DE10031347A1 - Cylindrical reactor for hydrocarbon oxidation has heat exchange plates radially aligned around central inner space and having inlets and outlets for the heat exchange agent - Google Patents

Abstract

Cylindrical reactor has heat exchange plates, along the longitudinal direction of the reactor, with inlets and outlets for the heat exchange agent and which are radially aligned around a central inner space.

Description

The invention relates to a cylindrical reactor spaced apart from one another Heat exchanger plates arranged in the longitudinal direction of the reactor and also a use of the reactor.

Generic reactors are known in chemical reaction technology, especially for the implementation of reactions with high heat, whereby it can be both exothermic and endothermic reactions. The de- C-197 54 185 describes a reactor with a cylindrical reactor vessel, wherein in the reactor vessel designed as a thermal plate heat exchanger plates in vertical orientation on the sieve bottom of the reactor next to each other, with a predetermined Are spaced from each other. The plates are made of a cooling medium flows through the in the area of the container ceiling using suitable facilities Heat exchanger plates supplied and in the area of the tank bottom via suitable Equipment is removed from the heat exchanger plates. Between Heat exchanger plates become a gaseous one in counterflow to the cooling medium Reaction medium, with feed in the area of the tank bottom and discharge in the Area of the tank ceiling. The heat exchangers designed as thermal sheets plates enable the realization of a compact heat exchanger with a large one Heating surface density without flow dead zones; however, they have the particular disadvantage that that they have to be adapted to the inside wall of the container, it being impossible to Thermosheets of a single size or a small number from each other different sizes, for example of 2 or 3 sizes.  

In contrast, it is an object of the invention to provide a reactor with heat exchanger plates To make available, which is easy to manufacture in terms of construction.

In one embodiment, the object of the invention is to provide a reactor places that is particularly advantageous in terms of flow technology, and that is flexible adaptation to the temperature profile of different chemical reactions.

The solution is based on a cylindrical reactor spaced apart in Longitudinal direction of the reactor arranged heat exchanger plates by a Heat exchangers are flowed through, with supply and discharge devices for the Heat exchange medium to the heat exchanger plates and with spaces between the heat exchanger plates through which a reaction medium flows.

The solution is then characterized in that the heat exchanger plates under Release of a central interior are arranged radially in the reactor.

In a special embodiment variant, the solution is characterized in that the Heat exchanger plates leaving a peripheral channel free from the reactor walls are spaced apart and that the reaction medium radially through the Gaps between the heat exchanger plates is performed.

It was therefore a simple and cost-effective solution for found a reactor with heat exchanger plates.

Cylindrical reactors usually have covers on both reactor ends are often dome-shaped, on, with feed and discharge devices for Reaction mixture and / or the heat exchange medium. Cylindrical reactors can basically be aligned in any position, with a vertical orientation in the Is generally preferred.

Heat exchanger plates are predominantly sheet-like structures, one with inlet and Leakage lines provided interior with a small thickness in relation to the area  exhibit. They are usually made from sheet metal, often from sheet steel. Each depending on the application, in particular the properties of the reaction medium and the However, heat exchangers can use special, especially corrosion-resistant, materials are used. The supply and discharge devices for the heat exchange medium are usually arranged at opposite ends of the heat exchange plates; at the radial alignment of the heat exchanger plates according to the invention in one cylindrical reactor, it is particularly advantageous to use the heat exchange medium Heat exchanger plates are fed in or out via ring lines. When standing vertically Alignment of the cylindrical reactor, it is particularly preferred that Heat exchange medium via the lower ring line to the heat exchanger plates to drain the upper ring line from the heat exchanger plates.

According to the invention, the heat exchanger plates are released with a central one Radial interior in the reactor, d. H. arranged along the reactor radii.

The central interior, which in a suitable manner with supply and discharge devices for the Reaction medium to or from the spaces between the heat exchanger plates is basically any geometric shape, for example the shape of a Polygons, especially the shape of a triangle, a square, one preferred regular hexagon or a preferred regular octagon as well as one have a substantially circular shape.

The heat exchanger plates preferably extend in the longitudinal direction of the reactor essentially over the entire length of the cylindrical reactor with the exception of Reactor ends.

