EP2379978B1 - Rotationally symmetrical fluiddistributor - Google Patents

Description

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

Fluid distributors are known inter alia from FR 983.419. 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 heat recovery. 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 It is to distribute the volume flow of fluids from the respective supply lines evenly on these channels. At the same time this should be streamlined, so that the pressure loss remains as low as possible. The prior art often requires a transition from circular cross-section tubes to numerous parallel channels of rectangular cross-section, with only every second channel allowed to flow therethrough.

In itself, the distribution of fluid flows in plate heat exchangers is already solved by the geometry (only every second channel is accessible to the flow). In this respect, the distribution of the fluids can not be solved by complicated transition pieces. However, this principle results in a sudden change in cross section (halving), since every second channel is closed and the fluid has to flow around these areas. This leads to high pressure losses. The transition pieces lead from a round to an angular cross-section and for the separation of the fluids different cross-sections are flown. The prior art often requires a transition from circular cross section tubes to a rectangular cross section flow area.

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

Proceeding from this, it was an object of the present invention to provide a novel fluid distributor, the dentlich simplifies the construction of a heat exchanger and allows the operation of the heat exchanger without valves.

This object is achieved with respect to the fluid distributor with the features of claim 1 and with respect to an apparatus for heat and / or mass transfer with the features of claim 10, wherein each represent the dependent claims advantageous developments.

• eine erste Apertur, die im Querschnitt zwei konzentrisch angeordnete Rohre aufweist, wobei das innere Rohr einen ersten Raum A einschließt, das äußere und das innere Rohr einen Raum B umschließen und das äußere Rohr den Durchmesser des Fluidverteilers vorgibt, sowie
• eine zweite Apertur, die im Querschnitt 2n Kreissektoren aufweist, wobei n eine ganze Zahl ≥ 1, vorzugsweise ≥ 2, ist und die Sektoren abwechselnd mit Raum A oder Raum B in Verbindung stehen, wobei zwischen der ersten und der zweiten Apertur das innere Rohr in Längsrichtung um den Rohrumfang herum angeordnet n Einschnitte und alternierend angeordnet n Ausstülpungen aufweist, umfasst,
• wobei jeder Einschnitt eine in Längsrichtung von der ersten zur zweiten Apertur verlaufende Trajektorie aufweist, die den Radius des inneren Rohres ausgehend vom ursprünglichen Radius des inneren Rohres auf Höhe der ersten Apertur längs in Richtung der zweiten Apertur stetig verkleinert, wobei alle Trajektorien der Einschnitte auf Höhe der zweiten Apertur im Mittelpunkt des Querschnitts des Fluidverteilers zusammenlaufen, und jede Ausstülpung eine in Längsrichtung von der ersten zur zweiten Apertur verlaufende Trajektorie aufweist, die den Radius des inneren Rohres ausgehend vom ursprünglichen Durchmesser des inneren Rohres auf Höhe der ersten Apertur längs in Richtung der zweiten Apertur stetig vergrößert, wobei alle Trajektorien der Ausstülpungen auf Höhe der zweiten Apertur mit dem äußeren Rohr zusammenlaufen.

According to the invention, a rotationally symmetrical fluid distributor is thus 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 2n circular sectors in cross section, where n is an integer 1, preferably ≥ 2, and the sectors are alternately associated with space A or space B, with the inner pipe in between the first and second apertures Arranged longitudinally around the pipe circumference n incisions and alternately arranged n has protuberances comprises,
• wherein each incision has a longitudinally extending from the first to the second aperture trajectory, the radius of the inner tube from the original radius of the inner tube at the height of the first aperture along the direction of the second aperture continuously reduced, all trajectories of the incisions in height the second aperture converge at the center of the cross-section of the fluid manifold, and each protuberance a longitudinally extending from the first to the second aperture trajectory, which increases the radius of the inner tube from the original diameter of the inner tube at the level of the first aperture longitudinally in the direction of the second aperture, all trajectories of the protuberances at the level of 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, a transition takes place between the first and second apertures, in which the inner tube has increasing indentations and protuberances, the notches, ie the trajectories of the respective indentations, extending in the longitudinal direction from the first to the second aperture in the direction of the center of the fluid distributor and at the latest at the second Aperture converge with the center of the fluid manifold. In return, the trajectory of the protuberances, ie the radial course of the protuberances, in the longitudinal course of the first to the second aperture in the direction of the outer tube, wherein at the latest at the second aperture, the trajectory of the protuberances merges with the outer tube. 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.

