DE19947803A1 - Reactor with a heat exchanger structure - Google Patents

Abstract

The invention relates to a reactor for the catalytic conversion of a feed stream with a heat exchanger structure in tube bundle construction with at least a first and a second heat transfer chamber in thermal contact therewith, one of which contains a reaction chamber occupied with a conversion catalyst material for converting the feed stream supplied. DOLLAR A According to the invention, heat-conducting corrugated fins coated with the reaction catalyst material are introduced into the reaction space. DOLLAR A use e.g. B. as a hydrogen-generating reforming reactor in mobile applications.

Description

The invention relates to a catalytic reactor implementation of a feed stream with a heat transfer support structure in tube bundle construction with at least one he and a second one that is in thermal contact with it Heat exchanger room, the first one with an order Settling catalyst material occupied reaction space for implementation tion of the feed stream included. Through the Heat exchanger structure can be one of the reaction space at least two fluid-separated, in thermal contact with each other Standing heat transfer rooms are supplied with heat as required or be dissipated by the other heat exchanger space is flowed through by a suitable temperature control medium. On in this way, defined temperature ver Conditions for performing endothermic, exothermic or auto Thermer reactions can be set.

Reak are particularly useful for heterogeneously catalyzed reactions gates required, where as large a contact area as possible as well as a good temperature control between the one to be implemented Feed stream and the reaction catalyst material ge is ensured to the implementation reaction with a large To be able to carry out yield and selectivity. One known The reactor type for this application are fixed bed reactors  gates, the reaction chamber with a catalyst pellet tion is filled. However, these reactors claim a right relatively large construction volume and have a so-called marginal goose due to bypass currents in the bulk tion and between the pellets and the reaction chamber walls. In addition, the thermal conductivity of pellet fillings is reduced equally low, resulting in an inhomogeneous Temperaturpro fil in the reaction space and as a result of this to a low level Yield and selectivity of the reaction can lead. For certain applications, such as B. to carry out what Fuel-producing reforming reactions in mobile applications reactors with high and if necessary in streams direction of variable heat flow density desired to a optimal process control and a sufficiently dynamic operation to ensure the behavior of the reactor.

In addition to introducing the reaction catalyst material as Pellet filling it is known the inner wall of the reaction chamber to be coated with the reaction catalyst material. The Of Application DE 196 53 991 A1 specifically discloses one to carry out endothermic catalytic reactions put reactor of this type, the heat exchanger structure in this reactor from a monolithic arrangement paral all stimulus and reaction channels running towards each other stands. While the inner wall surfaces of the reaction channels with are coated on the reaction catalyst material Heating channels on their inner wall surfaces with a combustion coated catalyst material to a catalytic Let the combustion process run through which the reacti reaction space-forming reaction channels are heated. That through The combustion of hot combustion gas can occur in Ge counter current or direct current for the flow of feed material in the reactors on channels through the heating channels. The ready position of the catalyst material as an inner wall coating avoids the inherent problems of pellet fillings, such as Marginality, low thermal conductivity, inhomogeneous temperature ratur distribution and large construction volume, but that's what  specific reaction area, d. H. the effective catalyst Surface relatively limited because the conversion catalyst material is only present on the inside of the reaction chamber.

The invention is the technical problem of providing development of a reactor of the type mentioned at the outset for a given capacity a relatively small volume and weight as well as a high specific reaction area can have avoidance of borderline effects.

The invention solves this problem by providing it a reactor with the features of claim 1. In this Reactor is a heat-conducting well rip in the reaction space introduced with the structure of the conversion catalyst are coated material. The application of the implementation catalyst sator material z. B. by coating the Wellrippenflä surface with a wash coat or through a microporous layer Surface processing of the corrugated fin surface and subsequent Storage or attachment of the reaction catalyst material in or to the enlarged corrugated fin surface in this way consequences.

