JP2007518053A - Heat exchanger and its heat exchange module - Google Patents

Abstract

The heat exchange bundle has a flow path (6 _a , 6 _b , 6 _c , 6 _d ) for the first heat exchange fluid and a second passage (28) for the second heat exchange fluid that can be condensed, for example. The module (102) which defines is included. The flow paths have different hydraulic diameters, and the hydraulic diameter of the second passageway (28) varies in an embodiment to decrease as condensation occurs. Applications are heat exchangers, condensers and evaporators.
[Selection] Figure 4

Description

  The present invention relates to a heat exchanger and a heat exchange module constituting a part of such a heat exchanger.

  From WO 98/16786, the modules defining the first passage for the first fluid are each composed of two metal plates, and a plurality of streams arranged in fluid parallel to each other between these two metal plates. Heat exchangers are known in which a path sheet is formed. Each flow path inserted between two adjacent flow paths of this sheet is adjacent to these two adjacent flow paths over the entire length of the sheet, and joins two metal plates 2. It is separated from two adjacent channels by a weld line of books. A second passage for the second fluid is formed between the modules in the internal space of the casing surrounding the module.

  According to this document, a module is manufactured using two flat metal plates, which are joined together by a welding line consisting of the aforementioned lines separating adjacent flow paths from each other, and then two metal sheets. A fluid under pressure is introduced between the plates to expand the two metal plates between the weld lines, thereby forming a flow path. The flow paths of the same module are fluidly parallel between two distribution areas common to all flow paths of the same module, which distribution areas themselves are connected to the connection box.

  During the hydroforming process (i.e., the expansion process described above), the second fluid is easier to operate during operation into a pseudo-channel formed between adjacent modules in the recesses between successive expansion regions. Limit expansion in the dispensing area. With the exception of those regions where expansion is limited, the flow path profile is continuous and even. Thus, the channel cross-section for the fluid is only modified locally at the outlet and inlet. The transition between the modified channel cross-sectional area and the constant channel cross-sectional area along the flow path is abrupt and localized.

  WO 01/07854 describes an improvement to a U-shape instead of straightening the flow path. The variation shown in FIG. 25 of this document includes the first and second fluid inlets in the first and second passages with abrupt transitions between the “normal” region and the modified region, and A local modification of the cross section of the flow path acting as an outlet is shown.

  DE-A1-19639115 describes a heat transfer element in the form of a plate consisting of two metal plates defining a flow path for exchange fluid therebetween. In the embodiment of FIGS. 4 and 5, each flow path has a substantially U-shape, which is divided into two in turn, and the ratio of the cross-section of the path from one end to the other end of the branched flow path is 1 to 4 It changes gradually. Therefore, each passage folded and branched on itself occupies a rectangular space, and the plurality of rectangular spaces are connected to each other by their adjacent long sides. The purpose of this arrangement is to reduce the velocity of the internal fluid when the internal fluid has almost completed its exchange process in order to better exchange heat in an area where the two exchange fluids have a small temperature difference from each other. That is. The use pointed out is as a cooling element for high temperature batteries of electric vehicles.

  Such exchangers are particularly complex to manufacture and have very limited flow rates.

  The object of the present invention is to control the evolution of the flow rate of at least one heat exchange fluid (especially if it undergoes at least partial phase change (eg condensation) as the heat exchange fluid flows) without significant additional costs. Is to provide a possible heat exchanger.

  Another object of the present invention is to realize a heat exchanger with a small loss of packing distributed in a controlled manner.

  Another object of the present invention is to provide a heat exchange module capable of constituting such an exchanger.

  In the heat exchanger according to the present invention, the modules defining the first passage for the first fluid are each composed of two metal plates, and the two metal plates are in fluid communication with each other between them. In general, a plurality of flow path sheets (nap) arranged in parallel are formed, and each flow path inserted between two adjacent flow paths of the sheet extends over the entire developed length thereof. Adjacent to two adjacent flow paths, separated from the two adjacent flow paths by two weld lines joining two metal plates, and a second for a second fluid The heat exchanger is characterized by the fact that the cross section of the passage varies generally along at least one passage while maintaining the continuity of the flow path profile. It is that.

