• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Heat exchanger (1) comprising a plurality of plates (2) arranged parallel to one another so as to define a first series of passages (10) for channeling at least a first fluid (F1) and a second series of passages (20) for channeling at at least one second fluid (F2) to be placed in heat exchange relation with at least said first fluid (F1), a mixing device (3) being arranged in said at least one passage (10) of the first series and comprising at least a first channel (31) for the flow of a first phase (61) of the first fluid (F1) in a longitudinal direction (z), at least a second channel (32) for the flow of a second phase ( 62) of the first fluid (F1), the first channel (31) comprising an inlet (311) for supplying said first channel (31) and a plurality of orifices (34) arranged downstream of the inlet (311) and each connecting, fuidically, the first channel (31) to the second channel (32). According to the invention, the first channel (31) has a cross section, measured perpendicular to the longitudinal direction (z), variable along said longitudinal direction (z).
    公开号:FR3064346A1
    申请号:FR1752476
    申请日:2017-03-24
    公开日:2018-09-28
    发明作者:Natacha Haik-Beraud；Philippe Grigoletto；Sophie LAZZARINI；Jean-Marc Peyron；Guillaume CARDON
    申请人:Air Liquide SA；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 WITH LIQUID / GAS MIXING DEVICE WITH REGULATING CHANNEL PORTION.
    FR 3 064 346 - A1 (57) Heat exchanger (1) comprising several plates (2) arranged parallel to each other so as to define a first series of passages (10) for channeling at least a first fluid (F1) and a second series of passages (20) for channeling at least one second fluid (F2) to be put in heat exchange relation with at least said first fluid (F1), a mixing device (3) being arranged in said at least one passage (10 ) of the first series and comprising at least a first channel (31) for the flow of a first phase (61) of the first fluid (F1) in a longitudinal direction (z), at least a second channel (32) for the flow of a second phase (62) of the first fluid (F1), the first channel (31) comprising an inlet (311) for supplying said first channel (31) and several orifices (34) arranged downstream of the input (311) and each fluidly connecting the first channel (31) to the second channel (32). According to the invention, the first channel (31) has a cross section, measured perpendicular to the longitudinal direction (z), variable along said longitudinal direction (z).

    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 heat exchange waves are inserted, formed by a succession of fins or wave legs, thus constituting a stack of vaporization passages and condensation passages, some of which may be intended for spray refrigerant and the 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 first fluid 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 fluid or fluids in exchange relationship 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.
    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 grooved bar is inserted in the series of passages intended to channel the two-phase mixture. This mixing device has separate channels for a liquid phase and a gaseous phase and an outlet for distributing the liquid-gas mixture to the heat exchange zone.
    A problem which arises with this type of mixing device relates to the distribution of the liquid-gas mixture in the width of the passage incorporating the mixing device. In order to mix the two phases, the mixing device generally comprises a first channel for the flow of one phase. This channel is provided with a series of orifices arranged along the channel, each orifice being in fluid communication with the second channel for the flow of the other phase. When the inlet of the first channel is supplied with fluid, the speed of flow of the fluid will tend to decrease as the fluid flows along the channel. This is due to the fact that the fluid flow decreases when the orifices are supplied.
    However, the orifices are generally machined perpendicular to the longitudinal direction of the fluid and are therefore less well supplied when the speed of the fluid is greater. The orifices arranged on the side of the channel entry therefore tend to be undernourished, while the ports furthest from the channel entrance are overfed. This results in an uneven introduction of the phase considered in the channel for the other phase, and hence an uneven distribution of the liquid-gas mixture in the width of the passage of the exchanger.
    In order to minimize this phenomenon, one solution is to supply the channel in question with two opposite inputs to the channel in order to minimize the longitudinal speed of the fluid. However, this solution is insufficient when we aim for a very homogeneous distribution, especially when the processes are very sensitive to maldistribution.
    Increasing the number of channels is possible but also has its limits: from the point of view of the mechanical strength and soldering of the device, the number of channels cannot be multiplied too much.