Since the corrugated fin surface coated in this way in the reaction space can be significantly larger than the area of the reactors walls bordering the outside, is on these Way for a given build volume a correspondingly higher spe specific reaction area provided than with a reak gate, in which only the reaction space be outside bordering walls with the reaction catalyst material are coated. At the same time in the invention Reactor with a catalyst pellet bed the difficulties such as marginalization and inhomogeneous tempe distribution, avoided. It also creates the ready provide the reaction catalyst material as a coating of corrugated fins introduced into the reaction space Requirements for this, the necessary heat flow density to provide a load dependent and locally defined order to  to ensure the most dynamic operating behavior possible. The reactor design according to the invention is stable against mechanical Loads and insensitive to abrasion and aging of the Reaction catalyst material. The reactor is suitable for Execution of both exothermic and endothermic or autothermal chemical reactions, for which a suitable Temperature control medium as heating or cooling medium through the with the Reaction space in heat contact further heat transfer Carrier can be passed through.

In a further developed according to claim 2 is the Reaction space from the interior of a bundle of several flat tubes formed, in which be with the reaction catalyst material layered corrugated fins are introduced. The flat tube bundle can be flowed through in parallel from a variable number Flat tubes with z. B. rectangular cross section that together form the reaction space.

In a further embodiment of the invention, the flat tubes according to claim 3 each formed by two half-shells be that featured with the cross section widening outwards are made. Through this to the side areas widening cross-sectional shape can the two Rohrschscha len under mechanical tension against one of them increasing, at least on the rib flanks with the conversion tion catalyst material coated corrugated fin and then ver together at the edge to form the flat tube be bound. In this way, the flat tube lies inside securely against the individual sheets of the inserted well rib biased so that good thermal contact between Corrugated fin and flat tube wall is given.

In a further embodiment of the invention is according to claim 4 the heat exchanger structure of a flat tube / fin block in which the several reaction space-forming Flat tubes, in the interior of which with the implementation catalyst Door material coated corrugated ribs are introduced under  Intermediate placement of flat tube-outside, heat-conducting well ribs are spaced apart. Thereby bil the spaces between the flat tubes of the flat tube / Finned blocks a heat exchanger space that matches that of the Flat tube interiors formed reaction space in thermal contact stands and in the also heat-conducting corrugated fins for Ver improvement of the heat transfer capacity are introduced. In further development of this type of reactor are according to claim 5 the flat tubes expanded so much at the ends that the Flat tube ends bridge the flat tube spaces and ge form a firm bond to one another suitable connection structure for feeding the to be implemented Feed stream and removal of the pro formed from it duct current can be assigned.

In a further embodiment of the invention, according to An Say 6 the flat tube / fin block in a heat transfer area inserted housing, and the flat tube outside heat transfer Tragerraum points in the longitudinal direction of its associated Wellrip pen running flow channels. Depending on the course of this Flat tube outside corrugated fins relative to those with the order settlement catalyst material coated corrugated fins in the Flat tubes can guide the temperature control medium as desired can be set, e.g. B. in parallel flow or alternatively in Cross flow for use conducted through the reaction space material flow. Suitable types are on the heat exchanger housing closing structures for supply and discharge of the temperature control medium on the one hand and the feed stream on the other hand hen. In a further embodiment of this type of reactor is according to Claim 7 of the heat flow through which the temperature control medium can flow storage room by appropriate design of its associated Connection structure divided into several sub-rooms Temperature medium can be flowed through in parallel or in series.

In a development of the invention according to claim 8 comprises the reaction space is a stack of crosswise in one selectable crossover angle, one above the other, with the  Reaction catalyst material coated corrugated fins, and the corrugated fin stack thus formed is from a bundle parallel, spaced heat exchanger tubes enforced, the tube interior in this embodiment heat transfer chamber through which the temperature control medium can flow det.

