EP2379978A2

EP2379978A2 - Apparatus for the distribution of fluids and the heat and/or mass exchange thereof

Info

Publication number: EP2379978A2
Application number: EP09795934A
Authority: EP
Inventors: Michael Hermann; Constanze Bongs; Hans-Martin Henning
Original assignee: Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
Current assignee: Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
Priority date: 2008-12-19
Filing date: 2009-12-21
Publication date: 2011-10-26
Anticipated expiration: 2029-12-21
Also published as: WO2010069602A3; WO2010069602A2; PL2379978T3; EP2379978B1

Abstract

The present invention relates to a fluid distributor, a heat and/or mass exchanger and an apparatus which has at least one fluid distributor and a heat and/or mass exchanger arranged thereon.

Description

Apparatus for the distribution of fluids and their heat and / or mass exchange

The present invention relates to a Fluidvertei- ller, a heat and / or material exchanger and an apparatus having at least one fluid distributor and arranged thereon a heat and / or material exchanger. Apparatuses for exchanging heat and / or substances between different fluids are state of the art. These include, for example, plate heat exchangers in which numerous flat fluid channels are arranged parallel to one another and thus offer a large exchange surface. This design is widely used, especially in air-air heat exchangers, which are used for example for the recovery of warmed. In the case of two fluids A and B, the channels are arranged alternately, that is to say in the sequence ABABAB. A special challenge exists At the same time, this should be streamlined, so that the pressure loss remains as low as possible. In the prior art, it is often necessary to transition from tubes of circular cross section to numerous parallel channels of rectangular cross section , whereby only every second channel may be flowed through

By itself, the distribution of the fluid streams in plate heat transferers is already solved by the geometry (only every second channel is accessible to the flow). In this respect, the distribution of the fluids is not to be solved by complicated transition pieces

However, this principle results in a sudden cross-flux change (halving), since every second channel is closed and the fluid must flow around these areas. This leads to high pressure losses. The transition pieces run from a round to an angular cross section and the fluids are separated in different cross sections incident flow. The prior art often requires a transition from circular cross-section tubes to a rectangular cross-flow section

In addition, in such heat exchangers, as described, for example, in WO 03/095917, numerous valves for controlling or for operation of the heat exchanger are necessary

Proceeding from this, it was an object of the present invention to provide a novel heat exchanger with associated fluid distributor, which has a significantly lightened simplified construction and can be operated without valves This object is achieved with respect to the fluid distributor with the features of claim 1, with respect to the heat and / or mass exchanger with the features of claim 11 and posted a device for heat and / or mass transfer with the features of claim 15, wherein each dependent Claims represent advantageous developments

Erfmdungsgemaß thus a rotationally symmetrical fluid distributor is provided, which in the longitudinal direction

A first aperture having in cross-section two concentrically arranged tubes, the inner tube enclosing a first space A, the outer and the inner tube enclosing a space B and the outer tube defining the diameter of the fluid distributor, and a second Aperture having in cross-section 2n circular sectors, where n is an integer ≥ 1, preferably ≥ 2, and the sectors are alternately connected to space A or B space, wherein between the first and the second aperture, the inner tube in the longitudinal direction um arranged around the pipe circumference n incisions and alternately arranged has n protuberances,

Wherein each incision has a longitudinally extending from the first to the second aperture Trajek- tone which reduces the radius of the inner tube, starting from the original radius of the inner tube at the height of the first aperture longitudinally in the direction of the second aperture, wherein all trajectories of the Incisions at the height of the second aperture converge in the center of the cross-section of the fluid distributor, and each invagination has a longitudinally extending from the first to the second aperture trajectory, which increases the radius of the inner tube, starting from the original diameter of the inner tube at the height of the first aperture longitudinally in the direction of the second aperture, all trajektorien the protuberances at height the second aperture converge with the outer tube. According to the invention, a rotationally symmetrical fluid distributor is understood to mean a device which always has a round (ie circular) cross-section, but the diameter in the longitudinal direction of the fluid distributor does not have to be constant, but can be constant. For example, the entire fluid distributor seen from the outside may have a cylindrical shape, but also have an increasing diameter, for example from the first to the second aperture. The fluid distributor has at its two ends on the first aperture and the second aperture. At the first aperture, the fluid manifold consists essentially of two nested tubes, the inner tube enclosing a space A and the outer and inner tubes enclosing a space B, while the second aperture is segmented, with the respective segments alternating with the first Rooms A and B, so the spaces that are enclosed at the first aperture of the inner tube or of the two tubes, in conjunction. In the fluid distributor takes place between the first and second aperture, a transition in which the inner tube has increasing notches and protuberances, wherein the notches, ie the trajectory of the respective notches, in the longitudinal course of the first to the second aperture in the direction of the center of the

