WO2019224767A1

WO2019224767A1 - Thermal exchanging device

Info

Publication number: WO2019224767A1
Application number: PCT/IB2019/054276
Authority: WO
Inventors: Luca Cipriani
Original assignee: Ecosfera Srl
Current assignee: Ecosfera Srl
Priority date: 2018-05-24
Filing date: 2019-05-23
Publication date: 2019-11-28
Anticipated expiration: 2020-11-24
Also published as: IT201800005663A1

Abstract

A heat exchanger DEVICE (D) for the exchange of thermal energy between air and a gaseous or liquid fluid, characterized in that it comprises a plurality (K) of modules (M) of the exchanger, between which at least one closed channel (C) is placed along which it is suitable to flow a feeding flow (F) of said gaseous or liquid fluid; each said module (M) being defined by at least two dissipating plate elements (P1, P2) which are equal to each other and with a relief surface adapted to be mutually fixed in an opposed way to define at least one portion (Ti) between said channel (C) provided with a varied waved pattern.

Description

THERMAL EXCHANGING DEVICE

The present invention relates to a thermal exchanging device .

The present invention is advantageously employed in industrial and/or civil field in order to effectively obtain the cooling or heating of environments in general, to which the following description makes explicit reference without thereby losing in generality, through the exchange of thermal energy between two fluid currents and having different temperatures.

In particular, in the present invention one of the two fluid flows defined by air or water is apt to carry out the heat exchange with an another fluid flow defined by a gas or by a liquid flowing within a supply circuit.

In general, in order to realize the exchange of thermal energy between two fluid flows having different temperatures, one of which is air and the other is a gaseous or liquid fluid which flows within a supply circuit, the use is currently known of an exchanger device made of bundles of tubes, which is substantially defined by a cylindrical inlet manifold of a fluid, to which are welded a plurality of tubes with a diameter lower than the diameter of the manifold, so as to define, together with an output cylindrical manifold, which is welded to the above-mentioned tubes on the opposite side with respect to the inlet manifold, a circulation flow of the cited fluid.

Each of such tubes goes through to a pack of sheets or aluminum fins suitably and mutually spaced, and develops according to a serpentine shape with one or more passages through the aforementioned pack of fins so as to terminate in the output cylindrical manifold. The heat exchange between circulating air and fluid therefore occurs in two phases, in which the first phase exchanges heat between the tube and the peripheral collars of the aforementioned aluminum fins, and in the second phase heat is exchanged between the collar of the fins and the fins themselves.

In this way, the air thus extracts heat from the fins, which in turn extract it from the tubes and from the fluid circulating within the tubes.

The actual heat exchange surface is therefore essentially defined only by the serpentine tubes and therefore is strongly dependent on their size and length extension. From the foregoing, it can easily imagined that such known device with bundles of tubes is not optimal from the point of view of the energy exchange efficiency. Furthermore, the device with bundles of tubes has the considerable disadvantage of exhibiting a poor flexibility of use, a not easy maintenance and therefore very often it has a considerably encumbrance, especially when the surface area is to be significantly increased, together with the related heat transfer coefficients of the aforementioned tubes.

The document US4470455 describes a plate exchanger provided with a plurality of corrugations, which however have discontinuities between them and are not arranged on the whole surface of the plates. In addition, the air passage channel is too wide and in fact in order to increase the heat exchange efficiency it is inserted into an inner sinusoidal element which improves the heat transfer to the air passing through it. In such system the external corrugations of the plates exposed to the air passage of a module do not come into contact with the corrugations of the near module .

The aforementioned document shows a sort of small net (17) which is brazed to the outside of the walls of the molded plates, such small net having to be inserted in a space obtained by increasing the connection collar of the inlet and outlet holes on the molded plates. This system requires that the small net be built separately and then introduced into the suitable spaces. In order to extract heat from the internal circuit, the small net must have contacts with the most extensive possible plate, and for this reason the corrugations are not made with continuity but are spaced apart so as to provide flat portions and therefore be in contact with the small net. The corrugations made in this way have more the purpose of keeping constant the distance between the plates rather than increasing the exchange coefficient .

US2006207753 describes a plate exchanger which is NOT equipped with corrugations, as the protrusions visible in the drawings are nothing more than spacers capable of precisely maintaining the exchange plates at a certain distance and furthermore these protrusions are not arranged on the entire exchange area.

The purpose of the present invention is therefore to overcome the drawbacks of the devices according to the known prior art described above.