Advantageous embodiments of the invention are in the Drawings are shown and are described below. Here show:

Fig. 1 is a side view of a corrugated fin blank before coating with a Umsetzungskatalysatormateri al,

Fig. 2 is a side view of the corrugated fin of Fig. 1 after coating with the conversion catalyst material,

Fig. 3 is a cross sectional view of the coated corrugated fin of Fig. 2 containing from two tube half-peel to be formed flat tube prior to the tube together menfügen half-shells,

Fig. 4 shows the finished flat tube of FIG. 3 according to piece together the two tube half-shells,

Fig. 5 is a cross-sectional view of a flat tube / rib block formed of flat tubes according to Fig. 4 and the interposed corrugated fins,

Fig. 6 is a side view of FIG. 5 constructed flat tube / fin block,

Fig. 7 is an end view of the flat-tube / fin block of FIG. 6,

Fig. 8 is a schematic, fragmentary side view of a comparison with FIG. 6 modified flat tube / fin block with tube sheet instead of the expanded flat tube ends,

Fig. 9 is a fragmentary sectional view taken along the line IX-IX of Fig. 8,

Fig. 10 is a longitudinal sectional view of a reactor having hills with egg nem housing flat tube / rib block in parallel flow design,

Fig. 11 is a half-sectional view taken along line XI-XI of Fig. 10,

Fig. 12 is a longitudinal sectional view of a reactor with introduced into a housing flat tube / fin block with Z- flow,

Fig. 13 is a longitudinal sectional view of a reactor with introduced into a housing flat tube / fin block with double-Z-flow guide,

Fig. 14 is a longitudinal sectional view of a reactor with introduced into a housing flat tube / fin block with a corresponding terminal by a structure se Riell tripartite Wärmeübertragerraum,

Fig. 15 is a longitudinal sectional view of a reactor with introduced into a housing flat tube / fin block with a three-part parallel by a corresponding terminal structure Wärmeübertragerraum,

Fig. 16 is a schematic cross-sectional view of a reactor with a heat transfer structure introduced into a housing and consisting of a corrugated fin stack and a bundle of heat exchangers penetrating them and

Fig. 17 is a half-sectional view of the reactor taken along line XVII-XVII of Fig. 16.

Fig. 1 shows a corrugated fin blank 1 , as it is used here to form a catalyst-coated corrugated fin. Fig. 2 shows such a ge formed from the blank 1 , provided with a coating 2 from a catalyst catalyst material corrugated fin 3rd To apply the catalyst layer 2 , the surface of the corrugated fin blank 1 can first be seen with a surface-enlarging wash coat or be subjected to a microporous surface treatment. The corrugated fin blank 1 typically consists of a 0.02 mm to 0.3 mm thick metal strip made of aluminum, stainless steel, copper or the like.

To produce a large number of very fine micropores, such a corrugated fin blank can, for. B. anodic oxidation in sulfuric acid or in another electrolyte such as carbonic acid, whereby a metal oxide-containing metal oxide surface layer is formed, see for example the dissertation by D. Scholl, University of Karlsruhe, 1989. The micropores have the shape Sacklö chern and are only in the oxide layer, so they do not continue into the metal, so that at the same time a relatively corrosion-resistant surface is created. The type of pore system with regard to pore density, pore diameter and pore length can be controlled via a number of parameters, such as type of electrolyte, voltage and time, during the anodic oxidation process and can thus be adapted to the desired requirements. Typical dimensions are 10 µm to 300 µm for the pore length and 10 nm to 100 nm for the pore diameter. The micropores formed are then doped with the reaction catalyst material, for example by soaking in a solution with subsequent baking or by a suitable CVD or PVD process. Preference is taken by suitable measures that the outside 3 a of the flat corrugated rib arches, as can be seen in Fig. 2, is not noticeably coated with the catalyst material, for example, by covering the corrugated fin on both sides outside during the coating process with a not removable coating or by scraping off the wash coat after coating.

FIGS. 3 and 4 illustrate the process for preparing a usable in the invention the flat tube 4 with a therein mounted, coated corrugated fin 3 of FIG. 2. These first two corresponding pipe half-shells 4 a, 4 b prefabricated, whose cross-sectional shape in the pre-made to stand from Fig . is visible. 3 As can be seen from this, the pipe half-shells 4 a, 4 b extend from their bent side edges 5 from a slightly V-shaped incline towards their central region 6 . As a result, they attach themselves to each side of the corrugated fin 3 enclosed by them with mechanical pretension against the corrugated fin arches 3 a, after which they are pressed against one another with their bent side edges 5 and firmly connected to one another there with a welding line 7 were. In this way, there is a close, force and heat flow contact between the corrugated fin 3 and the flat tube wall, which is a good thermal contact between the heat-conducting corrugated fin 3 and the tubular wall of the flat tube 4 and thus good heat transfer between the interior's 8 of the flat tube 4th and its outside space guaranteed. The two half-shells 4 a, 4 b are preferably made of stainless steel and can be produced endlessly from a strip material with a thickness of typically between 0.05 mm and 0.4 mm by folding. In order to provide the highest possible heat transfer area per unit volume to achieve a compact reactor design, a relatively fine fin structure for the corrugated fin 3 with typical fin densities between 15 Ri / dm and 150 Ri / dm is selected. The finished flat tube 4 preferably has a width between 10 mm and 50 mm and a height between 1 mm and 6 mm.