Fluid distributor and at the latest at the th aperture converge with the center of the fluid manifold. In contrast to this, the trajectory of the protuberances, ie the radial course of the protuberances, runs in the longitudinal direction from the first to the second aperture in the direction of the outer tube, whereby at the latest at the second aperture the trajectory of the protuberances with the outer tube converges. In this respect, a fluid transition between the circular / annular spatial distribution towards a segment-like spatial distribution of the spaces A and B is provided with the fluid distributor. The outer diameter of the entire fluid distributor can remain the same over the entire length of the distributor, but also vary.

In a preferred embodiment, the cuts around the inner tube are at angles α of a = (0, 2,..., 2n-2) and the protuberances around the inner tube.

In a 360 ° tube at angles a of a = (1, 3, ..., 2 «-l)

2 "net, i. it finds a uniform distribution of

Incisions and protuberances take place. Furthermore, such a preferred arrangement of the cuts or protuberances that the resulting segments that represent the space A, each having an equal area, (in the cross section of the second aperture), but also the segments that represent the space B always one have the same area. The area of a segment representing the space A and the area of a segment representing the space B (in each case relative to the cross section of the second aperture) can always be the same size, ie. the spatial relationship of the spaces A and B to each other is 1: 1, but it can also deviate cross-sectional area ratios occur.

In an advantageous embodiment 1 ≦ n ≦ 1000, preferably 3 ≦ n <500, particularly preferably 30 ≦ n ≦ 100, ie the fluid distributor has the corresponding number of segments. Further, it is advantageous if the ratio of

Cross-sectional areas with respect to space A and space B remains constant over the entire length of the fluid distributor. This preferred embodiment thus provides that at each point of the cross-section of the fluid distributor, the ratio of the area which originates from room A to the area which originates from room B, is the same. In the event that the volumes A and B are the same size, the cross-sectional area of A / B at each point of the fluid distributor is therefore equal to 1 in cross-section. The respective segments A and B at the second aperture are also inferential result in exactly the same areas. However, it is also possible that the cross-sectional areas of the space A can be much larger than those of B and vice versa (e.g., 50: 1 or

100: 1). In the case of the above preferred embodiment, that the area ratio of A to B over the entire length of the fluid distributor is exactly the same, this means that, for example, in the case that space A is greater than space B, the inner tube relative to the outer tube has a relatively large diameter. For the segments present at the second aperture, this means that the segments that represent the space A have a larger cross-section than the segments that represent the space B, so that the segments A are much wider than the segments that represent the space B. Furthermore, it is advantageous that the trajectories of the incisions and / or the protuberances run "sinusoidally." In this case, it is particularly preferred that the trajectory representing the incision and thus a reduction of the tube diameter of the inner tube from the original tube diameter to On the other hand, the trajectories of the protuberances extending from the original tube diameter of the inner tube at the first aperture to a widening of the tube this location, much like a sinusoid between 0 and π / 2. Such guidance of the trajectories results in excellent flow characteristics of the respective fluids within the fluid manifold.

The incisions preferably run in such a way that a wedge-shaped structure results, wherein the acute angle of the wedge can also be rounded or arcuately concave. The same can preferably apply to the protuberances.

In a further advantageous embodiment, webs may be present in the region between the outer and inner tubes which connect the outer and inner tubes and / or webs are present in the inner tube which connect the inner wall of the inner tube and the central axis of the inner tube, ie Webs converge in the central axis. Of course, this embodiment applies to the entire fluid distributor with the exception of the second aperture since, starting from the first aperture, the webs, which are present, for example, between the outer and inner tubes, have converged with the outer tube wall Footbridges used indoors are arranged at the level of the second aperture coincide with the center of the fluid distributor. In a further preferred embodiment it is provided that a core tube or a solid axis is arranged concentrically in the inner tube over the entire length of the fluid distributor, with the proviso that for this case, the second aperture in cross-section instead of the circular sectors circular sectors, wherein the trajectories of the incisions on the core tube or the solid axis terminate and in the event that webs are present in the inner tube, they connect the surface of the core tube or the solid axis with the notch base of the inner tube and the trajectories of the incisions on the core tube or the solid axis branch as soon as the notch base touches the surface of the core tube or the solid axis.