  According to the present invention, a structure of the type described in WO 98/16786 or WO 01/07854 (ie having adjacent separated channels over the entire developed length) is a passage along at least one passage It has been found to be particularly suitable for realizing an overall change in cross section.

  An “overall” change is a change other than the local change at the end of the passage described above in connection with the prior art, and the second heat exchange fluid circulates transversely to the flow path. In some cases, every time the second heat exchange fluid passes through the expansion of each of the two adjacent modules, the second heat exchange fluid undergoes a change other than a local change due to, for example, a reduction in passage cross section. means.

  “While maintaining the continuity of the flow path profile” means that the change in the cross section of the passage is a change in the cross section due to rapid expansion or narrowing, or a change in which a single flow path branches into two flow paths. Represents not due to profile discontinuity.

  The overall change in cross section can be achieved according to the invention by means of channels of different hydraulic diameters, by channels of gradually changing hydraulic diameter from one end to the other and / or between modules for the second fluid. By relative positioning of the modules so as to change the hydraulic diameter of the passage between them, and so on.

  The hydraulic diameter of the passage for fluid refers to the diameter of a theoretical cylindrical tube that exhibits the same flow resistance as a passage thought to have a non-circular cylindrical profile.

According to the second aspect of the present invention, the heat exchange module is composed of two metal plates, and the two metal plates are formed of a plurality of flow path sheets disposed in fluid parallel to each other therebetween. Each of the flow paths inserted between the two adjacent flow paths of the sheet is adjacent to the two adjacent flow paths over the entire length of the sheet. The heat exchange module is separated from the two adjacent flow paths by two weld lines that join the metal plates. The feature of the heat exchange module is that the cross section of the flow path is defined by the flow path profile. It consists of changing overall while maintaining continuity.
Other features and advantages of the present invention will become apparent from the following description of non-limiting examples.

In general, to make the drawings easier to understand, all the drawings in this application are very schematic, the number of channels in the module is significantly less than in most real cases, and the thickness of the metal plate is exaggerated. It is expressed.
1 to 3 schematically show different types of heat exchangers for illustrative purposes in order to better understand the present invention.

  In the embodiment shown in FIG. 1, the heat exchanger comprises a casing 1 having a rectangular profile with respect to a vertical axis, which contains a stack of substantially plate-shaped heat exchange modules 2 extending in a vertical plane. Yes. Each module 2 is basically formed of two metal plates 3 which are welded together along a vertical weld line 4 and have a vertical flow path 6 between them. Inflated between these weld lines 4 to define.

  Each flow path extends with one continuous profile over the entire height of the module 2. All the flow paths 6 are connected to the upper connection chamber 7 defined in the upper connection box 8 or the lower connection chamber 9 defined in the lower connection box 11 at each end (upper and lower ends). It is open. Accordingly, the plurality of flow paths 6 form a first heat exchange passage for the first fluid as a whole, and this first heat exchange passage is connected to the outside for the first fluid by the connection boxes 8 and 11 during operation. Can be connected to the circuit. The fluid-tight connection between the passage 6 and the chambers 7 and 9 is made by appropriately shaped connection strips 12 which are inserted between the two ends of the module 2 and in total of the connection box 8 or 11. Form the bottom. Accordingly, the flow path 6 is fluidly parallel to each other between the two junction boxes 7 and 9. Each of the channels 6 other than the two channels at both ends of the sheet of the channels of each module is separated from the two adjacent channels by each welding line 4 continuous over the entire developed length of the channel, Adjacent to two adjacent flow paths over the entire developed length. In the illustrated embodiment where the flow path is straight, the deployed length is the same as the outer circumference. In other embodiments in which the channel is curved and has a U shape, for example WO 01/07854, the deployed length is of course very different from the outer length.

