the problems mentioned above, in particular by proposing a heat exchanger in which the distribution of the liquid and gaseous phases of a mixture is as uniform as possible, without complicating excessively the structure of the exchanger, nor increase its size.
    The solution according to the invention is then a heat exchanger comprising:
    - Several plates arranged parallel to each other so as to define a first series of passages for channeling at least one refrigerant and a second series of passages for channeling at least one circulating fluid to be put in heat exchange relationship with at least said refrigerant , each passage being defined between two successive plates and extending parallel to a longitudinal axis,
    - at least one mixing device arranged in at least one passage of the first series, said mixing device being configured to receive a liquid phase and a gaseous phase of the refrigerant and distribute a mixture of said phases in said at least one passage, characterized in that that at least one passage of the second series adjacent to said at least one passage of the first series comprises a heat exchange structure divided, along the longitudinal axis z, into at least a first portion and a second portion juxtaposed along the longitudinal axis, the second portion extending opposite at least part of the mixing device and being configured so as to have a heat exchange coefficient lower than the heat exchange coefficient of the first portion.
    Depending on the case, the exchanger of the invention may include one or more of the following technical characteristics:
    - Said first and second portions respectively comprise at least a first wave and at least a second wave, said first and second waves being juxtaposed along the longitudinal axis z and each having several wave legs connected alternately by vertices of wave and by wave bases succeeding each other in a direction of undulation, the second wave extending opposite at least a part of the mixing device and being configured so as to have a heat exchange coefficient lower than the coefficient heat exchange of the first wave.
    - the second wave has a density lower than the density of the first wave, the density of each wave being defined as the number of wave legs per unit of length measured along the direction of ripple.
    - The density of the second wave represents between 20% and 80%, preferably between 25% and 50%, of the density of the first wave.
    - the density of the second wave is between 6 and 15 legs per inch or fine perinch (1 inch = 2.54 centimeters).
    - Said first and second portions are formed from strips, the second portion being formed from at least one strip having a thickness greater than the thickness of at least one strip forming said first wave of the portion.
    - The second wave is a straight wave, the first wave being chosen from a straight wave, a perforated straight wave, a partially offset wave, a wave wave or a herringbone type wave.
    - the second portion extends at least opposite the entire mixing device.
    - The second portion has, parallel to the longitudinal axis, a length between 30 and 500 mm.
    the heat exchange structure is further divided, along the longitudinal axis, into a third portion, the second portion being configured so as to have a heat exchange coefficient less than or equal to the heat exchange coefficient of the third portion, the second portion being arranged between the first portion and the third portion.
    - The exchanger comprises first means for distributing or discharging the circulating fluid in said or said at least one passage from the second series of passages and second means for distributing a liquid or gaseous phase of the refrigerant in said au minus one passage from the first series to the mixing device.
    - The mixing device comprises separate inlets for a liquid phase and a gaseous phase of the refrigerant, said separate inlets being fluidly connected, via a common mixing volume, to at least one outlet for mixing said liquid and gaseous phases.
    the outlet for a two-phase liquid / gas mixture of the mixing device is located, along the longitudinal axis, at a first position in said at least one passage of the first series, the second portion extending at least from the first position to a second position located between the first position and the first means of distribution or evacuation of circulating fluid.
    - the second portion extends to the first means of distribution or evacuation of circulating fluid.
    - The second portion is formed by all or part of said first means of distribution or evacuation of circulating fluid.
    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, for example natural gas, by exchange of heat with at least one other fluid, for example natural gas.
    The term 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 entirely 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.
    The present invention will now be better understood thanks to the following description, given solely by way of nonlimiting example and made with reference to the attached diagrams, among which:
    Figure 1 is a schematic sectional view, in a plane parallel to the longitudinal and transverse axes, of a portion of a passage of the heat exchanger supplied with a mixture of two liquid-gas phases according to the invention;
    Figures 2A and 2B are schematic sectional views, along two planes perpendicular to that of Figure 1, illustrating an example of structure and operation of the mixing device of an exchanger according to Figure 1;
    Figure 3 is a schematic sectional view, in a plane parallel to the longitudinal axis and perpendicular to the lateral axis, of series of passages of the heat exchanger of Figure 1 according to an embodiment of the invention ;
    Figure 4 is another schematic sectional view, in a plane parallel to that of Figure 3 but in a direction opposite to that of Figure 3, of series of passages of the heat exchanger of Figure 1 according to another embodiment of the invention;
    Figures 5A and 5B are schematic sectional views of portions of the heat exchange structure according to an embodiment of the invention.