It can be advantageous if the core tube has openings for mass transfer. The respective exchange openings can be fluidically connected to either one of the rooms A or B, but a mass transfer can take place with both rooms. The mass transfer openings of the core tube can be arranged over the entire length of the fluid distributor, but also only in certain areas.

A further preferred embodiment provides that the fluid distributor comprises a further tube arranged longitudinally from the first aperture or the second aperture concentrically around the outer tube and enclosing a space C lying between the further tube and the outer tube, as well as a tube in the longitudinal direction after the second aperture arranged third aperture having in cross section 3n circular sectors, where n is an integer ≥ 1, preferably ≥ 2, and the sectors alternately with space A, space C, space B and space C and so on , wherein between the second and the third aperture the outer tube is arranged longitudinally around the circumference of the tube n incisions at the level of the boundaries of the circular sectors and alternately arranged n outcuts of the circular sectors, wherein

Incision has a Trajektoπe which reduces the radius of the outer tube, starting from the original radius of the outer tube at the height of the second aperture along the direction of the third aperture, wherein all Tra¬ ektoπen the incisions at the height of the third aperture in the center of the cross section of the fluid distributor, and each protuberance has a trajectory which steadily increases the radius of the outer tube from the original diameter of the outer tube to the height of the second aperture along the direction of the third aperture, all trajectories of the third aperture protuberances coinciding with the third aperture converge another tube

This embodiment of the invention is based on the same principle as the general principle of the present invention, namely that by the transition from an inner tube disposed around an outer tube by notches or protuberances of the tube therein, a course of the spaces that lie between these tubes , can be adjusted so that at the exit aperture a segment-like side by side of the formerly concentric arranged spaces can take place The erfmdungsgemaße concept, which was described in the preceding paragraph, is However, not limited to the three spaces mentioned A, B and C, it can connect to the third aperture described there, which is in fluidic contact with three different rooms A, B and C, even more concentric tubes, so that the concept any number of different spaces can be expanded

According to the invention, there is likewise provided a rotationally symmetrical heat and / or material exchanger whose cross-section has at least 2n sectors separated from one another by a membrane, where n is an integer 1, preferably ≥ 2 with respect to the sectors which are suitable for the above-described heat and / or material exchangers likewise represent circular sectors, the special embodiments already mentioned for the fluid distributor also apply, for example with regard to the uniform distribution of the respective segments or the flat cross sections of the individual segments which are to be associated with the spaces A or B.

In a preferred embodiment, the membrane is material impermeable or at least partially permeable to material. In the event that a heat exchange is to take place with this exchanger, it is preferred if the membrane is impermeable to material but has good heat-conducting properties In this case, for example, metals or metal sheets In the event that a mass transfer should take place, semipermeable membranes or porous membranes are preferred In a further preferred embodiment, at least some of the sectors are at least partially equipped on the inside and / or outside with Sorptionsmate- πalien

Further advantageously, the heat exchanger and / or material exchanger comprises a core tube arranged in the center of the heat exchanger and / or substance exchanger or a solid axis, with the proviso that annular sectors are present instead of the circular sectors, the core tube having openings for mass transfer This embodiment of the heat exchanger and / or substance exchanger thus correlates with the above-described embodiment of the fluid distributor, in the event that the latter also has a core tube or a solid tube in the center

Further erfmdungsgemaß an apparatus for heat and / or mass exchange is provided which comprises a heat and / or material exchanger, as described above, wherein at least at one end or both ends of the heat and / or mass transfer a previously described Fluid distributor over the second aperture is form-fitting, wherein the number of sectors of the heat and / or mass exchanger and the fluid distributor is identical The two components are so merged, that the respective sectors of the fluid distributor and the heat and / or material exchanger congruent must come to rest, ie not only the number of sectors of the fluid distributor and the heat and / or mass exchanger must be identical, also the geometry of the sectors (for example, in the case that the sectors representing the space A and the sectors, the represent the room B, in the transverse must not be the same area at the height of the second aperture) must be identical.

The term positive fit may also include that the heat exchanger and the heat exchanger are firmly connected to one another, e.g. welded, glued, etc., are.

In a preferred embodiment, the heat and / or material exchanger and the at least one fluid distributor are axially rotatable relative to one another, wherein the rotation is preferably carried out by means of a motor. The individual components can also be separated by a small gap. The present invention will be explained in more detail below with reference to the attached figures, without restricting the invention to the parameters presented there. The invention described herein relates, in a first aspect, to a fluid distributor I, which starts from concentric inlet and outlet tubes for the fluids A (inner tube) and B (annular space between the inner and outer tube) and can be completely accommodated in a straight tube, which corresponds in outer diameter to the outer inlet and outlet pipe. Typically, "heat exchange" refers to the exchange of heat between the non-mixing fluids through impermeable walls "mass transfer" refers to applications where substances are transferred through the walls (e.g., filtration processes). There are also combinations of heat and mass transfer conceivable; In this case, heat can also be transferred via fabric particles transferred through the walls.