und die Ausstülpungen um das innere Rohr bei Winkeln α von $\alpha =\left(1,3,\dots ,2n-1\right)\frac{360°}{2n}$

angeordnet, d.h. es findet eine gleichmäßige Verteilung der Einschnitte und Ausstülpungen statt. Weiter bedingt eine derartige bevorzugte Anordnung der Einschnitte bzw. Ausstülpungen, dass die daraus resultierenden Segmente, die den Raum A repräsentieren, jeweils eine gleiche Fläche, (im Querschnitt der zweiten Apertur) aufweisen, aber auch die Segmente, die den Raum B repräsentieren stets eine gleiche Fläche aufweisen. Die Fläche eines Segmentes, das den Raum A repräsentiert, und die Fläche eines Segmentes, das den Raum B repräsentiert (jeweils bezogen auf den Querschnitt der zweiten Apertur), können dabei immer gleich groß sein, d.h. das räumliche Verhältnis der Räume A und B zueinander ist 1:1, es können jedoch auch hiervon abweichende Querschnittsflächenverhältnisse auftreten.In a preferred embodiment, the cuts are around the inner tube at angles α of $\alpha =\left(0.2.....2n-2\right)\frac{360°}{2n}$

and the protuberances around the inner tube at angles α of $\alpha =\left(1.3.....2n-1\right)\frac{360°}{2n}$

arranged, ie there is a uniform distribution of the incisions and protuberances instead. 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 one another 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.

Furthermore, it is advantageous if the ratio of the 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. Thus, in the case where the volumes A and B are equal, the cross-sectional area of A / B at each point of the fluid distributor is equal to 1 in cross-section. In conclusion, the respective segments A and B resulting at the second aperture also have 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 (eg 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 representing the space A have a larger cross-section than the segments representing the space B, so that the segments A are substantially wider than the segments representing the space B. The trajectories of the incisions and / or the protuberances are "sinusoidal" Here, the trajectory that represents the incision and thus leads to a reduction of the tube diameter of the inner tube from the original tube diameter to 0 (at the second aperture), approximately so On the other hand, the trajectories of the protuberances, which, starting from the original tube diameter of the inner tube at the first aperture, lead to a widening of the tube at this point, much like a sinusoid between 0 and π /. second 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 arcuate 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 the webs run in the middle axis together. This embodiment of course applies to the entire fluid distributor except at the level of the second aperture, since starting from the first aperture, the webs, which are present for example between the outer and inner tube, have run together with the wall of the outer tube or the webs, the inner tube are arranged coincide at the level of the second aperture with the center of the fluid manifold.

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 in this case the second aperture in cross-section instead of the circular sectors circular sectors, said trajectories the incisions on the core tube or the solid axis terminate and, in the case that webs are present in the inner tube, these 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 bottom 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 stand between the second and the third aperture, the outer tube in the longitudinal direction around the tube circumference around n incisions at the level of the boundaries of the circular sectors and alternately arranged n protuberances of the circular sectors, each incision having a trajectory which the radius of the outer tube starting from the original radius of the outer tube at the level of the second aperture along the direction of the third aperture, with all the trajectories of the incisions converging at the level of the third aperture in the center of the cross section of the fluid distributor, and each protuberance having a trajectory which the radius of the outer tube starting from the original one Diameter of the outer tube at the height of the second aperture is continuously increased longitudinally in the direction of the third aperture, all trajectories of the protuberances converge at the level of the third aperture with the other 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 outer tube disposed around an inner tube by notches or protrusions of the tube therein, a course of the spaces between these tubes lie, can be adjusted so that at the exit aperture a segment-like side by side of the previously concentric arranged spaces can be done. The inventive concept 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 therein, 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.