Fig. 5 shows a detail of a possible structure of a re actuator using the flat tube 4 of Fig. 4. Specifically, the flat tube / fin block preferably includes a plurality of parallel flat tubes 4 with internal corrugated fin 3 coated with the conversion catalyst material in a one- or two-dimensional arrangement , The flat tubes in a vertical direction H with a spacing with the interposition of second flat tube-outside corrugated fins 9 follow one another. FIG. 6 shows such a flat tube / fin block with ten flat tube layers as an example.

As can further be seen from Fig. 6, the flat tubes 4 extend with their ends 10 over the interposed flat tube-outside corrugated fins 9 and are widened to such an extent that the equilateral ends of two adjacent flat tubes 4 touch each other and so laterally close the space between the flat tubes. The mutually abutting walls of the flat tube ends 10 are connected to one another in a fluid-tight manner, for example by a soldered or welded connection 12 .

Fig. 7 shows the flat tube / fin block of FIG. 6 in an associated end view along an arrow 51 of FIG. 6 for an embodiment comprising in the block depth direction T of two rows 11 a, 11 b side of adjacent flat tubes 4. As can be seen from FIG. 7, there are two flat tubes 4 touching each other in each tube block, whereby they can be fixed to one another along their contacting side walls by a soldered or welded connection 13 , while two flat tubes 4 lying one below the other in a row of flat tubes 11 a, 11 b are connected to one another via their end regions 10 which are fixed to one another by the end-side soldered or welded connections 12 . In this way, the flat tube / fin block forms on its two lateral ends, as can be seen in FIG. 7, a completely flat mouth structure for the medium to be passed through the flat tube spaces 8 , without the need for collecting tube sheets into which the flat tube ends are otherwise to be plugged in.

Specifically, the fluidically parallel Flachroh can trough space 8 constitute a supplied feed stream of the flat-tube / fin block of FIG. 5 to 7 a reaction space of a reactor for catalytic imple mentation, the one placed conversion catalyst material is selected so as the coating of the flat tube inner-side corrugated fins 3 in that it comprises catalyzed the desired reaction. The flat tube gaps, in which the flat tube outside corrugated ribs 9 are introduced, then form a with the Reakti onsraum 8 as a first heat exchanger space in heat con tact, second heat exchanger space, which can be flowed through by a suitable temperature control medium. Depending on the application, this is a heating or cooling medium, depending on whether an exothermic, endothermic or autothermal reaction is to take place in the reaction space 8 . The corrugated fins 9 on the outside of the flat tube are likewise guided in a heat-conducting manner for this purpose and can consist of the same metal material as the corrugated fins 3 on the inside of the flat tube. The temperature control can via lateral column 15, the derliegenden between the gegeneinan flat tube ends 10 on the one hand and the Retired translated ends 9 a of the flat tube outer side corrugated fins 9 forms ge are introduced into the flat tube interspaces who to where it is in parallel-flow, depending on the choice of the feed and Removal in cocurrent or countercurrent flows to the feed stream which is passed through the flat tube interiors 8 .

If the temperature control medium is to be a heating medium, the corrugated fins 9 on the outside of the flat tube, as shown in FIG. 5, can be provided, analogously to the corrugated fins 3 on the inside of the flat tube, with a coating 14 made of a combustion catalyst material, which causes a catalytic combustion of a supplied fuel stream. The coating 14 made of the combustion catalyst material can be applied in the same way to a corrugated fin blank, as was described above for the coating of the corrugated fins 3 on the inside of the flat tube with the reaction catalyst material.