    The heat exchanger 1 according to the invention comprises a stack of plates 2 which extend along two dimensions, length and width, respectively along the longitudinal axis z and the lateral axis y. The plates 2 are arranged parallel one above the other with spacing and thus form a plurality of passages for fluids in indirect heat exchange relation via the plates 2. The lateral axis is orthogonal to the longitudinal axis z and parallel to the plates 2.
    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.
    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 shown in the Figure 1) to channel at least one circulating fluid F2, the flow of said fluids taking place generally along the longitudinal axis z. The passages 10 of the first series may be arranged, in whole or in part, alternately or adjacent to all or part of the passages 20 of the second series.
    In a manner known per se, the exchanger 1 comprises distribution and evacuation means 42, 43, 52, 53 configured to distribute the various fluids selectively in the passages 10, 20, as well as for evacuating said fluids from said passages 10, 20.
    The tightness of the passages 10, 20 along the edges of the plates 2 is generally ensured by lateral and longitudinal sealing strips 4 fixed to the plates 2. The lateral sealing strips 4 do not completely close 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 in the opposite corners. The openings placed one above the other are respectively joined in collectors of semi-tubular shape 40, 45, 50, 55, through which the distribution and evacuation of the fluids take place.
    In the representations of Figures 1, 3 and 4, the semitubular collectors 50, 45 are used for the introduction of fluids into the exchanger 1 and the semi-tubular collectors 40, 55 are used for evacuating these fluids from the exchanger 1.
    In this variant embodiment, the supply manifold for one of the fluids and the discharge manifold for the other fluid are located at the same end of the exchanger, the fluids F1, F2 thus circulating countercurrently in the exchanger 1.
    According to another alternative embodiment, the refrigerant and circulating fluid can also circulate 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.
    Preferably, the longitudinal axis is vertical when the exchanger 1 is in operation. The refrigerant F1 flows generally vertically and in the upward direction. Other directions and directions of flow of the fluids F1, F2 are of course conceivable, without departing from the scope of the present invention.
    Note that in the context of the invention, one or more refrigerants F1 and one or more circulating fluids F2 of different natures can flow within the passages 10, 20 of the first and second series of the same exchanger.
    The distribution and evacuation means 42, 43, 52, 53 advantageously comprise distribution waves 41, 44, 51, 54, arranged between two successive plates 2 in the form of corrugated sheets, which extend from the openings d 'entry and exit. The distribution waves 41, 44, 51, 54 ensure uniform distribution and recovery of the fluids over the entire width of the passages 10, 20.
    In addition, the passages 10, 20 advantageously comprise heat exchange structures disposed between the plates 2. These structures have the function of increasing the heat exchange surface of the exchanger. In fact, the heat exchange structures are in contact with the fluids circulating in the passages and transfer thermal fluxes by conduction to the adjacent plates 2, 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 2, in particular during assembly by brazing the exchanger and to avoid any deformation of the plates during the use of pressurized fluids. They also guide the flow of fluid in the exchanger passages.
    Preferably, these structures include heat exchange waves 11 which advantageously extend along the width and the length of the passages 10, 20, parallel to the plates 2, in the extension of the distribution waves 41, 44, 51, 54 according to the length of the passages 10, 20. The passages 10, 20 of the exchanger thus have a main part of their length constituting the heat exchange part proper, which is provided with a heat exchange structure, said main part being bordered by distribution parts filled with distribution waves 41, 44, 51, 54.
    Figure 1 illustrates a passage 10 of the first series 1 configured to dispense 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 liquid phase 61 and a gas phase 62 introduced separately into the exchanger 1 via a side collector 30 and the collector 50. The two phases 61, 62 are then mixed with each other by means of a mixing device 3 arranged in passage 10 and shown schematically in Figure 1. Advantageously, several passages 10, or even all of the passages 10 of the first series have a mixing device 3.