    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 a first fluid and a second series of passages for channeling at least a second fluid to be put in heat exchange relation with at least said first fluid, a mixing device being arranged in said at least one passage of the first series and comprising:
    - at least a first channel for the flow of a first phase of the first fluid in a longitudinal direction,
    - at least one second channel for the flow of a second phase of the first fluid,
    - The first channel comprising several orifices fluidly connecting the first channel to the second channel, characterized in that the first channel has a cross section, measured perpendicular to the longitudinal direction, variable along said longitudinal direction.
    Depending on the case, the exchanger of the invention may include one or more of the following technical characteristics:
    - The first channel comprises at least one change in cross section in the longitudinal direction.
    the first channel comprises a first inlet for a supply with the first phase and at least a first portion downstream of the first inlet, the cross section of the first channel at the level of the first portion being greater than the cross section of the first channel at level of the first entry.
    - The first portion comprises at least one recess formed in at least part of a wall of the first channel.
    - The mixing device comprises several first channels following one another in a lateral direction orthogonal to the longitudinal direction, said at least one recess opening into the first successive channel.
    the first channel comprises a first inlet for a supply with the first phase and at least a first portion arranged downstream of the first inlet, the cross section of the first channel at the level of the first portion being less than the cross section of the first channel at the first entrance.
    - The first channel comprises several first portions arranged along the longitudinal direction.
    - Said several first portions have different cross sections.
    - The cross sections of said several first portions decrease in the longitudinal direction.
    the first channel also comprises a second inlet for supplying the first phase and at least a second portion arranged downstream of said second inlet, the cross section of the first channel at the level of the second portion being less than the cross section of the first channel at the second input.
    - The first channel comprises several second portions arranged along the longitudinal direction.
    - The cross sections of said second portions decrease in the direction of the first entry.
    - At least one orifice is arranged at the level of the first and / or second portions.
    - the first and / or second portions extend in the longitudinal direction.
    the first channel comprises a first inlet for supplying said first channel with said first phase of the first fluid, said orifices being arranged downstream of the first inlet and forming a series of orifices comprising a first orifice arranged on the side of the first inlet of the first channel and a last opening.
    - At least one orifice is arranged at the level of each first first portion.
    - the first fluid is a refrigerant.
    - the second fluid is a circulating fluid.
    According to another aspect, the invention relates to a method of distributing a two-phase liquid / gas mixture within a heat exchanger according to the invention, as well as a method of heat exchange between said mixture two liquid / gas phases and at least one other fluid. The liquid-gas mixture can be a refrigerant or circulating fluid.
    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 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 view, in a sectional plane parallel to the plates of a heat exchanger, of a portion of a passage of an exchanger supplied with a mixture of two liquid-gas phases according to one embodiment of the invention;
    Figure 2 is a schematic sectional view, along a plane perpendicular to that of Figure 1, of an embodiment of a mixing device according to the invention;
    Figure 3 is a schematic three-dimensional view illustrating an embodiment of a mixing device according to the invention;
    Figures 4 and 5 are schematic three-dimensional views illustrating alternative embodiments of a mixing device according to the invention;
    Figure 6 is a partial sectional view, along a section plane parallel to that of Figure 1, of another embodiment of a mixing device according to the invention;
    Figure 7 is a partial sectional view, along a section plane parallel to that of Figure 1, of another embodiment of a mixing device according to the invention.
    Figure 1 illustrates a heat exchanger 1 comprising a stack of plates 2 (not visible) which extend in two dimensions, parallel to a plane defined by the directions z and y. The plates 2 are arranged parallel to one another with spacing and thus form a plurality of passages for fluids in relation to indirect heat exchange via said plates.
    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 comprise 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 first fluid F1, and a second series of passages 20 (not visible in the Figure 1) to channel at least one second fluid F2, the flow of said fluids taking place generally in the lateral direction y. 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 40, 52, 45, 54, 55 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 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 representation of FIG. 1, the semi-tubular collectors 50, 45 are used for the introduction of the 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 first and second fluids can also circulate cocurrently, 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 direction is oriented vertically there when the exchanger 1 is in operation. The first fluid 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 first refrigerants F1 and one or more second fluids F2 of different natures can flow within passages 10, 20 of the first and second series of the same exchanger.
    Advantageously, the exchanger according to the invention uses a first refrigerant F1 two-phase fluid and a second circulating F2 fluid.