The fluid distributor according to the invention can be used in 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 regard to the sectors described above with respect to the sectors which also constitute circular sectors for the heat and / or material exchanger described above, the particular embodiments already mentioned for the fluid distributor apply, for example with regard to the uniform distribution of the respective segments or the area cross sections of the individual segments to be associated with the rooms A or B.

The membrane may be cloth-impermeable or at least partially permeable to fabric. In the event that a heat exchange is to take place with this exchanger, it is preferred if the membrane is material-impermeable, but has good heat-conducting properties. Particularly suitable materials for the membrane in this case are, for example, metals or metal sheets. In the event that a mass transfer should take place, semipermeable membranes or porous membranes are preferred.

At least a portion of the sectors may be at least partially equipped with sorbent materials on the inside and / or outside.

Further advantageously, the heat and / or material exchanger comprises a core tube arranged in the center of the heat and / or mass exchanger in the longitudinal direction, with the proviso that annular sectors are present instead of the circular sectors, wherein the core tube openings for mass transfer with at least one part may have the circular sectors. This heat and / or material exchanger thus correlates with the previously described embodiment of the fluid distributor, in the event that it also has a core tube or a solid tube in the center.

Further, according to the invention, there is provided a heat and / or mass exchange apparatus comprising a heat and / or mass heat exchanger as described above, wherein at least one end or both ends of the heat and / or mass exchanger is one as described above Fluid distributor is positively mounted over the second aperture, wherein the number of sectors of the heat and / or mass exchanger and the fluid distributor is identical. The two components are joined together in such a way that the respective sectors of the fluid distributor and of the heat and / or mass exchanger congruently come to rest, ie not only the number of sectors of the fluid distributor and of the heat and / or mass exchanger must be identical the geometry of the sectors (for example, in the case where the sectors representing space A and the sectors representing space B are in cross section must not be the same area at the height of the second aperture) must be identical.

The term positive fit can also include that distributor and heat / material exchanger firmly connected to each other, 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. "Heat exchange" usually refers to the exchange of heat between the non-mixing fluids through impermeable walls. "Substance exchange" refers to applications in which substances are transferred through the walls (eg filter 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 "Stoffaustausch" includes adsorptive processes. During adsorption, a substance is attached to the sorptive coating, but not transferred to the secondary side. The expulsion of the adsorbed substance takes place, for example, via thermal desorption with a hot medium, which flows through the same (primary) channels following adsorption.

Such a fluid distributor I is for example in FIG. 1 shown in detail. The fluid distributor I is limited by an outer tube 3 and has at the level of the first aperture 1 an inner tube 2. In FIG. 1 the viewing direction is shown on the second aperture 4, which has the various segments (in this case 6) resulting from the transition from the two tubes 2 and 3 present on the first aperture side 1. The segments corresponding to the spaces A (this is the space enclosed by the pipe 2) and B (this is the space between the pipes 2 and 3) are the same in this case, ie the individual segments are 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 height of the aperture 4 in the center. The notches 5 thereby taper the diameter of the tube 2. On the other hand, the tube 2 also has protuberances 6, which expand from the original tube diameter of the tube 2, the tube diameter and converge at the level of the aperture 4 with the outer tube 3. In this way, through the flowing transition between the one another ordered tubes 2 and 3 at the level of the first aperture 1 achieved a segmental structure according to the aperture 4.

The ratio of the cross-sectional areas of the inner tube 2 (fluid A) and the annular space between tube 2 and 3 (fluid B) may be 1, for example, with the same fluids and similar mass flows, so that both cross-sectional areas are equal. The fluid distributor is constructed in such a way that the fluids A and B located in the inner tube 2 and in the annular space are alternately adjacent to one another in circular sectors at the end of the distributor, ie ABABAB .......