In particular, one purpose of the present invention is to provide a heat exchanging device having a high and optimal energy exchange efficiency. Another purpose of the present invention is to provide a heat exchanger device equipped with a modular constructive structure with high flexibility of use and easier and smoother implementation.

A further purpose is to provide a method for obtaining an optimal heat energy exchange with two fluid flows having different temperatures.

The structural and functional characteristics of the present invention and its advantages with reference to known art will become more clear and evident from the following claims, and in particular from an examination of a following detailed description, made with reference to the annexed drawings, which schematically shows a preferred but not limiting embodiment of the air heat exchanging device, in which:

- Figure 1 is a perspective view of an exchanging device according to the present invention;

- Figure 2 is a front view of the exchanging device of Figure 1;

- Figure 3 shows on an enlarged scale a side portion of the exchanging device of Figure 2;

- Figure 4 represents a schematic sectional view of a detail of the exchanging device of Figure 3;

- Figure 5 is a plan view of a single component of the exchanging device according to the present invention; - Figure 6 is an exploded perspective view of Figure 5 of the component G and represents the coupling of two elements PI and P2;

- Figure 7 represents a schematic sectional view of a portion of the component of Figure 5;

- Figure 8 is a perspective view on an enlarged scale of a portion of the exchanging device of Figures 1 to

3;

- Figure 9 is a perspective view partially in section and on an enlarged scale of a portion of the exchanging device of Figures 1 to 3;

- Figure 10 is a perspective view partially in section and on an enlarged scale of another portion of the exchanging device of Figures 1 to 3,

- Figures 11 and 12 show details of a variant of the exchanging device in question;

- Figures 13 and 14 show, partially in section, some details of another variant of the exchanging device in question;

- Figure 15 shows details of a further variant of the exchanging device of the present invention;

- Figures 16 and 17 show in section the corrugations Oi, while Figure 18 shows in plan view the distribution of corrugations Oi on the surface of the exchanging surface of the exchanging module which is object of the invention;

- Figures 19, 20, 21 show diagrams of different circuit configurations of a battery comprising several exchanging modules according to the present invention .

The module and system object of the invention provide a simpler embodiment than according to the known art, by making the heat transmission completely to the corrugated walls of the exchanger plates.

With particular reference to the accompanying Figures 1 to 4, a heat exchanging device is globally indicated with D, which is apt to realize the exchange of thermal energy between two fluid flows having different temperatures, one of which is air (or water) and the other is a gaseous or liquid fluid flowing inside the device D itself, along a closed supply channel C which connects an inlet manifold CE for the gaseous or liquid fluid to an outlet manifold CU being part of the device D itself.

The device D is of the type with dissipating plates and comprises at least two or preferably a plurality K of exchanger modules M, which are mutually stacked and secured, preferably but not limited through braze welding, among which a circulation flow F of the gaseous or liquid fluid is able to flow, and which are adapted to be crossed by an air flow A, preferably generated by an air suction source Sa known by itself, which spreads substantially transversely with respect to the circulating flow F of the gaseous or liquid fluid .

Each module M is defined by two dissipating plates Pi, P2, equal to each other and suitably welded together along their outer edge, preferably but not limited means of braze-welding, said plates Pi, P2 providing an exchange surface 2 with completely concerned and seamlessly corrugations Oi worked in relief on said exchange surface 2, said plates Pi, P2 being coupled to each other in an opposed way to define a single internal length Tf of the cited channel C, along which the gaseous or liquid flow F circulates, which single length Tf being provided of a undulated tortuous and substantially sinusoidal shape in cross section, as will be clarified in the following.

It should be further emphasized that the corrugations Oi between the two plates Pi and P2 are arranged at opposite angles, so as to be mutually in contact only in some points by maintaining the distance between them constant and thus allowing the gaseous or liquid fluid to cover an effective and wide heat exchange surface following a tortuous path.

As shown more clearly in attached Figures 5 to 7 and also 9 to 10, each plate PI, P2 is defined by an element 1 made of a metal sheet, the exchange surface 2 of which is preferably rectangular and is suitably provided with several series Si of corrugations Oi worked in relief on the heat exchange surface 2 itself and arranged, preferably but not limited to, with a conformation Z, between the various series Si, in a herringbone pattern, or in a similar/equivalent conformation .

The exchange surface 2 of each plate PI, P2 has also, at its opposite ends 2a and 2b, two holes 3a and 3b inside of which pass respectively the manifold EC and the manifold CU.

Each cited hole 3a, 3b lies on a respective area 4a, 4b housed in the relative ends 2a, 2b.