    The distribution and evacuation means of the exchanger advantageously include distribution waves 51, 54, arranged between two successive plates 2 in the form of corrugated sheets, which extend from the inlet and outlet openings. The distribution waves 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 length of the passages 10, 20, parallel to the plates 2, in the extension of the distribution waves 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 heat exchange part proper, which is furnished with a heat exchange structure, said main part being bordered by distribution parts. filled with distribution waves 51, 54.
    Figure 1 illustrates a passage 10 of the first series 1 configured to distribute a first fluid F1 in the form of a two-phase liquid-gas mixture. The first fluid F1 is separated in a separator device 6 into a first phase 61 and a second phase 62 introduced separately into the exchanger 1 via a lateral 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 the passage 10 and shown schematically in Figure 1. Advantageously, several passages 10, or even all of the passages 10 of the first series comprises a mixing device 3.
    Figure 2 is a schematic sectional view, in a plane perpendicular to that of Figure 1, of a mixing device advantageously consisting of a bar, or rod, housed in a passage 10.
    In the illustrated configuration, the mixing device 3 comprises several first channels 31a, 31b, ... adapted for the flow of a first phase 61 of the fluid F1.
    The first channel (s) 31 extend in the longitudinal direction z.
    Note that the direction of extent of a channel or a portion of channel means a direction of overall extent, the walls of the channel or of the portion of channel not necessarily being rectilinear in direction longitudinal z.
    Advantageously, several orifices 34 (only one visible in FIG. 2) follow one another in the longitudinal direction z. Note that the orifices 34 are not necessarily arranged in rectilinear alignment along the longitudinal direction z. In the example illustrated, the first phase 61 is liquid and the longitudinal direction z corresponds to the direction of flow of the first phase 61 in the first channels 31a, 31b ... These orifices are arranged so as to fluidly connect the first channel 31a to at least one second channel 32 adapted for the flow of the second phase 62, in the example illustrated a second gas phase 62.
    The first channels 31 a, 31 b ... and the second channels 32a, 32b, ... extend parallel to the plates 2. The orifices 34 of the various first channels 31a, 31b, ... can be staggered, as shown in Figures 3 to 5, which promotes a more homogeneous distribution of the first phase 61 in the second channels 32a, 32b, ...
    Preferably, the mixing device 3 according to the invention extends in the section of the passage 10 over almost all, or even all, of the height of the passage 10, so that the mixing device is in contact with each plate 2a , 2b forming the passage 10.
    The mixing device 3 is advantageously fixed to the plates 2 by brazing.
    The mixing device 3 is advantageously of generally parallelepiped shape.
    The mixing device 3 may have, parallel to the longitudinal direction y, a first dimension between 20 and 200 mm and, parallel to the lateral direction z, a second dimension between 100 and 1400 mm.
    According to the invention, the cross section of the first channel 31 varies along said longitudinal direction z.
    Note that in the context of the invention, the cross section of the first channel 31 means the section of the first channel 31 measured, in units of area, perpendicular to the longitudinal direction z. Thus, with reference to Figure 2, the cross section of the first channel 31 is measured in a plane defined by the directions x and y.
    The fact that the first channel has a cross section whose value varies according to the position considered along the z direction makes it possible to minimize, even eliminate, the effect of variable speed along the z direction of the first channel described above. . When the first phase 61 flows at a given speed, it is thus possible to modify or regulate it along the direction z, by adjusting the dimension of the cross section, in order to control the supply of the orifices 34 the along the first channel 31. This results in a more homogeneous supply of the orifices and therefore a more homogeneous distribution of the liquid-gas mixture in the width of the passage 10. This solution has the advantages of being simple to implement, of not not modify the size of the exchanger and not to complicate its structure.
    The variation in the cross section of the first channel 31 can be induced locally or gradually in the longitudinal direction z, along all or part of the first channel 31.
    Preferably, the first channel 31 comprises at least one change in cross section occurring in the longitudinal direction z. This change may be sudden or gradual and may consist of an increase or a decrease in said cross section.
    According to one embodiment of the invention, the first channel 31 comprises a first inlet 311 by which the first phase 61 is introduced, during the operation of the exchanger, into the first channel 31. At least a first portion 310 of the first channel 31, located downstream of the first inlet 311, has a cross section greater than the cross section of the first channel 31 at the level of the first inlet 311.