Likewise, by the definition given here of the Adsorption involves attaching a substance to the sorptive coating, but not transferring it to the secondary side.The adsorbed substance is expelled, for example, by thermal desorption with a hot medium following the Adsorption through the same (primary) channels.

Em such fluid distributor I is shown for example in Figure 1 in detail The fluid distributor I is limited by an outer tube 3 and has at the height of the first aperture 1 an inner tube 2. FIG. 1 shows the viewing direction of the second aperture 4, which has the various segments (in this case 6), which result from the transition from the two tubes 2 and 3, which are present on the first aperture side 1, to the segments corresponding to the spaces A (this is the space enclosed by the pipe 2) and B (this is the space lying between the pipes 2 and 3) are the same in this case, ie the individual segments are arranged at an angle of 60 ° to each other. The transition between the first aperture 1 and the second aperture 4 is designed such that the inner tube 2 has both notches 5 and protuberances 6, wherein the notches of the tube 2 with increasing course from the first aperture 1 to the second aperture 4 towards Center converge and meet at the center of the aperture 4. The notches 5 rejuvenate the

Diameter of the tube 2. On the other hand, the tube 2 as well protuberances 6, which expand from the original tube diameter of the tube 2, the tube diameter and converge at the height of the aperture 4 with the outer tube 3. In this way, the flowing transition between the a segmental structure according to the A-pertur 4 achieved at the level of the first aperture 1 The ratio of the cross-sectional areas of the inner tube 2 (fluid A) and the annulus between tube 2 and 3 (fluid B) can be the same fluids and similar mass flows, for example, be 1, so that both cross-sectional areas are the same. The fluid distributor is constructed in such a way that the inside

Pipe 2 and located in the annulus fluids A and B at the end of the manifold m sectors alternately ne next to each other, so ABABAB Figure 3 shows the Em- and the outlet cross-section (inlet aperture 1 and outlet aperture 4) of a distributor I with 6 circular sectors The special feature of the distributor consists in that the cross section continuously changes from concentric circles to circular sectors, on the one hand increasing the diameter of the inner tube and, on the other hand, introducing wedge-shaped incisions 5, which are advantageously dimensioned such that they compensate the increase in area due to the growing diameter It is achieved that the cross-sectional areas for fluid A and B and thus their flow rates remain the same throughout the manifold A transition from the aperture 1 to the aperture 4 is illustrated by several cross-sectional images in Figure 4, the changes in the circumference of the inner tube 2 g It can clearly be seen that, although the diameter of the outer tube 3 remains constant over the entire length from the aperture 1 to the aperture 4, but in the tube 2 Notches 5 and protuberances 6 are mounted, wherein the notches 5 converge at the aperture 4 at the center of the fluid distributor, while the protuberances 6 converge at the height of the aperture 4 with the outer tube 3, whereby the transition of two concentric tubes 2 and 3 at the aperture 1 to a segment-like juxtaposition of the spaces A and B takes place at aperture 4. The specified ratio of the cross-sectional areas for the fluids A and B may also differ significantly from 1, z B if it is fluid A to water and fluid B to In this case, the narrow sectors z B are given the character of water-cooled fins (see FIG. 1 a). Here, a fluid distributor with 15 channels A and 16 channels B with an ash ratio A is shown / B >> 1 shown In order to obtain flow-technically favorable geometries, it is advantageous to determine the increase in diameter and the course of the wedge points Here, for example, is a sinusoidal course The incisions 5 need not be wedge-shaped, they may also be rounded, for example, which may have a positive effect on the flow (FIG. 5).