  A second passage for the second heat exchange fluid is defined between modules 2 and 2. Access to the second passage is performed by second connection boxes 13 and 14 arranged on the side wall of the casing 1, and these second connection boxes are connected to the connection chambers 7 or 9 at both ends 19 of the connection strip 12. The inner chambers 16 and 17 are arranged in such a way as to communicate with the gap 18 between the edges of the module 2 on the side facing the side. In the embodiment of the junction box 13, the outer periphery thereof is liquid-tightly welded to the outer periphery 22 of a rectangular opening formed in the casing 1. One side 21 of the outer periphery 22 is formed by the aligned end portions 19.

  Therefore, the second heat exchange fluid flows between the junction boxes 13 and 14 while passing through the second heat exchange passage formed of the internal space of the casing 1 located between the modules 2 and 2.

  In the illustrated embodiment, the side junction box 13 is located in a high portion immediately adjacent to the upper junction box 8 for the first passage, while the side junction box 14 is the lower junction box 11 of the first passage. It is arranged in the lower part of the casing 1 in the immediate vicinity. The second fluid enters laterally between the modules, flows between the modules parallel to the flow path 6 and then laterally exits from the other junction box. Each of these two fluids can flow in the up or down direction depending on the application. A parallel flow exchanger in which the two fluids flow in opposite directions (thus, in this embodiment, one fluid flows up and the other flows down) is referred to as a “counterflow” exchanger. An exchanger in which two kinds of fluids flow not only in parallel but also in the same direction is referred to as a “cocurrent exchanger”.

In the embodiment shown in FIG. 2, only the difference from that in FIG. 1 will be described.
In this embodiment, the side junction boxes for the second passages 13 and 14 completely cover the two opposite sides of the casing 1, so that these sides have a second fluid in the plane of the module 2. It is completely open so that it can flow in the horizontal direction. Such an exchanger in which the two fluids flow in different directions is called a “cross flow type”.

  Only the differences from the embodiment of FIG. 2 will be described for the embodiment of FIG. In this cross-flow type exchanger, the flow path 6 is oriented horizontally and the module 2 is also in the vertical plane. Accordingly, the passage of the first fluid is oriented horizontally. On the other hand, the connection boxes 13 and 14 for the second fluid are arranged above and below the casing 1 so that the flow direction of the second fluid is vertical between the modules 2. In particular, the embodiment shown in FIG. 3 is a condenser. The lower connection box 13 is provided with an inlet 23 for the gas, and the upper connection box 4 is provided with an outlet 24 for the residual gas portion of the incoming flow 23. When this flow 23 passes between the modules 2 in which a cooling fluid such as cold water flows through the flow path 6, the condensable part of the second fluid forms water droplets, which are It falls to the bottom 26 of the box 13 and is discharged from the lower liquid outlet 27.

  In such a condenser, the initial fluid volume decreases as a portion of this gas condenses, so that the second fluid has a volumetric flow rate that decreases from the inlet 23 toward the outlet 24.

  Accordingly, if the passage cross section of the second passage is substantially the same along the second passage between the inlet junction box 13 and the outlet junction box 14, the flow rate will be reduced. If this rate is appropriate at the entrance of the second passage, this rate will be too small for good heat exchange near the exit. In contrast, if this velocity is appropriate near the outlet, this velocity is too high at the inlet and the gas will tend to take water droplets towards the outlet, contrary to the desired separation action. Let's go.

  This condenser embodiment was chosen to better illustrate the benefits of different passage cross sections within different regions of the same passage, but other embodiments (especially evaporators) can be envisaged. Furthermore, it can be assumed that the speed is adapted in a direction that optimizes the effect obtained, in particular in heat exchangers.