The manufacture of the flat tube / fin block, he can follow that first the individual flat tubes 4 and the inter mediate, flat tube outer corrugated fins 9 are loosely folded into a block and then housed as a braced package in a housing and / or in a common soldering process are soldered together . If the corrugated fin arches are left uncoated, the corrugated fin 9 can be soldered to the flat tubes 4 more easily.

In the flat-tube / fin block of FIG. 5 to 7 extend the flat-tube outer-side corrugated fins 14 parallel to the longitudinal axis of the flat tube inner-side corrugated fins 3 longitudinal axis. If they are created as shown with the corrugated fins 3 aligned with the flat tube inner side corrugated fins 3 against the flat tube outer wall, there is a particularly stable design, which allows the use of very wide flat tubes without sacrificing stability if necessary. In addition, any desired height and depth dimensioning for the flat tube / fin block can be realized by modularly joining any number of flat tubes 4 in a two-dimensional block arrangement. For applications without outside support by corrugated fins on the outside of the flat tube, narrower flat tubes are preferably used to withstand the required pressure loads. As an alternative to the longitudinal ribbing shown, ie. the introduction of the corrugated fins on the outside of the flat tube with the longitudinal direction parallel to the longitudinal direction of the flat tube, a realization of the flat tube / finned block with transverse ribbing is possible, in which the outside of the corrugated fins on the outside of the flat tube is inserted into the flat tube spaces with the longitudinal direction of the flat tube being preferably perpendicular. In this case, the flow channels of the temperature control medium heat transfer space defined by the flat tube-side corrugated fins and the flat tube outer walls run perpendicular to the reaction space flow channels, which are defined in each case by the flat tube-side corrugated fin and the flat tube inner wall, that is to say the temperature control medium is cross-flowed to the feed stream to be converted leads.

In FIGS. 8 and 9 a variant of the flat tube / Rip is shown penblocks of Fig. 5 to 7 fragmentary, when not expanded, the flat tube ends, but fluid-tight manner in a tube plate are inserted. For this purpose, a tube sheet 16 is welded by corresponding weld connections 17 between the ends 10 a of flat tubes 4 of the type shown in FIG. 4, the corrugated fins 3 on the inside of the flat tube ending in front of the height of the tube base and the tube base 16 laterally closing off the flat tube spaces . Via column 15 a between the tube sheet 16 and the opposite ends 9 a of the flat tube outside Wellrip pen 9 , the temperature control medium 18 is supplied, while the supply and discharge of the material 19 passed through the reaction chamber takes place via the front flat tube mouths. In the sectional view of FIG. 9, two flat tube layers, each with three contacting flat tubes 4 each, are shown as a section of the entire flat tube / rib block, a continuous corrugated fin 9 in the form of a longitudinal ribbing being introduced between two flat tube layers. Alternatively, the corrugated fins on the outside of the flat tube can also be introduced in this embodiment as transverse ribbing with a corrugated fin longitudinal axis running perpendicular to the longitudinal axis of the flat tube.

In Figs. 10 to 15, various possible reactor are shown configurations in each of which a flat tube / fin block is accommodated as a heat transfer structure in a housing un, the suitable connection structures for supplying and discharging the reacted feed stream or of the is from recovered product stream in or clear the inside of the flat tube and for the supply and discharge of the tempering medium passed through the likewise finned flat tube spaces.

The reactor shown in FIGS. 10 and 11 has a partially ribbed design with a Z-flow. More precisely, the flat tubes 4 of the flat tube / fin block 21 housed in a housing 20 un extend between two opposite, parallel tube sheets 22 a, 22 b, each of which is associated with an associated housing connection 23 a, 23 b, around the front to feed feed stream 24 to be implemented in the reaction space formed by the flat tube interiors and to take the generated product stream 25 on the opposite side. The flat tube outside corrugated fins 9 in the flat tube interspaces end along two closing lines 26 a, 26 b, the oblique to the tube sheets 22 a, 22 b fen, with a distance to the tube sheets 22 a, 22 b, so that a respective wedge-shaped, non-ribbed Inflow area 27 a and Ab flow area 27 b is formed, each of which a radial Ge housing connection 28 a, 28 b is assigned. In this way, the temperature control medium 29 is guided in a Z-shape through the housing 20 , it flows in the effective heat transfer area of the flat tube / fin block 21 in countercurrent to the material flow to be implemented. Fig. 11 shows in a half cross section of the flat tube / fin block used in Fig. 10 using an example in which the block half shown comprises three rows of six flat tubes 4 arranged one below the other with touch contact, with which there are three continuous corrugated fins on the outside of the flat tube 9 alternate with longitudinal ribbing.