According to an alternative embodiment shown in Figures 11 and 12, the provision of a single corrugated plate PI, P2 is carried out by a preferably but not limited welding by braze welding to a plate with a flat surface Pp of a network structure R with a different conformation . In other words, the network structure R is welded by braze welding to the plates PI, P2 and keeps the lengths of channel C uniformly spaced from each other, so that the air A can pass through the exchanger D with a double effect: the network R absorbs part of the heat transmitted from the inside of channel C, and the various corrugations through which the flow will pass in a perpendicular direction so contributing to the is remixing, thus increasing the exchange coefficient.

As an alternative to the network R, it is also possible to use metal spacers (not shown) .

According to a further alternative embodiment of the device D illustrated in Figure 15, which must be used mainly but not exclusively in cases in which the air forcing systems are not largely prevailing, it will be possible to increase the heights of the air channels. The exchange surface 2 of the sheet 1 which forms each plate PI, P2 has groups of corrugations Oi with dampened amplitude and with peaks Y at increased height, so that once two plates PI and P2 have been coupled/welded together to form the module M such plates PI and P2 are substantially in contact with each other only in correspondence of the aforementioned peaks Y, thus obtaining a greater flow rate of air A and flow F and, therefore, a greater efficiency of the device D.

In this way, in conclusion, the overlap between the two plates Pi and P2 which forms the pair G of the single module M with the respective areas 4a, 4b mutually opposite and with the subsequent welding of the ends 2a, 2b of the plate Pi with the respective ends 2a, 2b of the plate P2, therefore leads to the formation of two single lengths Tf mutually superimposed with a varied wave pattern along which, in use, the flow F of gaseous or liquid fluid passes, so advantageously carrying out an effective heat exchange with the air A which diffuses forcefully and transversely with respect to the length Tf along a relative slit Fa for diffusion of the air A itself formed by the superposition of the two lengths Tf and arranged between the two lengths Tf themselves .

In particular, the slit Fa is provided with a varied/tortuous wave pattern extending both on the horizontal and on the vertical plane, being defined by the aforementioned series Si of corrugations Oi in relief on the exchange surface 2.

It should be emphasized that, in this way, the corrugations Oi between the two plates Pi and P2 will be arranged with opposite angles, so as to be in contact with each other only in some points, keeping the distance between them constant and thus allowing the gaseous or liquid fluid to cover an effective and wide heat exchange surface.

In particular, the tortuous shape of the single length Tf on both the horizontal and vertical planes, and therefore by extension of all the lengths Tf present in the package K of modules M of the channel C along which the flow F of gaseous or liquid fluid passes, will allow an optimal mixing of the fluid itself to the full benefit of the energy exchange coefficient with air A which diffuses transversely with respect to the flow F itself along the relative slit Fa.

It is also worth noting the considerable increase in the size of the area exposed to the action of energy exchange between gaseous or liquid fluid and the air obtained with the device D described above.

In fact, considering a traditional exchanging device with bundles of tubes, with an exchange tube with a diameter of, for example, 20 mm, the cross-section of such tube will have an area of 314 mmq, so its circumference will be 62.8 mm.

Starting now from the assumption that the area of the cross-section of the tube and the area of the cross- section of the channel G of the device in question are equal, to find the surface exposed to the fluid in the device D it will be sufficient to suppose a hypothetical channel height of 2,5 mm: then to find the length of the base of the rectangle, it will proceed by dividing the area of 314 mmq by 2,5 thus obtaining a value equal to 125, 6 mm. It follows that the surface exposed to the device D in object is (125,6 x 2) + (2,5 x 2) = 258,2 mm. In other words, with the same sectional area, the surface exposed to the fluid contained with a conventional device with a bundle of tubes is 62,8 mm, whereas the exposed surface using the device D in object described above is 258,2 mm.

Such a simple example, moreover, does not take account of the corrugations which averagely increase the surface area of 20-30%, then the effective surface area exposed with the innovative device D described here will be approximately 310 mm.

Therefore, ranging from 62,8 mm to 310 mm there is therefore a considerable increase in the energy exchange area of about 400%.

Another important effect can now be considered in relation to the increase of the surface directed to the thermal exchange of the internal fluid. The best way to understand also this concept consists, as before, to set some hypothetical conditions to compare. It is therefore assumed that:

- for the traditional heat exchanger, ten tubes depart from the manifold which cross the package of fins three times;

- for the traditional exchanger, the distance between the axis of the tubes is 50 mm both vertically and horizontally;

- for the traditional exchanger, the pitch of the fins is 2,5 mm;

- for the traditional exchanger, the width of the battery is 1000 mm;

- for the APHE exchanger, the overall dimensions are identical to those of the traditional one;

- for the APHE exchanger, the average channel height is 2,5 mm .