    The arrangement of a portion of channel 310 with an enlarged passage section on the path of the first phase 61 in the first channel 31 makes it possible to reduce its flow speed and therefore to favor its distribution in an orifice 34 arranged in or in downstream of said portion 310.
    Thus, the first portion 310 can be shaped so as to induce a decrease in the flow speed of the first phase 61. In other words, the first portion 310 can be shaped so that when the first phase 61 s' flows at a first speed V1 from the first inlet 311, said portion 310 induces a reduction in the flow speed such that phase 61 flows at a second speed V2, less than V1, at the level of said portion 310. It it is thus possible to compensate for the effect of greater speed at the input of the first channel 31.
    Advantageously, the first channel 31 comprises several orifices 34 forming a series with a first orifice arranged on the side of the entry 311 and a last orifice located on the side of the end opposite to the entry 311. A first portion 310 is arranged preferably at least at the level of the first orifice.
    Note that the terms "upstream" and "downstream" are used with reference to the overall flow direction of the first phase 61 from the entrance to the first channel 31 considered.
    Alternatively or additionally, the first channel 31 can comprise at least a first portion 310 having a cross section less than the cross section of the first channel 31 at the level of the first inlet 311.
    Thus, the first portion 310 can be shaped to induce an increase in the flow speed and, for example, compensate for the losses of frictional loads which can take place along the longitudinal direction z.
    Preferably, the first portion 310 with modified section has a constant or almost constant cross section along the direction z.
    Said first portion 310 advantageously extends in the longitudinal direction z.
    The dimensioning, the number and the distribution of first portions 310 arranged in the same first channel 31 or in several first channels 31a, 31b, ... is adapted according to the desired fluid velocity profiles along the same channel and / or between several first channels arranged in the device 3.
    Advantageously, at least one orifice 34 of the first channel 31 is arranged at or downstream of the first portion 310.
    Figures 3 to 5 illustrate alternative embodiments of mixing devices 3 according to the invention in which the first portion 310 has a cross section greater than that of the first inlet 311.
    The increase in the cross section of the first channel 31 at the level of the first portion 310 can result from an increase in the width of said first channel 31, measured in the longitudinal direction y and / or result from an increase in the depth of the first channel 31, measured in a direction x orthogonal to the directions y and z.
    More precisely, and as illustrated in FIG. 4, the first channel 31 typically comprises a first inlet 311 for supplying with the first phase 61. The orifices 34 are arranged downstream of the inlet 311. If the channel 31 has a first cross section value S1 given at the first inlet 311, said portion 310 has a second fluid passage section S2 larger than S1.
    Preferably, the first portion 310 extends, in the longitudinal direction z, at least on either side of an orifice 34. It is thus possible to compensate for a change in flow speed induced by the supply d an orifice 34 for supplying the following orifice 34 at an identical or almost identical speed.
    Advantageously, the S2 / S1 ratio is greater than or equal to 1.2, preferably between 1.2 and 2, so as to be able to significantly improve the distribution of the first phase 61 in the orifice or orifices 34 considered.
    As seen in Figures 3 to 5, the mixing device 3 generally forms a parallelepiped delimited in particular by a first surface 3a intended to be arranged facing a plate 2 of the exchanger and a second surface 3b arranged opposite d another plate 2. The first and second surfaces 3a, 3b preferably extend generally parallel to the plates 2. The mixing device 3 is preferably arranged in the passage 10 so that the first and second surfaces 3a, 3b are located in contact with the plates 2.
    The first channels 31a, 31b are advantageously in the form of recesses whose length is large compared to the width, measured in the lateral direction y or the height, measured in a vertical direction x orthogonal to the directions y and z, of said channels.
    The device 3 may comprise several lateral channels 32 succeeding each other within the device 3 and / or several first channels 31. FIGS. 3 to 5 illustrate a device 3 comprising a row of first channels 31 parallel to each other and a row of second channels 32 parallel to each other.
    It being specified that the channels 31 and 32 can be of distinct and identical shape and number. The distances between the first successive channels 31 and the distances between the second successive channels 32 can also vary.
    Note that the pitch between the orifices 34 succeeding each other in a first channel 31 may be constant along the longitudinal direction z, or else vary so as to compensate for the phenomena of unequal speed previously described. Typically, the pitch between the holes 34 is tighter on the side of the inlet 311 of the first channel 31.