    According to an alternative embodiment, the mixing device 3 includes separate inputs 31, 32 for the liquid or gas phases of the refrigerant F1. Said separate inlets 31, 32 are fluidly connected, via a common mixing volume, to at least one outlet 33 for a two-phase liquid / gas mixture. The inputs 31, 32 and / or the outputs 33 can open at the end faces 35, 36 of the mixing device 3, or recede towards the inside of the device 3 with respect to said faces 35, 36.
    According to the embodiment illustrated in Figures 2A and 2B, the mixing device 3 is a bar, or rod, which extends in the width of the passage 10. The bar 3 has grooves 31, 32 machined perpendicular to each other and connected by holes 34.
    In the representations of Figures 1,2A and 2B, the gas phase 62 is introduced into a row of grooves 31 arranged parallel to the longitudinal axis z and the liquid phase 61 is introduced into at least one groove 32 which extends parallel to the transverse axis y.
    According to another exemplary embodiment, not illustrated, the mixing device 3 may comprise one or more tubes into which a phase of the refrigerant F1 is introduced, this phase emerging from the tube or tubes through holes drilled in their wall. The other phase is introduced upstream of the tube or tubes and flows around these tubes.
    Of course, the points of introduction of the liquid 61 and gaseous 62 phases into the exchanger can be reversed with respect to the representations given in the Figures.
    Figure 3 is a schematic sectional view, in a plane parallel to the longitudinal axis z and perpendicular to the lateral axis y, of the exchanger of Figure 1. There is seen a stack of passages 10, 20 of the first and second series, shown to a number limited to 4 for the sake of simplification.
    According to the invention, a heat exchange structure is housed in at least one passage 20 adjacent to passage 10 comprising the mixing device 3. This heat exchange structure is divided, along the longitudinal axis z, into at least one first portion 100 and a second portion 200, the second portion 200 extending opposite at least a portion of the mixing device 3. The first and second portions 100, 200 are juxtaposed along the longitudinal axis z of the exchanger 1, that is to say positioned end to end, as illustrated in Figures 3 and 4. In other words, The first and second portions 100, 200 follow one another, or are located immediately next to each other , along the z axis.
    The terms "facing" mean "opposite" or "at the level" of the mixing device 3. In other words, at least part of the second portion 200 is located along the axis z , at a position where part of the mixing device 3 is also located.
    According to the invention, the second portion 200 is configured so as to have a heat exchange coefficient lower than the heat exchange coefficient of the first portion 100.
    By positioning a structure of low thermal efficiency in a part of the adjacent passage located at the level of the mixing device, the heat exchanges which can take place with the circulating fluid are greatly reduced at the points of entry of the liquid and gaseous phases of the refrigerant. in the exchanger. This makes it possible to limit, or even avoid vaporization of the liquid phase of the refrigerant before it is mixed with the gaseous phase of said refrigerant. 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 various passages for the two-phase mixture.
    This solution has the advantages of being simple to implement, of not modifying the size of the exchanger and of not making its structure more complex. In addition, the heat exchange structure according to the invention makes it possible to reduce the heat transfers to the mixing device, and this without weakening the mechanical strength of the exchanger, since the spacer function between the plates 2 continues to be provided by the second portion 200.
    By heat exchange coefficient, or heat transfer coefficient, is meant a coefficient quantifying the flow of energy passing through the heat exchange structure, per unit of area, volume or length.
    The heat exchange coefficient can be defined as follows (in this case for a surface heat transfer):
    , W Α.ΔΤ.Δΐ with:
    - h: heat exchange coefficient, expressed in watts per square meter-kelvin (W m ~ 2 K 1 ),
    - ΔΟ: energy transferred in joules (J),
    - A: exchange area in square meters (m 2 ),
    - AT: temperature difference on either side of the exchange surface in kelvins or in degrees Celsius (K or ° C),
    - At: time interval in seconds (s).
    The heat transfer coefficient of a structure depends on intrinsic parameters, that is to say specific to the exchange structure itself, in particular the density of the wave forming the structure, the thickness of the wave, as well as extrinsic parameters, that is to say specific to the process implemented, in particular fluid flow and temperature difference between the fluids). The thermal transfer coefficient is determined using the Nusselt number (Nu) via the following relationship:
    h.L ·.
    Nude = with:
    - h: heat transfer coefficient,
    - L c , characteristic length,
    - k, thermal conductivity of the fluid.
    Many empirical correlations provide an equation for calculating the Nusselt number from which it is possible to extract the heat transfer coefficient.