The main advantage of the invention is that the distributor has a dual function It distributes the fluids continuously and at the same time serves as (pre-) heat and / or material exchanger. From the beginning, heat and / or substance can be transferred Outside surface of the inner tube 2 instead, the exchange surface between the fluids is then increased continuously until the final cross-section is achieved with circular sectors, where she finally reaches her maximum. The number of sectors determines the absolute maximum of the exchange area. Due to the construction, none of the sectors is distinguished from the others and the flow is gradually diverted - without abrupt changes of direction. As a result, a uniform flow is achieved with low pressure drop, so that together with an efficient heat and / or mass transfer a high overall efficiency can be achieved with a compact, modular design. Since the inlet and outlet cross sections 1 and 4 are circular, eliminates the otherwise often common transition pieces that increase pressure loss, cost and space requirements. In the illustrated invention, only the inner tube 2 must be performed before and after the distributor I through the wall of the outer tube 3 (eg via elbows), or the inlet or outlet of the annular space takes place axially or (semi-) radially in one Distance to the inlet or outlet of the inner tube. Various such guides of the fluids A and B and the respective tubes 2 and 3 are shown in Fig. 6, wherein the guide is not limited to the arrow directions. A variant shown in Fig. 7 of the construction described above has in the inner and / or in the outer part of the manifold webs (ribs) 7 and 8, which are internally connected to the central axis and the outside with the outer tube 3. The inner webs 8 each lead from the wedge base radially to the central axis; the outer webs 7 lead radially from the outer contour of the distributor to the outer tube 3 and lie in each case on the bisector between two inner webs. The webs increase both the stability of the construction and, in the case of a heat exchanger, the heat transfer between the fluids. because heat is transported radially by conduction through this fin construction to the exchange surface between the fluids. In. FIG. 8 shows, in analogy to the explanations with regard to FIG. 4, a plurality of cross sections along the fluid distributor from aperture 1 to aperture 4, as a course of the geometric configuration of the inner tube 2 is designed if both between the inner tube 2 and the outer tube 3 webs 7 and in the interior of the inner tube 2 webs 8 are arranged. It can be seen that the webs 8 in course on the aperture 4 also due to the fact that the incisions 5 converge toward the center of the fluid distributor towards the center converge and disappear, while the webs 7 between the protuberances 6 and the outer tube 3 are and even here at the aperture 4 disappear. The result is an extremely stable structure of the fluid distributor, in particular because the inner tube 2 is firmly fixed by the webs 7 in the outer tube 3. This becomes particularly evident in splitters with many sectors (Figure 9). However, the pressure loss increases, so that the decision whether to use webs, also depends on the consideration of the total energy balance. Also constructions with webs can be made rounded (Fig. 10).

The introduction of webs leads to the fact that already the inlet cross sections are divided into several sectors. This makes it possible to flow through both the inner tube and the outer annular space with more than one fluid. This fact can be used for example, by cascading three fluids A, B and C such that they eventually end up in sectors in the order ACBCACBC. This is achieved by distributing the fluids A and B in a first distributor as before and connecting the outlet of this first distributor directly to the inlet of a larger distributor whose inner tube diameter corresponds to the outer tube diameter of the first distributor and whose outlet Inner tube is divided into as many sectors as the outlet of the first distributor in the annular space of the second manifold, a third fluid C is introduced so that finally at the outlet of the manifold all three fluids in the order ACBCACBC .. side by side

(Figure 11). This cascading can theoretically be continued as desired; with another fluid D, for example, the order ADCDBDCDADCDBDCD was achieved. The fluid C may also be supplied to an annular space surrounding the first distributor, as indicated for example in FIG. 11 in the fifth image from the left. Here, the first manifold is enclosed by a further tube 10 and fed to a third fluid C. Here, a deformation of the first fluid distributor takes place at the height of the partitions forming the segments (notches 12) and protuberances 13 at the height of the segments towards the further tube 10, so that a segment-like alternating juxtaposition of the three fluids A, B and C at the height of the third aperture 11 results. By the webs, it is in principle also possible to introduce not only in each case a fluid A and a fluid B at the inlet of the first distributor, but - depending on the number of sectors - several fluids Ai, A ₂ , A _3,. , or B ₁ , B ₂ , B ₃ , the same applies to fluid C. For example, membrane distillation for desalination of seawater: A (cold seawater), B (warm seawater), C (permeate), semipermeable membrane between B and C, condenser foil between A and C The webs between A and B in this case should have a low thermal conductivity so that as little heat exchange between A and B takes place. Another possible application is that two fluids A and B heat up a third fluid C (eg heating of the supply air C) by two exhaust gas streams A and B, which should not mix) Furthermore, the apparatus could be used as a fuel cell, in which A (oxygen) and C (hydrogen) react to B (water) between A and C is an electrolyte membrane, between C and B is a water-permeable membrane Both fluid distributor I and heat exchangers can also be equipped with a core tube K or a solid axis are constructed. The core tube is to be considered in the calculation of the cross-sectional areas As soon as the wedge touches the core tube, the tip is replaced by a circular arc, so that at the outlet of the distributor no longer circular sectors, but circular sectors arise. The transition from the wedge to the circular sector must also be taken into account when calculating the cross-sectional areas

Figure 12 shows sections through a fluid manifold I with core tube K, in Figure 13 is the three-dimensional impression of the transition from the wedge to the circular sector sketched In a special construction of the manifold are openings between the fluid channels and the core tube provided, which allow fluid can flow into the core tube. This may be useful, for example, if fluid A is used for cooling fluid B and accumulates in this condensate, which is to be removed via the core tube K. To allow drainage, vertical installation of the apparatus may be advantageous. For horizontal installation, the channels can be drained one after the other by turning the distributor. In principle, the device can be installed at any angle. The core tube can also be used to supply fluids.