    The first and / or second channels 31, 32 can be formed from internal recesses formed within the mixing device 3. They can also be through at the surfaces 3a and / or 3b and form main grooves 31, 32, as illustrated in Figures 3 to 5. The first and / or second channels 31, 32 may have cross sections of different shape, rectangular, circular or other, preferably rectangular cross sections.
    According to one embodiment, the first portion 310 comprises a recess formed in at least part of a wall of the first channel 31.
    Advantageously, at least one orifice 34 is arranged in said recess. The arrangement of an orifice 34 at the level of the recess makes it possible, thanks to the change in the direction of flow of the fluid induced locally by the recess, to supply the orifice 34 with a reduced flow speed and therefore better the supply, which is particularly advantageous for the orifices 34 located on the side of the inlet 311 of the channel 31.
    Several recesses can be arranged in the same first channel 31 and / or in one or more successive first channels 31. Said recesses may have a cross section of rounded, rectangular shape or any other suitable shape. The number of orifices placed in the recesses, as well as the shape and the dimension of the recesses can be variable along the first channel 31. The production of these recesses can for example be done by milling.
    According to a particular configuration, at least one recess 310 formed in at least part of a wall of the first channel 31a opens into the first successive channel 31b.
    FIG. 3 representing an example of a mixing device 3 in the form of a bar, orifices 34 being drilled in the bottom of several first channels 31. The recess comprises a secondary groove 310 formed in the bottom wall of the first channel 31. Said secondary groove may extend along the channel, at the orifices, over all or part of the length of the channel.
    As a variant, the recess can be formed in one or more of the side walls of several first channels 31.
    The bottom wall of the first channels 31 is preferably generally rectilinear in the longitudinal direction z.
    FIG. 4 illustrates another example of a mixing device 3 in which the recess is formed in a side wall of several first channels 31, thus forming a network of niches 310. All or part of the orifices 34 can be arranged in these niches. The turn followed by the flow of the fluid at the entry of the niches makes it possible to reduce the speed upstream of the orifices and facilitates the flow of the flow towards these orifices. In addition, the supply of an orifice 34 located in such niches is done at a controlled flow rate which is that of the first phase 61 around the orifice, while minimizing, or even eliminating, the variations in the flow rate of the first phase 61 flowing in the main part of the first channel 31.
    These niches preferably have dimensions comparable to the width of the first channel 31 and are of considerable height with respect to the height of the channel 31, said heights being measured in the direction x.
    In the example illustrated in FIG. 5, all or part of the orifices 34 is arranged in niches of a first channel 31a, said niches being dimensioned so that they communicate with another first channel 31b immediately adjacent. A network of orifices 34 is thus obtained supplied at reduced speed and in a more homogeneous manner. Several network configurations can be envisaged depending on the desired distribution.
    Figures 6 and 7 illustrate alternative embodiments of mixing devices 3 according to the invention in which the first portion 310 has a smaller cross section than that of the first inlet 311. In addition, the mixing devices 3 can have one or many of the features mentioned above.
    Figure 6 is a partial view of an embodiment in which the first channel 31 comprises several first portions 310 having cross sections smaller than that of the first inlet 311.
    Thus, the first portions 310 are shaped so as to induce a reduction in the passage section which compensates for the reduction in the flow rate of the fluid as the successive orifices are supplied. This tends to standardize the flow speed of the fluid along the first channel 31 and therefore to a more homogeneous supply of the orifices.
    According to a particular embodiment, the sections of fluid passages of the first portions 310 decrease in the longitudinal direction z.
    As seen in Figure 6, the first channel 31 has a first cross section S1 at the entrance 311. The first phase 61 then flows at a first portion 310 having a second lower cross section S2 to said first section S1. The first channel 31 may also include another first portion 310 arranged downstream of the first portion and having a third section S3 lower than the second section S2.
    Advantageously, the section ratio S2 / S1 and / or the ratio between two first successive portions 310 is less than or equal to 0.8, preferably between 0.5 and 0.8. This makes it possible to significantly improve the distribution of the first phase 61 in the orifice (s) 34 considered.