The dimensions of the traditional battery can thus be obtained as follows: regarding the height the pitch of 50 mm is multiplied by the number of tubes, so 50 x 10 = 500 mm in height; regarding the depth the pitch of 50 mm is multiplied by the number of passages of each tube, so 50 x 3 = 150 mm in depth.

These are also the dimensions of the fins and will serve as the basis for the hypothetical dimension of the channel surface of the device D in question. It is known that the width has been assumed to be 1000 mm so the tubes which pass through the finned package will be 1000 mm long.

It is also known that there are ten tubes passing through the finned package three times, so the total number of tubes that develops is 30. The total tube length will therefore be 30 m. Knowing that the circumference of the tube is 62,8 mm it will be sufficient to multiply it by the total length of the tube and the total exchange surface will be obtained through which the water flows in the traditional battery, 62, 8 mm x 30000 mm = 1.884.000 mmq, that is

1.884 mq .

To calculate the total exchange area of the APHE system in comparison, the total area of an exchange channel must be initially calculated, the perimeter of the section being still known: 310 mm. This value must therefore be multiplied by the height of the channel, to maintain the comparison conditions and therefore it will be 500 mm high, but, still due to the effect of the ripples also in height, it will be increased by about 20% and therefore the height of the surface developed with the ripples will be 600 mm. Therefore the total exchange surface of each channel will be 310 x 600 = 186.000 mmq. It has been assumed that the average height of a channel is 2,5 mm, but to form a channel, however, two plates with a depth of 2,5 mm each are needed, so the effective dimension of a channel will be 5 mm, and with a width of the exchanger of 1000 mm there will therefore be about 200 lengths of exchange channel through which water flows and a total surface of 186.000 x 200 = 37.200.000 mmq that is 37,2 mq of surface through which water flows.

Therefore, in conclusion, with the same dimensions the increase in area between the two exchangers goes from 1,884 mq for the traditional battery to 37,2 mq for the device D, with an increase of approximately 1.900%. Furthermore, the device D allows to achieve the following additional significant advantages with respect to the known art:

Distance of fluid threads .

In traditional battery systems, the tubes can have different diameters, with an average between 8 and 10 mm. The molecules running through the tube at its center will therefore have a distance of 4,5 mm from the exchange surface.

On the contrary, in the device D described above, the channel lengths can have thicknesses of a few millimeters, from 2 to 3 mm, which means that the fluid threads at the center of each length have an average distance of 1/1,5 mm from the exchange surface, which is much closer compared to traditional systems.

Lateral air inlet

The direction of the two flows of exchange of air and internal fluid, is therefore perpendicular, so if the internal fluid has a direction from bottom to top (vertically) , the air will have a direction from right to left or from left to right (horizontally) . The geometries of the aforementioned plates have always a base lower than their height, so the fluid flowing over a narrow channel will cross on the longest side the air with its original temperature for its entire path. This important factor allows the internal fluid of air to always cross the air with the maximal temperature difference .

Materials used.

The materials used for traditional devices are mainly copper and aluminum, which materials are not very effective against corrosion.

The material used is mainly due to the realization of the device D object of the present invention and is preferably stainless steel AISI304 or 316, a material very resistant to corrosive fluids (for example acid solutions for anodic oxidations) and therefore is more suitable in all applications requiring particular resistance to the marine atmosphere and against acid rain .

Robustness

In traditional tube bundle devices, at the outer ends there is a considerable number of aluminum fins which are extremely thin and a slight hit is enough to bend them; they are extremely delicate and if bent they prevent the correct air flow obstructing the path. In a similar position, the device D offers a structure composed of pairs of stainless steel plates with plates 0,3 - 0,4 mm thick which are welded together externally, thus creating thicknesses of 0,6 - 0,8 mm at the welding points: this results in an external surface which is certainly more resistant to hits and does not require special protection.

Monolithic system

A traditional device forms a set of elements fixed to each other by the mechanical union between the tubes and the fins, whereas the tubes at different temperatures tend however to expand and retract, creating over time a sort of separation between the components: this leads to an inevitable weakening of the structure itself, and in fact it is necessary to house battery in an external frame which keeps everything together. In the device D in object, the plates are each welded to the other in many points, so obtaining an extremely robust monolithic structure, in which each element is welded thereby obtaining a self- supporting structure which can be mechanically engaged through possible fixings produced on the peripheral plates, so probably no containment frame will be needed .