The reactor shown in FIG. 12 corresponds essentially to that of FIGS. 10 and 11, the same reference numerals being used for the sake of simplicity for functionally identical elements and in this respect reference can be made to the above description of FIGS. 10 and 11. In this reactor, in contrast to the reactor of FIGS . 10 and 11, the flat tube-outside ribbing of the flat tube / fin block 21 a, starting from a rib area 30 with a corrugated fin longitudinal axis parallel to the flat tube longitudinal axis, is not at the level of the two oblique lines 26 a, 26 b, but instead continues with each egg miter on the ribbing area 30 abutting ribbing 31 a, 31 b, the front end 32 a, 32 b of the respective radial housing connection 28 a, 28 b is assigned. In this way, the temperature control medium 29 in the two endsei term Berippungsteilbereichen 32 a, 32 b in cross-current and in Berippungsmittelbereich 30 in countercurrent to the performed by the reac tion space conducted, reacted feed stream 24 and product stream 25th

A further variant with regard to the management of the temperature control medium 29 is realized in the reactor of FIG. 13, the same reference numerals being used for functionally identical elements as in the reactor of FIGS. 10 and 11 and referring to the description there who can . In the reactor of Fig. 13, a flat tube / Rip penblock 21 b is used, in which the flat tube outer longitudinal ribbing symmetrical to a longitudinal plane of the housing along an oblique course with respect to the tube sheets 22 a, 22 b, the fin end surface 34 a, 34 b ends, each as a connection structure a circumferential inflow or outflow ring 35 a, 35 b is assigned, into which the associated radial housing connection 28 a, 28 b opens. In this way, there is a double-Z flow through the flat tube / fin block 21 b through the temperature medium 29 in countercurrent to the feed stream 24 or product stream 25 passed through the flat tube interior, to be converted.

In the reactor variant shown in FIG. 14, a flat tube / finned block 37 is accommodated in a housing 36 , the flat tubes in turn extending in a straight line between two opposite tube sheets 37 a, 37 b, to which a respective housing connection 38 a, 38 b for feeding the feedstock stream 24 to be implemented and assigned to the discharge of the product stream 25 obtained. The flat tube outside ribbing of the flat tube / fin block 37 is out as transverse ribbing, ie the flat tube outside corrugated ribs run with their longitudinal axis perpendicular to the flat tube longitudinal axis. Due to a special, assigned connection structure, the tempering medium heat exchanger space containing the cross ribbing of the flat tube / fin block is divided into three serially connected parts 39 a, 39 b, 39 c. The inlet side 40 a of the upstream part 39 a is assigned a ra dialer inlet connection 41 , while on the opposite side of the housing the outlet side 40 b of the upstream part 39 a of the temperature medium heat exchanger space through a first housing-side deflection 42 with the inlet side 43 a of the middle part 39 b is in fluid communication. Via a second housing-side deflection 44 , the outlet side 43 b of the middle part 39 b is connected to the inlet side 45 a of the downstream part 39 c of the temperature control medium heat exchanger space. B at the outlet side 45, a radial outlet port 46 connects.

Thus, in the reactor of FIG. 14, the temperature control medium 29 is conducted in cross flow to the feed stream 24 or the product stream 25 formed therefrom, and after entering through the inlet connection 49 it flows through the upstream part 39 a of the associated, cross-ribbed heat exchanger space, from there into the middle part 39 b is deflected, this flows through and is then deflected into the downstream part 39 c, after the flow of which it is connected to the outlet 46 via the outlet 46 exits the reactor housing.