    As illustrated in FIG. 6, the decrease in the cross section of the first channel 31 can result from a decrease in the width of the first channel 31, measured in the longitudinal direction y. Alternatively or additionally, it is also possible to envisage a reduction in the cross section of the first channel 31 resulting from a reduction in its height, measured in the vertical direction x.
    Figure 7 partially illustrates another particularly advantageous embodiment of the invention when the first channel 31 has two inputs for supplying the first phase 61. More specifically, the first channel 31 comprises a first input 311 and a second entry 312 for the injection of the first phase 61. The second entry is preferably arranged at a second end of the first channel situated opposite a first end comprising the first entry
    311.
    The first channel 31 comprises at least a second portion 313 arranged downstream of said second inlet 312, the cross section of the first channel 31 at the level of the second portion 313 being less than the cross section of the first channel 31 at the level of the second inlet
    312.
    The speed of flow of the first phase 61 is thus even better adapted as it flows so as to gradually compensate for the variation in flow rate during the passage of the first phase 61 above the successive orifices 34 along the first channel 31.
    Preferably, the first channel 31 comprises several second portions 313 arranged along the longitudinal direction z. The cross sections of said second portions 313 decrease in the direction of the first inlet 311.
    Advantageously, the ratio between the sections of the first channel 31 at the level of the second portion 313 and of the second inlet 312 and / or the ratio between two second successive portions 313 is less than 0.8, preferably between 0.5 and 0.8.
    Figure 7 illustrates the case where the first and second portions 310, 313 are arranged symmetrically with respect to the center of the first channel 31. Said portions could however be arranged in different numbers and have different cross sections on either side from the center of the first channel 31.
    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, the exchanger according to the invention is mainly described in the case where the passages 10, 20 extend in the longitudinal direction y, the first longitudinal channel 31 extending in the longitudinal direction z and the lateral 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 longitudinal channel 31 extending in the lateral direction y and a lateral channel 32 extending in the longitudinal direction z. The lateral y and longitudinal z directions may also not be orthogonal to each other.
    权利要求:
    Claims (14)
    [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) for channeling at least a first fluid (F1) and a second series of passages (20) for channel at least one second fluid (F2) to be put in heat exchange relationship with at least said first fluid (F1), a mixing device (3) being arranged in said at least one passage (10) of the first series and comprising :
    - at least a first channel (31) for the flow of a first phase (61) of the first fluid (F1), said first channel (31) extending in a longitudinal direction (z),
    - at least one second channel (32) for the flow of a second phase (62) of the first fluid (F1),
    - the first channel (31) comprising several orifices (34) fluidly connecting the first channel (31) to the second channel (32), characterized in that the first channel (31) has a cross section, measured perpendicular to the longitudinal direction ( z), variable along said longitudinal direction (z).
    [2" id="c-fr-0002]
    2. Exchanger according to claim 1, characterized in that the first channel (31) comprises at least one change in cross section in the longitudinal direction (z).
    [3" id="c-fr-0003]
    3. Exchanger according to one of claims 1 or 2, characterized in that the first channel (31) comprises a first inlet (311) for a supply with the first phase (61) and at least a first portion (310) in downstream of the first inlet (311), the cross section of the first channel (31) at the level of the first portion (310) being greater than the cross section of the first channel (31) at the level of the first inlet (311).
    [4" id="c-fr-0004]
    4. Exchanger according to one of the preceding claims, characterized in that the first portion (310) comprises at least one recess formed in at least part of a wall of the first channel (31).
    [5" id="c-fr-0005]
    5. Exchanger according to claim 4, characterized in that the mixing device (3) comprises several first channels (31a, 31b, ...) succeeding each other in a lateral direction (y) orthogonal to the longitudinal direction (z), said at least one recess opening into the first successive channel (31b).
    [6" id="c-fr-0006]
    6. Exchanger according to one of claims 1 or 2, characterized in that the first channel (31) comprises a first inlet (311) for a supply with the first phase (61) and at least a first portion (310) arranged downstream of the first inlet (311), the cross section of the first channel (31) at the level of the first portion (310) being less than the cross section of the first channel (31) at the level of the first inlet (311).
    [7" id="c-fr-0007]
    7. Exchanger according to one of claims 3 to 6, characterized in that the first channel (31) comprises several first portions (310) arranged along the longitudinal direction (z).