In a second aspect, the present invention relates to a heat and / or material exchanger II, which is shown in FIG. 2 a as a separate component, which is provided with two fluid distributors 1 a and 1 b, which are each at the ends of the heat and / or mass exchanger II can be arranged, is shown. In this case, the respective circular sectors, which can be connected to the fluid distributors Ia and / or Ib, are arranged identically to the resulting divisions of the circular segments on the aperture 4 of the fluid distributor Ia or Ib. In essence, the segments of the heat and / or mass exchanger II run parallel to one another. The membranes may be permeable to fabric and / or fabric impermeable. Likewise, there is the possibility that, as in the case of the preferred embodiments of the fluid distributor I, a core tube may be arranged in the heat and / or material exchanger II.

In a third embodiment, the present invention relates to a heat and / or material exchange apparatus III, which is shown for example in FIG. 2b, and from the assembled parts, which are shown in Figure 2a, is arranged. Thus, the apparatus consists of two fluid distributors Ia and Ib flanking a heat and / or material exchanger II at its respective ends.

The apparatus III consists of at least one, usually two symmetrically arranged fluid distributors Ia and Ib and usually, but not necessarily, from an intermediate heat and / or material exchanger II (Figure 2b). It can be operated both in DC and in countercurrent.

The construction of the apparatus makes it possible to divert the fluid flows into different channels by rotating at least one distributor Ia and / or Ib and / or the heat or material exchanger II around the angle of a circular sector. For example, it is possible to allow fluid A in the inner tube and fluid B to enter the annular space and, depending on the rotation, either fluid A in the inner tube and fluid B in the annular space or fluid A in the annular space and fluid B in the inner tube. In this way, different channel connections can be switched using stepper motors, so that valves can be omitted. Due to the alternating arrangement of the sectors only one direction of rotation is required; each indexing by the angle of a sector alternates between inner tube and annulus, a further rotation in the same direction by the same angle switches back to the original state. In this way, the distributor receives a third function; he is thus fluid distributor, heat and / or material exchanger and actuator in a component. This function can be used especially if the channels have different functions and the fluids alternately have these functions should use.

In addition to the classic heat exchanger application in cocurrent or countercurrent, the appliance shown in combination with the actuator function by turning the possibility to build a sorption heat exchanger, which can be used for example for solar air conditioning. Such a conventional plate-type sorption heat exchanger is described in EP 1 508 015 B1. This has heat exchanger and sorption channels which are in thermal contact (eg alternately stacked). On the inner surfaces of the sorption channels, a sorption material is applied. The heat exchange channels contain a cooling fluid, the sorption channels a fluid from which at least one component is to be extracted, which can be absorbed by the sorption material. The sorption heat exchanger also contains humidifying components for humidification or supersaturation of the cooling fluid. Typically, both fluids are air of different temperature and humidity; the medium to be extracted is water, and various sorbents (for example silica gel) can be used as the sorption material. The sorption heat exchanger of the prior art requires a plurality of valves to distribute different air flows to heat exchange or sorption channels. In the apparatus III described here, this can be done by rotation of the distributor Ia and / or Ib. A possible mode of operation is shown below as an example for a ventilation mode (supply air is conditioned ambient air) in DC configuration: The fluids at the inlet are exhaust air (inside) and ambient air (outside), the middle piece here consists of heat exchanger and sorption sectors, at the outlet are the fluids exhaust air (inside) and supply air (outside). For the regeneration of the sorption material there should be the possibility to heat the ambient air (eg by heat from solar panels). The ambient air can already be heated in a component upstream of the distributor or, for example, via the jacket surface of the outer tube at the inlet. The heat exchanger ducts must be able to be humidified, so humidifiers, eg nozzles, should be provided which supply water radially to every other sector. The heat exchanger and the sorption channels can be provided with further internal ribs (radially or parallel to the cylindrical surface) to increase the surface area within each sector.