Production costs

The construction of traditional tube devices is not simple, as that the fluids or gases passing through the tubes are generally collected in manifolds that diffuse the total flow into several smaller diameter tubes, whereas the tubes pass through the sheets or packages of aluminum fins back and forth several times, and this involves the welding of 180° bends which force the fluids contained to reenter the packages several times.

To build a package of fins in particular it is necessary: - to cut the tubes at a given length, - to bend a part of the tubes at 180°, - to cut, pierce and press the aluminum sheets, - to align the sheets, - to insert the tubes in the battery of sheets, - and to spread the tubes to adhere to the holes of the sheets, to weld the bends at 180 to prepare the two manifolds to weld the tubes to the manifolds to prepare the frame containing the battery, - and to mount the battery inside the frame.

It was also found that by acting on some factors including the height of the fluid channel F (see Fig. 16), the cross-sectional shape of the corrugations Oi (see Fig. 17), the distribution of the corrugations Oi on the exchange surface 2 (see Fig. 18) and the control of the circuits of each module M inside the device (see Figs. 19, 20, 21), it is possible to increase the efficiency of the module of the invention.

Regarding the height X of the channel of fluid F, the optimization of heat exchange efficiency/load loss occurs in the range of values between 1 mm and 30 mm. Through the control of the heights the load losses of more or less dense fluids can e controlled, for example low corrugations for water or high for very dense oils, molasses and all fluids with high viscosity. In addition to controlling the load losses, the channel heights will also affect the exchange coefficients, for example where slight temperature differences are needed, plates with very low channels will be chosen, for example considering the evaporation phase of the Freon gas in the conditioning.

Regarding the cross-sectional shape of the corrugations Oi, this is optimized in a substantially triangular cross-sectional shape (as shown in Figs. 4, 10, 16, 17) . Considering Y (as shown in Fig. 17) as the angle between the inclined plane of the corrugation Oi and the horizontal plane (ideally parallel to the module M) , the optimization of heat exchange efficiency/load losses in the range of Y values between 30° and 60°, are obtained.

Regarding the distribution of the corrugations Oi on the exchange surface 2 it has been found that for the exchanger object of the invention an optimized efficiency is obtained when the distribution of the corrugations Oi is made like a herringbone and the complementary angle Z between the top edge of the corrugations Oi and the direction of the longitudinal axis of the plate PI, P2 is included in the range of Z values between 25° and 65°.

Finally, regarding the control of the circuitry of each module M inside the device (see Figs. 19, 20, 21), it is intended to better clarify this concept in the following .

Normally all the plates are drilled at the ends to allow the inlet CE and the outlet CU of the internal fluid in the exchange channels C, and in this case the battery distribution scheme is depicted in Figure 19. However, it is possible to keep blind an inlet CE on one of the two plates PI, P2 which together make up a first module M and a second module M to obtain the distribution scheme shown in Fig. 20. Furthermore, by keeping blind further inlets CE on one of the two plates Pi, P2 which are associated with further modules M, the distribution scheme shown in Fig. 21 can be obtained. In this way it is possible to get forced paths allowing to divide the course of the channels C in determined directions and therefore create groups of distinct channels going in opposite directions.

The increase of more "sections" of channels, forces the fluid to increase the speeds in the different sections, thus creating greater turbulence which contributes to increase the energy exchange coefficient of a battery comprising several modules according to the invention.

Below some examples of possible circuits are given, by assuming that the total fluid flow rate is 10.000 liters per hour.

In the first case, in the circuitry 1-1 the flow rate for each single channel of the 12 channels drawn will be (10.000/12) 833,3 1/h (Fig. 19) .

In the second case, in the circuit 1-2 the flow rate for each individual channel will be (10.000/6) 1.666, 6 1/h (Fig. 20) . In the third case, in the circuit 1-4 the flow rate for each individual channel will be (10.000/3) 3.333,3 1/h (Fig. 21) .

The construction of the device D in object requires very little manpower. For the realization of the plates in fact it is necessary to press them with a oleo- dynamic press starting from a metal strip of a certain width; once printed the plates must be stacked to form the packages. All of them are carried out automatically and the operator's contribution will be limited to control of the process and to the change of the bands and the molds when the batch is finished. Once having obtained the plate packages it is necessary to place the connections, place the packages to be welded on the oven trolley and introduce the loaded trolley into the oven .