The fins can be selected differently for the three parts 39 a, 39 b, 39 c of the temperature medium heat exchanger space. So z. B. the inlet-side part 39 a contain corrugated fins with a combustion catalyst coating, while the corrugated fins in the middle part 39 b can only function as support and heat-conducting fins without a coating and the downstream part 39 c can remain entirely without corrugated fins. So that z. B. generate a temperature gradient along the reaction chamber flow path in a simple manner.

Fig. 15 shows a variant of the reactor of Fig. 14, wherein again functionally identical elements are provided with the same reference characters. The reactor of FIG. 15 differs from that of FIG. 14 in that the three parts 39 a, 39 b, 39 c of the temperature control medium heat exchanger space are not connected in series but in parallel. For this purpose, each of the three parts 39 a, 39 b, 39 c each has its own connection configuration with a radial inlet port 47 a, 48 a, 49 a and a ge opposite radial outlet port 47 b, 48 b, 49 b assigned. In each of the three radial inlet ports 47 a, 48 a, 49 a there is a controllable throttle valve 50 , 51 , 52 , with which the flows of tempering medium 29 for each of the three parallel flow parts 39 a, 39 b, 39 c of the corresponding gene Heat exchanger space can be regulated separately. Since very variable temperature distributions can be set in the reaction space formed by the flat tube interiors along its flow path, for example a higher temperature in the inlet-side region of the reaction chamber and a lower temperature in the outlet-side reaction space region.

Also in the reactor of FIG. 15 different ribbings for the three parts 39 are again a, 39 b, 39 c of the Temperierme dium-Wärmeübertragerraums possible to achieve a desired Tempe raturprofil as described above to the reactor of FIG. 14 he explained.

It is understood that the various described above NEN reactor variants instead of the ones shown also the reverse Flow directions for the temperature control medium and to be converted feed stream can be selected. Furthermore  are the reactors also with reversed roles from Tempe Medium and feedstock to be used, d. H. in In this case, the corrugated fins of the flat tube outside Flat tube / finned blocks with the conversion catalyst material coated, while the corrugated fins in the flat tubes unbe stay stratified or z. B. with a combustion catalytic converter door material are coated. The reaction space is in the sem case formed by the pipe gaps, while the Flat tube interiors the tempering medium heat exchanger room form.

FIGS. 16 and 17 show a further type of reactor according to the invention, in which a stacked with heat exchanger tubes 53 by modifying the stack of cross-wise at an intersection angle of 90 °, with a Umsetzungskatalysa door material coated corrugated fins as a roughly square in cross-section heat exchanger structure 54 ULTRASONIC in a cylindricity housing 55 is introduced. The four inter mediate the cube-shaped or cuboidal heat exchanger structure 54 and the cylindrical housing 55 remaining sector spaces on the one hand two opposite connection spaces 56 a, 56 b for the feed stream to be converted, which flows in the flow channels formed by the alternating crosswise lying corrugated fins are, and on the other hand two ge opposite connection spaces 57 a, 57 b for a tempering medium passed through the heat exchanger round tubes 53 .

To form the heat exchanger structure 54 , depending on the loading, corrugated fins 58 a with a lower fin density or woof fins 58 b with a higher fin density can be used, as schematically indicated in FIG. 16 as an insert. If necessary, the corrugated fin stack can also be constructed from corrugated fin of different fin density. The round tubes 53 are inserted through circular openings, which are provided in the corrugated fins, as a two-dimensional bundle of spaced tubes, as can be seen in FIG. 17, and then fixed with mechanical or hydraulic expansion with the corrugated fin stack. At the end, the heat exchanger tubes 53 are each inserted into a tube plate 59 a, 59 b, the tube plates 59 a, 59 b sealing off the reaction space formed by the corrugated fin channels 60 between the heat exchanger tubes 53 against the two temperature medium connection spaces 57 a, 57 b.