In the embodiment shown in FIG. 4, each module 102 has flow paths 6 _a , 6 _b , 6 _c and 6 _d having different hydraulic diameters.
In the embodiment of FIG. 4, the pitch of the welding line 4 (i.e., the distance between the weld line 4 successive one) is equal to a constant value, called P _0. The difference in hydraulic diameter between adjacent flow paths is obtained by the difference in expansion of the metal plate 3 in each region defining one flow path, and the flow paths 6 _{a to} 6 _d are respectively connected to one of the modules 102. It has an expansion amplitude G _a -G _d that increases from one edge to the other. The profile (and hence the hydraulic diameter) of each channel 6 _a , 6 _b , 6 _c , or 6 _d is constant over the entire length of the channel.

When two modules 102 as described above are juxtaposed in two parallel planes P with modules having the same hydraulic diameter facing each other, the direction is perpendicular to the direction of the flow paths 6 _{a to} 6 _d. The hydraulic diameter available in the second passage 28 between these modules 102 generally varies from one end of the second passage to the other. If, for example, the second passage is rising, in the illustrated configuration where the flow path has a hydraulic diameter that increases from bottom to top, the hydraulic diameter of the second passage decreases from its starting point to its end. . This corresponds to the desired situation in the condenser of FIG. 3 according to the description given above.

Although only the differences from the embodiment of FIG. 4 will be described, in the embodiment shown in FIG. 5, each module 202 is composed of a plurality of groups of flow paths having the same hydraulic diameter, but these hydraulic diameters are different for each group. Is different. In the schematic diagram of FIG. 5, there are two groups of two flow paths each. That is, a group below the channels 6 _a and 6 _b having the same relatively small hydraulic diameter and a group above the channels 6 _c and 6 _d having the same relatively large hydraulic diameter. Again, the difference between the hydraulic diameter results from the difference in expansion having the same pitch P _0. Accordingly, the second passage 28, the smaller second hydraulic between the first and the hydraulic diameter, the flow passage 6 adjacent _c and 6 _d between the flow channel 6 _a and 6 _b of the adjacent module 202 Diameter.

Only the differences from the embodiment of FIG. 5 will be described, but in the embodiment of FIG. 6, between the two groups of flow paths 6 _a , 6 _b and 6 _c , 6 _d , the flow paths 6 _a and 6 there is an intermediate passage 6 _e having expansion G _e intermediate value between the higher strength expansion smaller expansion and the flow path 6 _c and 6 _d of _b. As a result, the hydraulic diameter of the flow path _{6 e} is intermediate between the larger hydraulic diameter of the channel ₆ a, _{6 b} of the hydraulic diameter and the flow path ₆ c, _{6 d.} Further, the second passage 28 is between the flow paths 6 _c and 6 _d between the larger values defined between the flow paths 6 _a and 6 _b between the flow paths 6 _e of the adjacent modules 302. Has an intermediate value with the smaller value defined.

In all of the examples described so far, the pitch P ₀ between the weld lines 4 was the same for all weld lines of one module as well as for all modules. In the embodiment shown in FIG. 7, the expansion G ₀ is the same for all channels of all modules 402. On the other hand, the flow path of one sheet has a first group of flow paths 6 _g and a second group of flow paths 6 _h . Pitch P _g between the two weld lines which define the flow path 6 _g each other is greater than the pitch P _h between two weld lines which define the flow path 6 _h another. In this embodiment, the hydraulic diameter of the passage 28 decreases as the weld line pitch decreases.

The embodiment shown in FIG. 8 is a combination of pitch and expansion variations. Regularly increasing pitch _P j to P _n and four flow paths ₆ j having an expansion _G j ~G _n to increase again regularly from the bottom to the top of each module _{502, 6 k,} 6 _m, There are 6 _n .