FIG. 3 shows the inlet and the outlet cross-section (inlet aperture 1 and outlet aperture 4) of a distributor I with 6 circular sectors. The peculiarity of the distributor is that the cross section continuously changes from concentric circles to circular sectors, on the one hand increases the diameter of the inner tube and on the other hand, for example, wedge-shaped incisions 5 are introduced, which are advantageously dimensioned such that they increase the area increase by the growing diameter again compensate. This ensures that the cross-sectional areas for fluid A and B and thus also their flow rates remain the same throughout the distributor.

A transition from the aperture 1 to the aperture 4 is based on several cross-sectional images in FIG FIG. 4 shown, which represent the changes in the circumference of the inner tube 2 in more detail. 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 level of the aperture 4 with the outer tube 3, whereby the transition of two concentric tubes 2 and 3 in the Aperture 1 to a segment-like juxtaposition of the spaces A and B takes place at aperture 4.

The fixed ratio of the cross-sectional areas for the fluids A and B may also differ significantly from 1, e.g. when fluid A is water and fluid B is air (e.g., an air-water heat exchanger). In this case, the narrow sectors get e.g. the character of water-cooled ribs (see Fig. La). Here a fluid distributor with 15 channels A and 16 channels B with an area ratio A / B >> 1 is shown.

In order to obtain aerodynamically favorable geometries, it is advantageous to determine the diameter increase and the course of the wedge tips. Favorable here is, for example, a sinusoidal course. The cuts 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 already serves as a pre-heat and / or mass exchanger. Heat and / or fabric can be transferred from the beginning. Initially, this takes place only over the outer surface of the inner tube 2; the exchange surface between the fluids is then increased continuously until the final cross-section is reached with circular sectors, where she finally reaches her maximum. The number of sectors determines the absolute maximum of the exchange area. By design, none of the sectors are excellent over 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 corresponding tubes 2 and 3 are in Fig. 6 illustrated, wherein the guide is not limited to the arrow directions.

An in Fig. 7 illustrated variant 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 outside to 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 heat conduction through this fin construction to the exchange surface between the fluids.

In FIG. 8 are in analogy to the comments regarding FIG. 4 a plurality of cross sections along the fluid distributor from aperture 1 to aperture 4 shown as a course of the geometric configuration of the inner tube 2 is designed when both between the inner tube 2 and the outer tube 3 webs 7 and in the interior of the inside lying 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. As a result, 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 distributors with many sectors ( Fig. 9 ). However, the pressure loss increases, so that the decision whether to use webs, also depends on the consideration of the total energy balance. Even constructions with bars 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 so as to be adjacent to each other 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 inner tube is divided into just as many sectors is like the exit of the first distributor. In the annular space of the second distributor, a third fluid C is introduced, so that finally at the outlet of the distributor all three fluids in the order ACBCACBC ... are adjacent ( Fig. 11 ). This cascading can theoretically be continued as desired; with another fluid D, for example, the order ADCDBDCDADCDBDCD ... would be achieved. The fluid C can also be supplied in an annular space surrounding the first manifold, as in eg Fig. 11 indicated in the fifth picture from the left. Here, the first distributor is enclosed by a further tube 10 and fed to a third fluid C. In this case, a deformation of the first fluid distributor at the level of the partitions forming the segments (notches 12) and protuberances 13 at the level of the segments towards the other tube 10, so that a segment-like alternating juxtaposition of the three fluids A, B and C at the level of the third aperture 11 results. Due to the webs, it is in principle also possible to introduce not just one fluid A and one fluid B at the inlet of the first distributor, but-depending on the number of sectors-several fluids A ₁ , A ₂ , A ₃ , .... ..... or B ₁ , B ₂ , B ₃ , .......... The same applies to Fluid C. For example, cascading could be useful for chemical reactions or membrane or filter processes. An example is the membrane distillation for seawater desalination: A (cold sea water), B (warm sea water), C (permeate), semipermeable membrane between B and C, capacitor film between A and C. The webs between A and B should in this case a low Have thermal conductivity, so that the least possible heat exchange between A and B takes place. Another application is that two fluids A and B heat a third fluid C (eg heating of the supply air C by two exhaust 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 manifolds I and heat exchangers can also be constructed with a core tube K or a solid axis. The core tube must be taken into account when calculating the cross-sectional areas. Once the wedge touches the core tube, the tip is replaced by a circular arc, so that eventually no longer circular sectors, but circular sectors arise at the outlet of the distributor. The transition from the wedge to the annulus sector must also be taken into account when calculating the cross-sectional areas.