    In particular, the heat exchange coefficient of a structure can be determined, in the case of liquid and gas monophasic fluid, by the Nusselt number calculated from the relationship below:
    Nu = CjRePr 173 with Nu: Nusselt number Cj: Colburn factor Re: Reynolds number Pr: Prandtl number
    In the two-phase liquid-gas case, the heat exchange coefficient can be determined using correlation methods known per se.
    In the context of the invention, the heat exchange coefficient of the second portion 200 and the heat exchange coefficient of the first portion 100 are compared to the same or almost identical theoretical measurement or determination method, the proper conditions the exchange process (ie extrinsic parameters) being identical or almost identical.
    Preferably, such a heat exchange structure is housed in several, or even all, of the passages 20 which are adjacent to passages 10 comprising a mixing device 3. Said structure extends over almost all, or even all, of the width of the passages 20 along the y axis, so that the structure is advantageously in contact with each plate 2 forming the passage 20.
    According to an advantageous embodiment of the invention, said first and second portions 100, 200 of the heat exchange structure respectively comprise a first wave and a second wave 100,
    200. The waves 100, 200 each include several wave legs 123,
    223, or fins 123, 223, connected alternately by wave vertices 121, 221 and by wave bases 122, 222 succeeding each other in directions of undulation D1, D2. The second wave 200 extends opposite at least part of the mixing device 3 and has a density lower than the density of the first wave. Reducing the density of the second wave 200 makes it possible to reduce the exchange surface of the structure opposite the mixing device, which makes it possible to reduce the heat exchanges by convection between the fluids circulating in the mixing device and in the passage adjacent to the second series.
    Preferably, the density of the second wave represents between 10% and 90%, preferably between 20% and 80%, more preferably between 25 and 50%, of the density of the first wave.
    In the context of the invention, the density of each wave 100, 200 is defined as the number of wave legs 123, 223 per unit of length measured along the respective directions of undulation D1, D2. To measure the density of a wave, we generally consider a given length of the wave along its direction of undulation, and we determine the number of wavelengths found on this length, or on a multiple of this length with subsequent division by said multiple, for greater accuracy. Generally, the length considered is one inch, or 2.54 cm. We speak of the number of struts per 2.54 cm or the number of fins per 2.54 cm.
    Referring to FIGS. 5A and 5B, the second wave 200 therefore has a distance p2 between two successive wave legs 223 greater than the distance p1 between two successive wave legs 123 from the first wave 100.
    Preferably, the density of the second wave 200 is between 6 and 15 legs per 2.54 centimeters, that is to say 6 and 15 legs per inch or fine perinch.
    As for the density of the first wave 100, it can be between 15 and 30 legs by 2.54 centimeters, that is to say 15 and 30 legs per inch or thin per inch, preferably between 18 and 25 legs by 2.54 centimeters, i.e. 18 and 25 legs per inch or fine perinch.
    Figures 5A and 5B illustrate exemplary embodiments in which the wave legs 123, 223 and the wave bases 122, 22 form, in cross section, rectilinear segments parallel to each other, the wave legs 123, 223 lying in planes perpendicular to directions D1, D2. Alternatively, the waves 100, 200 may have a cross section of sinusoidal, triangular or any other suitable shape.
    Advantageously, the first and second portions 100, 200 are each formed from one or more strips, that is to say thin metal sheets, preferably formed from aluminum or an aluminum alloy. These strips have thicknesses preferably between 0.2 and 0.6 mm.
    According to a particular embodiment, the second portion 200 is formed from a strip having a thickness greater than the thickness of the strip forming the first portion 100. This makes it possible to reduce the density of the second portion 200 while giving it sufficient rigidity to ensure good mechanical strength of the exchanger.
    In the context of the invention, the first and second waves can have heights h1, h2 typically between 3 and 10 mm. Preferably, the heights h1, h2 are chosen so that the first and second waves 100, 200 extend in almost all, if not all, of the width of the passage 20 in the transverse direction y.
    Preferably, the first wave 100 and / or the second wave 200 are arranged in the passages 10, 20 of the first and second series so that their directions of undulation D1, D2 are generally parallel to the direction of flow of the fluids in passages 10, 20 (so-called “easy way” arrangement). Such an arrangement offers better control of the process and greatly limits the risk of blocking the exchanger passages. Thus, with a vertical arrangement of the exchanger 1 in accordance with the representations of Figures 3 and 4, the waves 100, 200 are waves with vertical generators.