In the following, the various switching states are to be illustrated with reference to FIG. 14. The following abbreviations are used:

UL = ambient air AL = exhaust air ZL = supply air

FL = exhaust air

WK = heat exchanger channels

SK = sorption channels 1) conditioning fresh air

Sheath heater on entry (or no supply of hot regeneration air) Humidification in WK on

UL - »SK (Adsorption) -> ZL AL -> WK -> FL 2) Rotation of manifold 2 (exit)

3) Regeneration adsorbent

Jacket heating at the inlet (or supply of hot regeneration air)

Humidification in WK from UL -> SK (Desorption) -> FL

AL -> WK -> ZL (WK does not flow through in apparatus Al, AL is switched to second apparatus)

4) Rotation of manifold 1 (inlet) and manifold 2 (outlet)

5) Pre-cooling heat exchanger jacket heating at inlet (or no supply of hot regeneration air t) Humidification in WK at UL - »WK -τ> FL AL -> SK -> ZL (WK does not flow through in apparatus A1, AL opens second device switched)

6) Rotation of manifold Ia (entrance)

7) = 1)

In addition to the described apparatus A1, a second apparatus A2 is required, which carries out the same steps 1) to 7) with a time delay: while one of the apparatuses performs step 1), the other executes steps 3) to 5). In the event that the exhaust air is taken from the same room in which the supply air is fed, and the exhaust air must be conducted into the environment from which the ambient air is removed, the fluids must be recirculated accordingly. This can be done in a third apparatus A3 consisting of only two by one sector arranged distributed distributors without middle piece and in the reverse direction compared to the apparatuses Al and A2 flows through. The exhaust air from the outlet of Al / Manifold 2 or A2 / Manifold 2 (inside) is introduced into A3 / Manifold 1 (inside) and eventually blows open out of the annulus into the environment (because the manifolds have been crossed). The exhaust air of the room is in turn sucked open in the annulus of A3 / distributor 1 and ends in. A3 / distributor 2 (inside), which in turn with Al or

2 / distributor 1 (inside) is connected. A3 / distributor 2 (inside) must be connected to Al / distributor 1 and A2 / distributor 1 via a changeover valve so that the exhaust air is blown into either Al or A2 depending on the process step.

The geometry of the manifolds is very complex. Due to undercuts the production is therefore demanding. It may therefore be advantageous to produce individual distribution channels, which are then applied radially on an axis. These distributor channels, which correspond, for example, to those for fluid A in FIG. 9, can be manufactured, for example, by internal high-pressure forming (hydroforming, eg hydroforming). IHU is state of the art and is widely used for the production of complex components. It is conceivable to manufacture the channels from a tube (FIG. 15) or from a partially plated sheet metal composite which is shaped by generating an internal pressure in the regions not connected by a previously applied separating means (FIG. 16). In both cases, the shaping is achieved by forming in a suitable tool (pressing into the tool by internal pressure). Another possibility is to weave the channels three-dimensionally (this technology already exists) and then optionally stabilize them with a hardening material, such as epoxy resin.

Claims

claims

A rotationally symmetrical fluid distributor (I), comprising, in the longitudinal direction, a first aperture (1) having in cross-section two concentrically arranged tubes (2, 3), the inner tube (2) enclosing a first space A, the outer (1) 3) and the inner (2) 10 tube enclosing a space B and the outer

Pipe (3) defines the diameter of the fluid distributor (I), and a second aperture (4) having in cross section 2n circular sectors, where n is an integer 15> 1, preferably ≥ 2, and the sectors alternately with space A or Room B, characterized in that between the first and the second aperture 20, the inner tube (2) in the longitudinal direction around the

Pipe circumference arranged around n incisions (5) and alternately arranged n protuberances (6), wherein the 3 recess (5) has a longitudinal direction 25 from the first (1) to the second aperture (4) extending trajectory, the radius of the inner tube (2) starting from the original radius of the inner tube (2) at the height of the first aperture (1) along the direction of the second aperture (4) continuously reduced, wherein all trajectories of the incisions (5) at the height of the second aperture ( 4) converge at the center of the fluid manifold, and each protuberance (6) has a trajectory extending in the longitudinal direction from the first (1) to the second aperture (4), the radius of the inner tube (2) starting from the original diameter of the inner tube (2) at the level of the first aperture (1 ) are continuously increased longitudinally in the direction of the second aperture (4), with all the trajectories of the protuberances (6) converging with the outer tube (3) at the level of the second aperture (4).

2. Fluid distributor according to claim 1, characterized in that the incisions (5) to the inner tube (2) at

Angles a of a = (0, 2, ..., 2n-2) and

2 "the protuberances (6) around the inner tube (2)

Angles α of a = (1, 3, ..., 2n- \)

In are arranged.