Fig. 12 shows sections through a fluid distributor I with core tube K; in Fig. 13 is the three-dimensional impression of the transition from the wedge to the circular sector sketched. In a special construction of the manifold, there 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.

A heat and / or material exchanger II, the in FIG. 2a is shown as a separate component which can be arranged with two fluid distributors Ia and Ib, which can be arranged in each case at the ends of the heat and / or mass exchanger II. 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 are parallel to each other. The membranes may be permeable to material 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 second embodiment, the present invention relates to an apparatus for heat and / or material exchange III, the example in FIG. 2b is shown, and from the assembled parts, in the FIG. 2a are presented, 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 as a rule, but not necessarily, from an intermediate heat and / or material exchanger II ( Fig. 2b ). It can be operated both in DC and in countercurrent.

The construction of the apparatus makes it possible to divert the fluid streams 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 illustrated apparatus 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 sorption heat exchanger in conventional design with parallel plates is in EP 1 508 015 B1 described. 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 include a cooling fluid, the sorption channels a fluid from which at least one component to be extracted from the sorbent material is to be extracted. The sorptive 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 sorbent material. The sorption heat exchanger of the prior art requires a plurality of valves to distribute different air streams 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). To regenerate the sorbent material, it should be possible to heat the ambient air (e.g., by heat from solar panels). The heating of the ambient air may already take place in a component upstream of the distributor or e.g. take place over the outer surface of the outer tube at the entrance. The heat exchanger ducts must be able to be humidified, therefore humidifiers, e.g. Nozzle to provide, which provide radially every other sector with water. 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.

UL =

Umgebungsluft

AL =

Abluft

ZL =

Zuluft

FL =

Fortluft

WK =

Wärmetauscherkanäle

SK =

Sorptionskanäle

1. 1) Konditionierung Frischluft Mantelheizung am Eintritt aus (bzw. keine Zufuhr von heißer Regenerationsluft) Befeuchtung in WK an
   UL → SK (Adsorption) → ZL
   AL → WK → FL
2. 2) Drehung von Verteiler 2 (Austritt)
3. 3) Regeneration Adsorbens
   Mantelheizung am Eintritt an (bzw. Zufuhr von heißer Regenerationsluft)
   Befeuchtung in WK aus
   UL → SK (Desorption) → FL
   AL → WK → ZL (WK in Apparat A1 nicht durchströmt, AL wird auf zweiten Apparat geschaltet)
4. 4) Drehung von Verteiler 1 (Eintritt) und Verteiler 2 (Austritt)
5. 5) Vorkühlung Wärmetauscher
   Mantelheizung am Eintritt aus (bzw. keine Zufuhr von heißer Regenerationsluft)
   Befeuchtung in WK an
   UL → WK → FL
   AL → SK → ZL (WK in Apparat A1 nicht durchströmt, AL wird auf zweiten Apparat geschaltet)
6. 6) Drehung von Verteiler Ia (Eintritt)
7. 7)=1)

The following are the various switching states with reference to Fig. 14 being represented. The following abbreviations are used:

UL =

ambient air

AL =

exhaust

ZL =

supply air

FL =

Exhaust air

WK =

heat exchanger channels

SK =

sorption

1. 1) Conditioning fresh air jacket heating at inlet (or no supply of hot regeneration air ) moistening in WK
   UL → SK (adsorption) → ZL
   AL → WK → FL
2. 2) Rotation of manifold 2 (exit)
3. 3) Regeneration adsorbent
   Jacket heating at the inlet (or supply of hot regeneration air)
   Humidification in WK off
   UL → SK (desorption) → FL
   AL → WK → ZL (WK does not flow through apparatus A1, AL is switched to second apparatus)
4. 4) Rotation of manifold 1 (inlet) and manifold 2 (outlet)
5. 5) Pre-cooling heat exchanger
   Jacket heating at the inlet (or no supply of hot regeneration air)
   Humidification in WK
   UL → WK → FL
   AL → SK → ZL (WK does not flow through apparatus A1, AL is switched to second apparatus)
6. 6) Rotation of manifold Ia (entrance)
7. 7) = 1)

In addition to the described apparatus A1, a second apparatus A2 is needed which executes 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 guided, and the exhaust air must be conducted into the environment from which the ambient air is removed, the fluids must be recycled accordingly. This can be done in a third apparatus A3 consisting of only two by one sector staggered distributors without center piece exists and is flowed through in the reverse direction in comparison to the apparatuses A1 and A2. The exhaust air from the outlet of A1 / 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 into the annular space of A3 / distributor 1 and ends in A3 / distributor 2 (inside), which in turn is connected to A1 or 2 / distributor 1 (inside). A3 / distributor 2 (inside) must be connected to A1 / distributor 1 and A2 / distributor 1 via a changeover valve so that the exhaust air is blown into either A1 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 distribution channels, eg those for fluid A in Fig. 9 can be made for example by hydroforming (hydroforming, hydroforming). IHU is state of the art and is widely used for the production of complex components. It is conceivable to make the channels out of a tube ( Fig. 15 ) or from a partially plated sheet metal composite, which is formed by generating an internal pressure in the areas not connected by a previously applied release agent ( 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, if appropriate, subsequently with a hardening material, such as e.g. Epoxy resin, to stabilize.

Claims (14)

1. Rotationally-symmetrical fluid distributor (I) comprising, in the longitudinal direction,
   a first aperture (1) which has two tubes (2, 3) disposed concentrically in cross-section, the inner tube (2) enclosing a first chamber A, the outer (3) and inner (2) tube enclosing a chamber B and the outer tube (3) prescribing the diameter of the fluid distributor (I), and also
   a second aperture (4) which has 2n circular sectors in cross-section, n being an integer ≥ 1, preferably ≥ 2, and the sectors being in connection alternately with chamber A or chamber B,
   between the first and second aperture the inner tube (2) having n notches (5) disposed in the longitudinal direction around the tube circumference and n protuberances (6) disposed alternately,
   each notch (5) having a trajectory which extends in the longitudinal direction from the first (1) to the second aperture (4) and constantly reduces 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) longitudinally in the direction of the second aperture (4), all of the trajectories of the notches (5) converging in the centre of the fluid distributor at the height of the second aperture (4), and
   each protuberance (6) having a trajectory which extends in the longitudinal direction from the first (1) to the second aperture (4) and constantly increases the radius of the inner tube (2), starting from the original diameter of the inner tube (2), at the height of the first aperture (1) longitudinally in the direction of the second aperture (4), all of the trajectories of the protuberances (6) converging with the outer tube (3) at the height of the second aperture (4),
   characterised in that
   the trajectories of the notches (5) and of the protuberances (6) extend sinusoidally,
   the trajectory which represents the notch (5) essentially extending just like a sine curve between n/2 and n, and
   the trajectory which represents the protuberance (6) essentially extending just like a sine curve between 0 and n/2.
2. Fluid distributor according to claim 1, characterised in that
   the notches (5) are disposed around the inner tube (2) at angles α of $$\alpha =\left(0,2,\dots ,2n-2\right)\frac{360°}{2n}$$

   

   
   and the protuberances (6) are disposed around the inner tube (2) at angles α of $$\alpha =\left(1,3,\dots ,2n-1\right)\frac{360°}{2n}$$