    It is also conceivable that the first wave 100 and / or the second wave 200 are arranged so that their directions of undulation D1, D2 are generally perpendicular to the direction of flow of the fluids (so-called "hard way" arrangement). According to the representations of Figures 3 and 4, the waves 100, 200 are then waves with horizontal generatrices.
    We can use the different types of waves usually used in exchangers of the brazed plate and fin type to form the first and second waves 100, 200. The waves can be chosen from known wave types such as straight waves , partial offset waves (of the "serrated" type in English), waves of herring bones or herringbone (of the "herringbone" type in English), perforated or not.
    As the first wave, a partial offset or herringbone wave will advantageously be used. This type of wave creates turbulence in the flow of circulating fluid F2, which has the effect of increasing the heat exchange coefficient of the wave.
    As a second wave, it is advantageous to use a straight wave or a perforated straight line this type of wave creating less trubulence in the flow of the fluid, and therefore being less thermally efficient.
    The first portion 100 is advantageously located along a direction parallel to the direction of flow of the refrigerant F1 in the passage 10, downstream of the second portion 200, as illustrated in FIGS. 3 and 4. Preferably, the second portion 200 extends opposite the whole of the mixing device 3. It can also extend beyond one and / or the other of the end faces 35, 36 of the mixing device 3. Advantageously, the second portion 200 extends at least beyond the end face 35 through which the liquid or gas phase of the refrigerant F1 is brought, as shown in FIG. 4.
    In this way, 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 are reduced as much as possible before mixing with the gas phase.
    Thus, in the representation given in the Figures, the second portion 200 extends, following the direction of flow of the circulating fluid
    F2 during operation of the exchanger, downstream of the mixing device 3.
    The mixing device 3 can have, parallel to the longitudinal axis z, a length of between 30 and 80 mm.
    Preferably, the second portion 200 has, parallel to the longitudinal axis z, a length at least equal to the length of the mixing device 3. The second portion 200 may have, parallel to the longitudinal axis z, a length between 30 and 300 mm.
    As explained above, the exchanger 1 comprises distribution and evacuation means 42, 43, 52, 53 configured to distribute the various fluids selectively in the passages 10, 20, as well as for evacuating the said fluids from the said passages 10, 20.
    In particular, the exchanger 1 may comprise at one end 1a, which is located in the lower part of the exchanger in the case where the exchanger operates in a vertical position and the refrigerant F1 circulates in the upward direction (as illustrated in FIGS. 1, 3 and 4), second means 52 for distributing a liquid or gaseous phase of the refrigerant F1 in the passage (s) 10.
    The same end 1a further comprises first means 42 which may be, as the case may be, means for distributing or discharging the circulating fluid F2 in said or said at least one passage 20.
    In the flow configuration illustrated in Figures 1, 3 and 4, in which the fluids F1, F2 flow against the current, the first means 42 are means for removing the circulating fluid F2.
    As shown schematically in Figures 3 and 4, said at least one outlet 33 for mixing the liquid 61 and gaseous phases 62 is located, along the longitudinal axis z, at a first position z1 in the passage 10 of the first series.
    Advantageously, the second portion 200 extends at least from the first position z1 to a second position z2 located between the first position z1 and the first means 42 for distributing or discharging the circulating fluid F2. In this way, the amount of heat that can be transferred from the circulating fluid F2 to one or the other of the two phases is limited as much as possible as long as these are not mixed by the device 3, and the exchanges of heat between the fluids upstream of the device 3, once the two phases have been mixed, that is to say in the main part of the length of the exchanger constituting the heat exchange part proper.
    Thus, the first portion 100 advantageously extends, parallel to the axis z, between the second portion 200 and the second means 53 for evacuating the refrigerant F1.
    According to a particular embodiment, the position z2 can correspond to the position of the inlet 31 for one or the other of the phases of the refrigerant F1 along the axis z.
    In particular, the position z1 can correspond to the position of the end face 36 of the mixing device 3 and / or the position z2 can correspond to the position of the end face 35 of the mixing device 3.
    Advantageously, the second portion 200 extends, parallel to the axis z, up to the first means 42 for distributing or discharging the circulating fluid F2.