In the case of braze welding, the oven will carry out the welding of all plate packages in total autonomy and with a simple procedure.

Claims

1. Exchanging device (D) for the exchange of thermal energy between two fluid streams, characterized in that it comprises at least one exchanger module (M) , inside which at least one closed channel (C) being formed along the edges of which it is suitable to flow a feeding flow (F) of a first fluid stream: said module (M) being defined by at least two dissipating plate elements (PI, P2), equal to each other and with relief surfaces, adapted to be mutually fixed in opposite way to define at least one portion (Tf) of said channel (C) provided with a varied waved pattern; said one portion (Tf) being adapted to be crossed by a second fluid stream (A) diffusing substantially transversely with respect to said portion (Tf) and according to a varied waved pattern.

2. Device according to claim 1, characterized in that said first fluid stream comprises a gaseous or liquid fluid .

3. Device according to claim 1 or 2, characterized in that said second fluid stream comprises air.

4. Device according to claim 1 or 2, characterized in that said second fluid stream comprises water.

5. Device according to one or more claims from 1 to 4, characterized in that each of said plate elements (PI, P2) is defined by a metal sheet element (1), at least one surface of which (2) being suitably provided with several series (Si) of corrugations (Oi) machined in relief and present on said surface (2) .

6. Device according to claim 5, characterized in that said series (Si) of said corrugations (Oi) machined in relief and present on said surface (2) have a substantially herringbone (Z) conformation or similar.

7. Device according to claim 6, characterized in that said corrugations (Oi) are provided with dampened amplitude (As) with peaks (Y) at an increased height.

8. Device according to one or more claims from 5 to 7, characterized in that said series (Si) of corrugations (Oi) are arranged at mutually opposed angles.

9. Device according to one or more claims from 1 to 8, characterized in that each of said plate elements (PI, P2) is defined by a metal sheet element (1; Pp) , on at least one surface of which a wire mesh-type structure (R) or equivalent is fixed.

10. Device according to one or more claims from 5 to 9, characterized in that said surface (2) of said sheet element (1) has, on its opposite ends (2a, 2b), two respective holes (3a, 3b) inside which an inlet conduit (CE) and an outlet conduit (CU) of said flow (F) respectively pass; each of said holes (3a, 3b) lying on a respective recessed area (4a, 4b) disposed in said relative end (2a, 2b) of said surface (2) .

11. Device according to one or more claims from 1 to

10, characterized in that said fixing of said two plate elements (PI, P2) comprises a preferred but not limited welding .

12. Device according to one or more claims from 1 to

11, characterized in that it comprised a staked plurality (K) of said exchanger modules (M) .

13. Device according claim 12, characterized in that said modules (M) of said plurality (K) of modules are mutually fixed by means of a preferred but not limited welding .

14. Exchanging device (D) for the exchange of thermal energy between air (A) and a second gaseous or liquid fluid, characterized in that it comprises at least two superimposed exchanger modules M) , inside module (M) at least one channel (C) being formed along which it is suitable to flow a feeding flow (F) of a second fluid; said module (M) being defined by at least two dissipating plate elements (PI, P2), equal to each other and comprising an exchange surface (2) completely covered on its entire surface of a plurality of corrugations (Oi) machined in relief, said plates (PI, P2) being mutually coupled in opposite way to define one single inner portion (Tf) of said channel (C) provided with a varied waved pattern, along which said flow (F) is able to circulate, said at least two superimposed modules (M) further defining a plurality of slits (Fa) for the diffusion of air (A) transversely arranged with regard to the flow (F) when in use, also being provided with a varied waved pattern, said at least two modules (M) being arranged so that the corrugations (Oi) of the upper module (M) are arranged in contact at their top with the corresponding corrugations (Oi) of the lower module (M) , in order to further increase the heat exchange efficiency of the device .

15. Method for the realization of an exchange of thermal energy between two fluid streams, characterized in that it comprises at least the steps of generating a feeding flow (F) of a first fluid stream inside a channel (C) closed with at least one portion (Tf) having a varied waved pattern; and of generating a second fluid stream (A) to be diffused on said portion (Tf) substantially transversely with respect to said portion (Tf) and according to a varied waved pattern.

16. Method according to claim 15, characterized in that such first fluid stream comprises a gaseous or liquid fluid .

17. Method according to claim 15 or 16, characterized in that said second fluid stream comprises air (A) .

18. Method according to claim 15 or 16, characterized in that said second fluid stream comprises water.