3. Fluid distributor according to one of the preceding claims, characterized in that 1 ≤ n ≤ 1000, preferably 3 ≤ n ≤ 500, particularly preferably

30 ≤ n <100.

4. Fluid distributor according to one of the preceding claims, characterized in that the ratio of the cross-sectional areas with respect to space A and space B over the entire length of the fluid distributor (I) remains constant.

5. Fluid distributor according to one of the preceding claims, characterized in that the trajectories of the incisions (5) and / or the protuberances (6) are sinusoidal.

6. Fluid distributor according to one of the preceding claims, characterized in that the input sections (5) are substantially wedge-shaped, wherein the acute angle of the wedge may also be rounded or arcuate concave.

7. Fluid distributor according to one of the preceding arrival claims, characterized in that in the area between the outer (3) and inner tube (2) webs (7) are present, the outer (3) and inner tube (2) connect and / or in the inner tube (2) webs (8) are present, which connect the inner wall of the inner tube (2) and the central axis of the inner tube (2).

8. fluid distributor according to one of the preceding claims, characterized in that concentrically in the inner tube (2) over the entire length of the fluid distributor a core tube (K) or a solid axis is arranged, with the proviso that in this case the second aperture

(4) has circular-section sectors instead of the circular sectors, with the trajectories of the cuts (5) ending on the core tube (K) or the solid axle and, in the case that webs (8) are present in the inner tube (2), these connect the surface of the core tube or the solid axis with the notch base of the inner tube (2) and the trajectories of the incisions

(5) branching on the core tube (K) or the solid axis as soon as the notch bottom touches the surface of the core tube (K) or the solid axis.

9. fluid distributor according to the preceding claim, characterized in that the core tube (K) has openings for mass transfer.

Fluid distributor according to one of the preceding claims, comprising a further tube (10) arranged longitudinally of the first aperture (1) or the second aperture (4) concentrically around the outer tube 5 (3), which connects between the further tube (10). 10) and the outer tube (3) lying space C encloses, as well as in the longitudinal direction after the second aperture (4) arranged third aperture (11) having 10 in cross section 3n circular sectors, where n is an integer ≥ 1, preferably ≥ 2 and the sectors are alternately labeled with room A, room C, room B and room C, etc, characterized

15 that between the second (4) and the third

(11) Aperture the outer tube (3) arranged in the longitudinal direction around the circumference of the tube n incisions (12) at the height of the boundaries of the circular sectors and alternately arranged n Ausstulpun

20 gene (13) of the circular sectors, each notch (12) has a trajectory, the radius of the outer tube (3) starting from the original radius of the outer tube (3) at the height of the second aperture (4)

25 along xn direction of the third aperture (11) continuously reduced, with all the trajectories of the incisions (12) converge at the height of the third aperture (11) in the center of the fluid distributor, and

30 each protuberance (13) has a trajectory which continuously increases the radius of the outer tube (3) starting from the original diameter of the outer tube (3) at the height of the second aperture (4) in the direction of the third aperture (11). enlarged, all trajectories of the protuberances (13) converging at the level of the third aperture (11) with the further tube (10).

11. A rotationally symmetrical heat and / or material exchanger (II) whose cross section has at least 2n sectors separated from one another by a membrane, where n is an integer I _1, preferably> 2.

12. Heat and / or material exchanger (II) according to the preceding claim, characterized in that the membrane is material impermeable to material or at least partially permeable.

13. Heat and / or material exchanger (II) according to one of the two preceding claims, character- ized in that at least part of the sectors is at least partially equipped on the inside and / or outside with sorbent materials.

14. heat and / or material exchanger (II) according to one of claims 11 to 13, comprising a center of the heat and / or mass transfer in the longitudinal direction arranged core tube or solid axis, with the proviso that instead of the circular sectors circular ring sectors are present, wherein the core tube may have openings for mass transfer with at least a part of the circular ring sectors.

15. apparatus for heat and / or mass transfer (III) comprising a heat and / or material exchanger according to one of claims 11 to 15 wherein at least one end of the heat and / or mass exchanger with a fluid distributor according to one of claims 1 to 8 via its second aperture. is conclusively connected, wherein the number of sectors of the heat and / or mass exchanger and the fluid distributor are identical.

16. Apparatus (III) according to the preceding claim, characterized in that the heat and / or material exchanger and the at least one Fluidver divider are axially rotatable relative to each other, wherein the rotation is preferably carried out by means of a motor.