    In particular, the second portion 200 can be formed by all or part of said first means 42 for distributing or evacuating circulating fluid F2.
    In the case where the heat exchange structure comprises a second portion 200 formed by a wave 200, the wave 200 is advantageously formed by an extension of the distribution wave 41 in the main part of the length of the exchanger constituting the heat exchange part proper.
    According to an alternative embodiment shown diagrammatically in FIG. 3, the heat exchange structure can also be divided, along the longitudinal axis z, into a third portion 300, the second portion 200 being arranged between the first portion 100 and the third serving 300.
    According to the invention, the second portion 200 is configured so as to have an exchange coefficient lower than the heat exchange coefficient of the third portion 300. In particular, the third portion 300 may include a third wave 300 of identical characteristics at the second wave 200.
    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 the skilled person can also be envisaged without departing from the scope of the invention.
    For example, in the exchanger configuration illustrated on the
    Figures, the liquid phase of the F1 fluid is injected laterally and the gas phase is injected at the lower end of the exchanger. Other injection configurations are of course conceivable, depending on the liquid-gas proportion in the two-phase mixture or according to the constraints imposed by the process to be implemented. Thus, one could consider injecting the gas phase laterally, upstream or downstream of the lateral injection point of the liquid phase.
    权利要求:
    Claims (15)
    [1" id="c-fr-0001]
    1. Heat exchanger (1) comprising:
    - Several plates (2) arranged parallel to each other so as to define a first series of passages (10) to channel at least one refrigerant (F1) and a second series of passages (20) to channel at least one circulating fluid (F2 ) to put in heat exchange relation
    A with at least said refrigerant (F1), each passage (10, 20) being defined between two successive plates (2) and extending parallel to a longitudinal axis (z),
    - at least one mixing device (3) arranged in at least one passage (10) of the first series, said mixing device (3) being configured to receive a liquid phase (61) and a gaseous phase (62) of the refrigerant ( F1) and distribute a mixture of said phases (61, 62) in said at least one passage (10), characterized in that at least one passage (20) of the second series adjacent to said at least one passage (10) of the first series comprises a heat exchange structure divided, along the longitudinal axis (z), into at least a first portion (100) and a second portion (200) juxtaposed along the longitudinal axis (z), the second portion (200) extending opposite at least part of the mixing device (3) and being configured so as to have a heat exchange coefficient lower than the heat exchange coefficient of the first portion (100).
    [2" id="c-fr-0002]
    2. Exchanger according to claim 1, characterized in that said first and second portions (100, 200) respectively comprise at least a first wave and at least a second wave, said first and second waves being juxtaposed along the longitudinal axis (z) and each having several wave legs (123, 223) connected alternately by wave vertices (121, 221) and by wave bases (122, 222) succeeding each other in a ripple direction ( D1, D2), the second wave extending opposite at least part of the mixing device (3) and being configured so as to have a heat exchange coefficient lower than the heat exchange coefficient of the first wave.
    [3" id="c-fr-0003]
    3. Exchanger according to claim 2, characterized in that the second wave has a density lower than the density of the first wave, the density of each wave being defined as the number of wave legs per unit of length measured along the ripple direction (D1, D2).
    [4" id="c-fr-0004]
    4. Exchanger according to claim 3, characterized in that the density of the second wave represents between 20% and 80%, preferably between 25% and 50%, of the density of the first wave.
    [5" id="c-fr-0005]
    5. Exchanger according to one of claims 3 or 4, characterized in that the density of the second wave is between 6 and 15 legs per inch (1 inch = 2.54 centimeters).
    [6" id="c-fr-0006]
    6. Exchanger according to one of the preceding claims, characterized in that said first and second portions (100, 200) are formed from strips, the second portion (200) being formed from at least one strip having a thickness greater than the thickness of at least one strip forming said first wave of the portion (100).
    [7" id="c-fr-0007]
    7. Exchanger according to one of claims 2 to 6, characterized in that the second wave is a straight wave, the first wave being chosen from a straight wave, a perforated straight wave, a partially offset wave, a wave wave or a wave of the type "with herringbones".
    [8" id="c-fr-0008]
    8. Exchanger according to one of the preceding claims, characterized in that the second portion (200) extends at least opposite the entire mixing device (3).
    [9" id="c-fr-0009]
    9. Exchanger according to one of the preceding claims, characterized in that the second portion (200) has, parallel to the longitudinal axis (z), a length between 30 and 500 mm.