FIG. 9 shows the hydroforming stage for making a module with four groups of channels 6 _p , 6 _q , 6 _r , 6 _s with different hydraulic diameters resulting at least partly from different expansions. Before injecting the hydroforming liquid, the module's flat blank (this stage consists of two flat metal plates welded together, eg by laser) along the weld line as shown in Fig. 4 above. Are arranged between two dies 31, 32 that define a cavity with working surfaces 33 _p , 33 _q , 33 _r , 33 _s and 34 _p , 34 _q , 34 _r , 34 _s from each other (these Module blanks extend between the two working surfaces, two working surfaces each having a distance corresponding to the desired expansion in the respective area). FIG. 9 shows the results obtained after differentiating and expanding the various channels according to the spacing of the working surfaces (there are channels between these working surfaces).

FIG. 10 shows that each die (only the lower die 31 is shown) has a flat working surface 33 corresponding to the expected maximum expansion and a shim 36 _p that fits to define an area where less expansion is desired. , 36 _q , 36 _s .

  For the upper die 32 (not shown in FIG. 10), these shims must be fixed below the working surface of the die before the hydroforming stage to avoid them falling due to gravity. Fixing these shims is also desirable for the lower die.

FIGS. 9 and 10 further illustrate that the present invention changes the hydraulic diameter in a first direction (eg, increasing direction) between, for example, groups 6 _p and 6 _q or 6 _q and 6 _r , then the heat exchanger It is shown that it is possible to change in the second direction (here the direction decreasing between groups 6 _r and 6 _s ) if desired for optimization.
In all the embodiments described with reference to FIGS. 4 to 8, the module weld lines 4 are parallel to each other and the hydraulic diameter of the flow path is constant over its entire length.

  In the embodiment shown in FIG. 11, all the weld lines 604 of the module 602 are converged and in this embodiment are converged toward the same point located beyond one end of the module. In other words, adjacent weld lines form a relatively small angle indicated by A in FIG. Accordingly, the pitch between the weld lines to be inherited increases from one end of each flow path to the other end, similar to the hydraulic diameter of the flow paths. Such a module has an isosceles trapezoidal overall shape and has diagonal longitudinal edges 37 that are substantially parallel to the two weld lines 604 at the ends of the flow path sheet.

  Such a module is useful for making a condenser of the shape of FIG. 1 or FIG. 2 (ie, having a vertical flow path). When the large end of the flow path is facing upward, the fluid to be condensed can take a course that descends in the flow path, and within this flow path, the fluid becomes increasingly smaller as its volume decreases by condensation. Encounter smaller hydraulic diameters. The second fluid (eg, water) passes between the modules or forms a bath between the modules. It is also possible to form an upflow evaporator with the same modular arrangement, where the first fluid encounters a hydraulic diameter that increases as its volume increases by evaporation.

  Such a module can also be, for example, a reflux condenser (ie, as described above with reference to FIG. 3, the flow to be evaporated rises and the water droplets formed are refluxed downward into the recovery device). Can be arranged with the large end of the channel facing down.

  The expansion of the channels can be constant along each channel, or conversely can be increased from the narrowest end of each channel to the widest end.

  FIG. 12 shows the side of a bundle of modules 602 with channels such that expansion increases from bottom to top and the modules are in parallel vertical planes. In the embodiment shown in FIG. 13, the same module 602 as in FIG. 12 is arranged on a plane that converges at a point located beyond the narrow end of the flow path, compared to the embodiment of FIG. The hydraulic diameter of the second passage on the side where the end of the flow path is narrowed is reduced.

  FIG. 14 very schematically shows the bundle when the expansion is constant along each flow path of the module of FIG. The bundle takes the form of a hexahedron that is an isosceles trapezoid in a plane parallel to the two faces facing each other. The casing for such a bundle typically takes a corresponding shape and has two parallel parallel faces in the form of an isosceles trapezoid and two rectangular faces connecting the diagonal sides of the trapezoid.