    [8" id="c-fr-0008]
    8. Exchanger according to claim 7, characterized in that said several first portions (310) have different cross sections.
    [9" id="c-fr-0009]
    9. Exchanger according to one of claims 6 to 8, characterized in that the cross sections of said several first portions (310) decrease in the longitudinal direction (z).
    [10" id="c-fr-0010]
    10. Exchanger according to one of claims 3 to 9, characterized in that the first channel (31) further comprises a second inlet (312) for a supply with the first phase (61) and at least a second portion (313 ) arranged downstream of said second inlet (312), the cross section of the first channel (31) at the second portion (313) being less than the cross section of the first channel (31) at the second inlet (312) ).
    5
    [11" id="c-fr-0011]
    11. Exchanger according to claim 10, characterized in that the first channel (31) comprises several second portions (313) arranged along the longitudinal direction (z).
    [12" id="c-fr-0012]
    12. Exchanger according to claim 11, characterized in that
    10 the cross sections of said second portions (313) decrease in the direction of the first entry (311).
    [13" id="c-fr-0013]
    13. Exchanger according to one of claims 3 to 12, characterized in that at least one orifice (34) is arranged at the level of the first and / or
    15 second portions (310, 313).
    [14" id="c-fr-0014]
    14. Exchanger according to one of claims 3 to 13, characterized in that the first and / or second portions (310, 313) extend in the longitudinal direction (z).
    1/4
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    BE542659A|
    同族专利:
    公开号 | 公开日
    CN110462331A|2019-11-15|
    CN110462331B|2021-07-13|
    WO2018172644A1|2018-09-27|
    FR3064346B1|2019-03-29|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3380517A|1966-09-26|1968-04-30|Trane Co|Plate type heat exchangers|
    JPS5886396A|1981-11-17|1983-05-23|Kobe Steel Ltd|Gas-liquid dispersing device for plate fin type heat exchanger|
    FR2563620A1|1984-04-27|1985-10-31|Linde Ag|PLATE TYPE HEAT EXCHANGER|
    CN103983138A|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|WO2021122115A1|2019-12-19|2021-06-24|L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude|Mixing device promoting a homogeneous distribution of a diphasic mixture, heat exchange facility and associated mixing method|JPH0252790B2|1981-11-19|1990-11-14|Kogata Gasu Reibo Gijutsu Kenkyu Kumiai|
    CN1236271C|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|FR3099557B1|2019-08-01|2021-07-30|Air Liquide|Natural gas liquefaction process with improved circulation of a mixed refrigerant stream|
    FR3099560B1|2019-08-01|2021-07-02|Air Liquide|Natural gas liquefaction process with improved injection of a mixed refrigerant stream|
    FR3099563B1|2019-08-01|2021-07-30|Air Liquide|Heat exchanger with passage configuration and improved heat exchange structures|
    FR3099559B1|2019-08-01|2021-07-16|Air Liquide|Natural gas liquefaction process with improved exchanger configuration|
    FR3103543B1|2019-11-21|2021-10-22|Air Liquide|Heat exchanger with arrangement of mixing devices improving the distribution of a two-phase mixture|
    法律状态:
    2018-03-23| PLFP| Fee payment|Year of fee payment: 2 |
    2018-09-28| PLSC| Search report ready|Effective date: 20180928 |
    2020-03-19| PLFP| Fee payment|Year of fee payment: 4 |
    2021-03-23| PLFP| Fee payment|Year of fee payment: 5 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1752476|2017-03-24|
    FR1752476A|FR3064346B1|2017-03-24|2017-03-24|HEAT EXCHANGER WITH LIQUID / GAS MIXER DEVICE WITH REGULATORY CHANNEL PORTION|FR1752476A| FR3064346B1|2017-03-24|2017-03-24|HEAT EXCHANGER WITH LIQUID / GAS MIXER DEVICE WITH REGULATORY CHANNEL PORTION|
    PCT/FR2018/050454| WO2018172644A1|2017-03-24|2018-02-27|Heat exchanger with a liquid/gas mixer device having a regulating channel portion|
    CN201880020623.1A| CN110462331B|2017-03-24|2018-02-27|Heat exchanger|
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