    [10" id="c-fr-0010]
    10. Exchanger according to one of the preceding claims, characterized in that the heat exchange structure is further divided, along the longitudinal axis (z), into a third portion (300), the second portion (200) being configured to have a heat exchange coefficient less than or equal to the heat exchange coefficient of the third portion (300), the second portion (200) being arranged between the first portion (100) and the third portion (300) .
    [11" id="c-fr-0011]
    11. Exchanger according to one of the preceding claims, characterized in that it comprises, at the same end of the exchanger, first means (42) for distributing or discharging the circulating fluid (F2) in said or said at least one passage from the second series of passages (20) and second means (52) for distributing a liquid or gaseous phase of the refrigerant (F1) in said at least one passage (10) from the first series to the mixing device (3).
    [12" id="c-fr-0012]
    12. Exchanger according to one of the preceding claims, characterized in that the mixing device (3) comprises separate inlets (31, 32) for a liquid phase (61) and a gas phase (62) of the refrigerant (F1) , said separate inlets (31, 32) being fluidly connected, via a common mixing volume, to at least one outlet (33) for mixing said liquid and gaseous phases (61,62).
    [13" id="c-fr-0013]
    13. Exchanger according to claim 12, characterized in that the outlet (33) for a two-phase liquid / gas mixture of the mixing device (3) is located, along the longitudinal axis (z), at a first position (z1 ) in said at least one passage (10) of the first series, the second portion (200) extending at least from the first position (z1) to a second position (z2) located between the first position ( z1) and the first means (42) of distribution or evacuation of circulating fluid (F2).
    [14" id="c-fr-0014]
    14. Exchanger according to one of claims 11 to 13, 5 characterized in that the second portion (200) extends to the first means (42) of distribution or evacuation of circulating fluid (F2).
    [15" id="c-fr-0015]
    15. Exchanger according to one of claims 11 to 14, characterized in that the second portion (200) is formed by all or part
    10 of said first means (42) of distribution or evacuation of circulating fluid (F2).
    1/5 φ éi
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    BE542659A|
    同族专利:
    公开号 | 公开日
    EP3479044B1|2020-08-05|
    EP3479044A1|2019-05-08|
    CN107560472B|2021-03-02|
    US11022377B2|2021-06-01|
    US20190242651A1|2019-08-08|
    RU2019101427A|2020-07-20|
    CN207147287U|2018-03-27|
    WO2018002509A1|2018-01-04|
    FR3053452B1|2018-07-13|
    CN107560472A|2018-01-09|
    RU2731464C2|2020-09-03|
    RU2019101427A3|2020-07-20|
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    法律状态:
    2017-07-24| PLFP| Fee payment|Year of fee payment: 2 |
    2018-01-05| PLSC| Search report ready|Effective date: 20180105 |
    2018-07-25| PLFP| Fee payment|Year of fee payment: 3 |
    2020-07-21| PLFP| Fee payment|Year of fee payment: 5 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1656320A|FR3053452B1|2016-07-01|2016-07-01|HEAT EXCHANGER COMPRISING A DEVICE FOR DISPENSING A LIQUID / GAS MIXTURE|
    FR1656320|2016-07-01|FR1656320A| FR3053452B1|2016-07-01|2016-07-01|HEAT EXCHANGER COMPRISING A DEVICE FOR DISPENSING A LIQUID / GAS MIXTURE|
    RU2019101427A| RU2731464C2|2016-07-01|2017-06-27|Heat exchanger comprising a device for distribution of liquid-gas mixture|
    PCT/FR2017/051709| WO2018002509A1|2016-07-01|2017-06-27|Heat exchanger comprising a device for distributing a liquid/gas mixture|
    EP17746159.7A| EP3479044B1|2016-07-01|2017-06-27|Heat exchanger comprising a device for distributing a liquid/gas mixture|
    US16/312,078| US11022377B2|2016-07-01|2017-06-27|Heat exchanger comprising a device for distributing a liquid/gas mixture|
    CN201720800165.6U| CN207147287U|2016-07-01|2017-06-30|Heat exchanger|
    CN201710522395.5A| CN107560472B|2016-07-01|2017-06-30|Heat exchanger comprising a device for distributing a liquid/gas mixture|
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