In the reactor constructed in this way, the temperature control medium passed through the heat exchanger tubes 53 flows in cross flow to the material flow through the stack of crosswise superimposed th, with the reaction catalyst material coated corrugated fins, on which the desired chemical reaction reaction takes place within the heat exchanger structure 54 . The resulting or required conversion heat is dissipated via the round tubes 53 to the tempering medium or supplied by the latter. To achieve a good heat transfer, the round tubes 53 have relatively small diameters in the range between 1 mm and 5 mm. In addition, the round tubes 53 are arranged in a relatively small transverse and longitudinal division of 2 mm to 10 mm distance. The corrugated fins in turn typically have a thickness of 0.02 mm to 0.3 mm and a fin density of 50 Ri / dm to 150 Ri / dm.

Using the exemplary embodiments described in detail above it is clear that the reactor of the invention with relative small construction volume is feasible and a high spec cal reaction surface with an orderly reaction catalyst door system that has no marginal effects and kei ne bypass effects shows, so that for the to be implemented Diffusion paths and dwellings remain constant allow times to be achieved in the reaction space. This has a very good selectivity and yield of the reaction, a homogeneous Temperature distribution and if necessary a good and locally de Finished heat input into the system. The reak tor has a good dynamic operating behavior and a high mechanical stability. The conversion catalyst material  al is abrasion-free in the reaction space. If for fixation only welding and no solder connections are used any entry may be undesirable, catalytically active prevents thinner materials, as they can occur in solders nen. The high modular variability in the construction of the reactor enables its implementation in a wide variety of currents Guides such as countercurrent, cocurrent and crossflow and combi nations, as well as for the most diverse implementation performance and in different reactor stages with ver different reaction temperatures. The reak according to the invention tor is used for any catalytic chemical processes reversible, especially for carrying hydrogen gender reforms in stationary and mobile applications phrases such as B. for steam reforming of methanol, and as an oxidation stage downstream of a reformer for removing carbon monoxide from the raw gas.

Claims (8)

1. Reactor for the catalytic conversion of a feed stream with

• - A heat exchanger structure in tube bundle construction with at least a first and a second heat exchanger chamber in thermal contact therewith, the first of which contains a reaction chamber occupied with a reaction catalyst material for converting the feed stream supplied, characterized in that
• - In the reaction chamber ( 8 ), a heat-conducting, with the implementation catalyst material coated corrugated fin structure ( 3 ) is introduced.

2. Reactor according to claim 1, further characterized in that the reaction space from the interior ( 8 ) of a bundle of several flat tubes ( 4 ) is formed, in which with the implementation of catalyst material corrugated fins ( 3 ) are introduced. 3. Reactor according to claim 2, further characterized in that the flat tubes ( 4 ) are each formed by two tube half-shells ( 4 a, 4 b), which are prefabricated with an outwardly widening cross section and under mechanical prestress against an accommodated, at least the corrugated fin ( 3 ) coated with the reaction catalyst material are connected to one another at the edges. 4. Reactor according to claim 2 or 3, further characterized in that the heat exchanger structure is formed by a flat tube / fin block, in which the plurality of reaction space-forming flat tubes ( 4 ) with the interposition of flat tube-side, heat-conducting corrugated fins ( 9 ) are arranged. 5. Reactor according to claim 4, further characterized in that the flat tubes ( 4 ) are widened at the ends, the ends ( 10 ) of adjacent flat tubes lying against one another and being firmly connected to one another. 6. Reactor according to claim 4 or 5, further characterized thereby records that the flat tube / fin block in a housing is brought and the flat tube outside heat exchanger space in the longitudinal direction of its associated corrugated ribs includes flow channels, the housing respective Connection structures for the supply and discharge of a flat Temperature flowing through the pipe outside the heat exchanger space riermediums and that passed through the reaction chamber Has feed stream. 7. Reactor according to claim 6, further characterized in that the flat tube outside heat exchanger space is divided by ent speaking design of the tempering medium connection structure in several, parallel or serial of the tempering medium by flowable subspaces ( 39 a, 39 b, 39 c). 8. Reactor according to claim 1, further characterized in that the reaction space comprises a stack of crosswise overlying one, coated with the reaction catalyst material corrugated fins ( 58 a, 58 b) and the corrugated fin stack of a bundle of parallel, spaced-apart heat transfer tubes ( 53 ) is penetrated, the tube interior forms the second heat exchanger space for passing a temperature medium.