  In addition, if the expansion of the flow path is variable as shown in FIGS. 12 and 13, the bundle takes the form of a truncated pyramid. That is, the two surfaces of the trapezoid are inclined with respect to each other, and the other two surfaces on the side are also trapezoidal. The casing typically takes the corresponding form.

  In the embodiment shown in FIG. 15, module 702 has exactly the same flow path with the same width and the same expansion over the entire length of the flow path. These modules are fan-shaped to each other to converge beyond one end of the flow path, and are therefore arranged in an oblique plane to each other, so that the second passage (assuming cocurrent or counterflow type) The hydraulic diameter varies from one end to the other.

  Also, although not shown, in order to achieve the variable hydraulic diameter of the second passage when the exchanger is a cross-flow type, the modules are fanned together by rotating relative to each other about an axis parallel to the weld line. , And can be arranged in the longitudinal direction of the flow path.

  In the embodiment of FIGS. 1 to 3, the modules 2 are offset from each other in their own plane so that the top of the corrugation of one module is located opposite the corrugation depression of the two adjacent modules. . This arrangement, whether for a cross-flow exchanger (FIGS. 2 and 3), in the case of a parallel flow exchanger (FIG. 1), the second fluid enters from one side opening and the second fluid Is advantageous for circulation in the second passage in a direction transverse to the flow path, in order to exit from the other side openings. On the other hand, in order to simplify the illustration, all the embodiments described with reference to FIGS. 4 to 8, 14, and 15 show that the corrugated top and top of the two adjacent modules face each other, and the depression and the depression face each other. Show other possible arrangements. This is merely exemplary, and the present invention is also applicable to an offset arrangement as in FIGS.

The present invention is particularly applicable with the following specifications:
-Development length of flow path: 0.5 to 10 m
-Width of flow path sheet: 0.12 to 2 m
-The pitch before and after the module: 8 to 105 mm
-Pitch before and after the weld line: 10 to 100 mm
-Expansion of the flow path: 5-80 mm measured inside the flow path

  The metal plate is typically stainless steel with a thickness of a few tenths of a millimeter (no upper limit of 10/10), and a thin metal plate is advantageous for heat exchange, but the pressure difference between the two fluids And thermal distortion must also be considered.

  Of course, the present invention is not limited to the embodiment described and illustrated above. The aforementioned hydraulic diameter changing means can be combined in a very large number of ways.

  It is preferable to form a flow path having a constant hydraulic diameter over a portion of the length and a gradually changing hydraulic diameter over the remainder of the length.

  The exchanger described with reference to FIGS. 1 to 3 is not trivial or limiting. For example, if the replacement modules are placed without being offset from each other (thus the corrugations are top-to-top), the second fluid is laterally transferred in a manner similar to that described in FIG. 25 of WO 01/07854. The expansion of the flow path can be locally reduced in the region provided for introduction in the direction. If the second fluid is a bath, a casing is not necessary.

The present invention is also compatible with non-straight channels such as the U-shaped channel of WO 01/07854.
For the embodiment of FIGS. 11 to 14:
-Expansion gradually along each channel;
The pitch between the weld lines is conversely constant;
It is possible to make such a module.

FIG. 1 is a perspective view of a vertical flow type, parallel flow type, and plate type heat exchanger. FIG. 2 is a perspective view of a cross-flow plate heat exchanger, where the flow in the module (or plate) is vertical. FIG. 3 is a perspective view of a gas flow rising plate type condenser having plates arranged in a vertical plane. FIG. 4 is a schematic perspective view of two modules according to the first embodiment of the present invention. 5-8 are similar to parts of FIG. 4, but show four other embodiments of the present invention. FIG. 9 is a schematic cross-sectional view showing a heat exchange module according to still another embodiment manufactured by hydroforming in a die. FIG. 10 is a diagram of a variation for forming a die half. FIG. 11 is a perspective view of a heat exchange module according to still another embodiment of the present invention. 12 and 13 are elevation views of two embodiments of a bundle of modules according to FIG. FIG. 14 is a perspective view of a heat exchange module according to still another embodiment of the present invention. FIG. 15 is a diagram of another embodiment of a module bundle for the heat exchanger of the present invention.