   
3. Fluid distributor according to one of the preceding claims, characterised in that there applies 1 ≤ n ≤ 1,000, preferably 3 ≤ n ≤ 500, particularly preferred 30 ≤ n ≤ 100.
4. Fluid distributor according to one of the preceding claims, characterised in that the ratio of the cross-sectional areas relating to chamber A and chamber B remains constant over the entire length of the fluid distributor (I).
5. Fluid distributor according to one of the preceding claims, characterised in that the notches (5) are essentially wedgeshaped, the acute angle of the wedge being able also to be rounded or curved concavely.
6. Fluid distributor according to one of the preceding claims, characterised in that, in the region between outer (3) and inner tube (2), webs (7) are present which connect the outer (3) and inner tube (2) 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).
7. Fluid distributor according to one of the preceding claims, characterised in that a core tube (K) or a solid axis is disposed concentrically in the inner tube (2) over the entire length of the fluid distributor, with the proviso that in this case the second aperture (4) has, instead of the circular sectors, circular ring sectors, the trajectories of the notches (5 ending on the core tube (K) or on the solid axis, and in the case where webs (8) are present in the inner tube (2), these connect the surface of the core tube or on the solid axis to the notch base of the inner tube (2), and the trajectories of the notches (5) branch off on the core tube (K) or on the solid axis, as soon as the notch base contacts the surface of the core tube (K) or of the solid axis.
8. Fluid distributor according to the preceding claim, characterised in that the core tube (K) has openings for material exchange.
9. Fluid distributor according to one of the preceding claims, comprising a further tube (10) which is disposed in the longitudinal direction from the first aperture (1) or from the second aperture (4) concentrically around the outer tube (3) and encloses a chamber C which is situated between the further tube (10) and the outer tube (3),
   and also a third aperture (11) which is disposed in the longitudinal direction after the second aperture (4) and has in cross-section 3n circular sectors, n being an integer ≥ 1, preferably ≥ 2, and the sectors being in connection alternately with chamber A, chamber C, chamber B and chamber C etc.,
   characterised in that ,
   between the second (4) and the third (11) aperture, the outer tube (3) has n notches (12) disposed in the longitudinal direction around the tube circumference at the height of the boundaries of the circular sectors and n protuberances (13) of the circular sectors disposed alternately,
   each notch (12) having a trajectory which constantly reduces 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) longitudinally in the direction of the third aperture (11), all of the trajectories of the notches (12) converging in the centre of the fluid distributor at the height of the third aperture (11), and
   each protuberance (13) having a trajectory which constantly 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) longitudinally in the direction of the third aperture (11), all of the trajectories of the protuberances (13) converging with the further tube (10) at the height of the third aperture (11).
10. Apparatus for heat- and/or material exchange (III), comprising a rotationally-symmetrical heat- and/or material exchanger (II), the cross-section of which has at least 2n sectors which are separated from each other by a membrane, n being an integer ≥ 1, preferably ≥ 2,
    at least one end of the heat- and/or material exchanger (II) being connected in a form fit to a fluid distributor (I) according to one of the claims 1 to 7 via the second aperture thereof, the number of sectors of the heat- and/or material exchanger (II) and of the fluid distributor (I) being identical.
11. Apparatus (III) according to the preceding claim, characterised in that the heat- and/or material exchanger (II) and the at least one fluid distributor (I) are rotatable axially relative to each other, the rotation being implemented preferably by means of a motor.
12. Apparatus (III) according to one of the claims 10 to 11, characterised in that the membrane of the heat- and/or material exchanger (II) is material-impermeable or at least partially material-permeable.
13. Apparatus (III) according to one of the claims 10 to 12, characterised in that at least a part of the sectors of the heat- and/or material exchanger (II) is equipped at least partially on the inside and/or outside with sorption materials.
14. Apparatus (III) according to one of the claims 10 to 13, comprising a core tube or solid axis which is disposed in the centre of the heat- and/or material exchanger (II) in the longitudinal direction, with the proviso that, instead of the circular sectors, circular ring sectors are present, the core tube being able to have openings for the material exchange with at least a part of the circular ring sectors.

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