Claims (16)

The modules (2, 102, 202, 302, 402, 502, 602, 702) defining the first passage (6) for the first fluid are each from two metal plates (3) These two metal plates form a sheet of a plurality of flow paths (6) disposed between them in fluid parallel and are interposed between two adjacent flow paths of the sheet. Each inserted flow path is adjacent to the two adjacent flow paths over the entire length of the developed flow path, and is separated from the two adjacent flow paths by two welding lines that join two metal plates. Separated, and
A heat exchanger in which a second passage (28) for a second fluid is defined between the modules, comprising:
A heat exchanger characterized in that the cross-section of the passage changes entirely along at least one passage while maintaining the continuity of the profile of the flow path. The heat exchanger according to claim 1, characterized in that the pitch between adjacent weld lines (604) varies gradually over at least part of the length of the flow path of the module (602). 3. A heat exchanger according to claim 1 or 2, characterized in that the expansion of the metal plate of the module (602) is gradual over at least part of the length of the flow path. The pitch (P _g , P _h , P _j , P _k , P _m , P _n ) between adjacent weld lines (4) varies for each flow path of the module (402, 502). A heat exchanger based on one of 1 to 3. The expansion (G _a , G _b , G _c , G _d ; G _e ; G _j , G _k , G _m , G _n ) of the metal plate of the module (102, 202, 302, 502) is a flow path (6 _a , _{6 b, 6 c, 6 d} ; 6 e; 6 j, 6 k, 6 m, 6 n) heat exchanger based on either of claim 1, wherein the 4 to vary. 6. A heat exchanger according to any one of claims 1 to 5, characterized in that the mutual arrangement of the modules causes an overall change in the cross section of the passage along the second passage (28). 7. A heat exchanger according to any one of claims 1 to 6, characterized in that the overall change in the cross section of any one passage is in the same direction as the change in gas flow in this passage used for the phase change process. 8. A heat exchanger according to claim 1, wherein the modules are in parallel planes (P). The heat exchanger module is based on either of claims 1, characterized in that in the plane of convergence (P ₁₎ 7 of the. 10. A heat exchanger according to any one of the preceding claims, characterized in that the modules have longitudinal edges (37) angled with respect to each other, each edge being substantially parallel to a respective end weld line (604). . Heat exchange modules (2, 102, 202, 302, 402, 502, 602) each consisting of two metal plates (3), the two metal plates being fluidly parallel to each other between them A plurality of flow path sheets arranged in the sheet are formed, and each of the flow paths interposed between two adjacent flow paths in the sheet are adjacent to each other over the entire developed length. The two adjacent flow paths are separated from the two adjacent flow paths by two welding lines joining two metal plates, and the feature is that of the path defined by the flow paths. The cross section is a heat exchange module consisting of changing overall while maintaining the continuity of the flow path profile. 12. A heat exchange module according to claim 11, wherein the pitch between adjacent weld lines (604) varies gradually over at least part of the length of the flow path. 13. The heat exchange module according to claim 11, wherein the expansion of the metal plate is gradually changed over at least a part of the length of the flow path. The pitch (P _g , P _h , P _j , P _k , P _m , P _n ) between adjacent weld lines (4) varies for each flow path, and is based on any one of claims 11 to 13 Heat exchange module. 15. The expansion (G _a , G _b , G _c , G _d ; G _e ; G _j , G _k , G _m , G _n ) of the metal plate varies for each flow path. Heat exchange module based on either. 16. A heat exchange module according to any of claims 11 to 15, characterized in that the modules have longitudinal edges (37) that are angled with respect to each other, each edge being substantially parallel to a respective end weld line.

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