In a preferred embodiment, the heat exchanger plates are released a peripheral channel spaced from the reactor walls, the Reaction medium radially through the spaces between the heat exchanger plates to be led. The peripheral channel is preferably ring-shaped. It serves as a collection and / or Distribution chamber for the reaction medium. The peripheral channel can be through a cylindrical-shaped sieve from the spaces between the  Heat exchanger plates must be separate; analogously, a corresponding sieve Separate the spaces between the heat exchanger plates from the central interior. This configuration can be particularly suitable if a reaction occurs below Use of a catalyst is carried out in the spaces between the heat exchanger plates is introduced and its discharge with the Reaction medium can be prevented by appropriate selection of the mesh size should.

The reaction medium can be guided radially and / or centripetal, in the event that a single sense of direction of the radial current supply is provided is, the centrifugal guidance of the reaction medium is particularly advantageous.

The radial flow of the reaction medium between the radially arranged Heat exchanger plates have the advantage of a low pressure drop. With reactions that the pressure ratios in the case of centrifugal guidance, due to the increasing distances between the heat exchanger plates, very cheap.

With radial flow of the reaction medium through the spaces between the radially arranged heat exchanger plates changes the available ones Heat exchange surface continuously. So the exchange area at centrifugal Leading the reaction medium continuously to the outside, resulting in reactions with changeable heat profile, especially with decreasing exotherm over the Reaction course, an optimization of the heat exchange is guaranteed.

The radial expansion of all heat exchanger plates is preferably the same; an adjustment the heat exchanger plates on the inside wall of the reactor is therefore not on the contrary, panels of a single type can be used.

The radial expansion of the heat exchanger plates is preferably in the range from 0.1 to 1 of the reactor radius, particularly preferably in the range from 0.4 to 0.9 of the reactor radius.  

The heat exchanger plates are essentially straight. this means not that they are completely flat structures, on the contrary, they can in particular be regularly bent, folded, kinked or curled. The heat exchanger plates are produced by known methods, in particular pressed or vacuum-drawn.

Preferably, periodically profiled structural elements in the heat exchanger plates, in particular corrugated plates. Such structural elements are as Mixing elements in static mixers are known, and for example in DE 196 23 051.9 described, in the present case they are used in particular to optimize the heat exchange. To adapt to the required heat profile, it is possible to have a higher board density in the to provide the outer reactor area relative to the inner reactor area, in particular additional plates in the outer reactor area with less radial expansion compared to the other heat exchanger plates, preferably with a radial expansion in the range from 0.1 to 0.7, particularly preferably 0.2 to 0.5, of the radial extent of the other heat exchanger plates. The additional plates can be the one below the other have the same dimensions, but it is also possible to have two or more To use construction types of additional panels, whereby the construction types are mutually differ by their radial extent and / or their length.

The additional heat exchanger plates are preferably symmetrical between the others Heat exchanger plates arranged. They allow an improved adaptation to that Temperature profile of the respective chemical reaction.

In a preferred embodiment, it is possible to use the heat exchanger plates wedge-shaped, in particular double wedge-shaped. After that they become the Sheets forming heat exchanger plates with a pointed and an opposite, somewhat wider degree. Due to the radial arrangement of the same in the reactor it is possible to have largely uniform flow paths for the reaction mixture guarantee. It is equally possible to use all heat exchanger plates with the same radial expansion or heat exchanger plates with different radial To provide expansion. The heat exchanger plates can particularly preferably be double be wedge-shaped.  

In a special embodiment, it is possible to at least one ring channel outer circumference of the reactor room equipped with the heat exchanger plates provide, with radially arranged outer heat exchanger plates.

An advantageous reactor variant has a continuous catalyst bed, with Filling dome at the top of the reactor and emptying device at the bottom of the Reactor. This creates a catalyst buffer that is always complete Catalyst filling guaranteed. Especially for performing reactions under adiabatic conditions, it is possible to modify the reactor such that in the Catalyst bed no heat exchanger plates are arranged.

The outer heat exchanger plates are particularly preferred over the others Heat exchanger plates arranged offset. The offset arrangement is particularly at strongly exothermic reactions favorable; between two Heat exchanger plates protruding end of the staggered heat exchanger plates the particularly high temperatures in the area between the heat exchanger plates intercepted. For this, it is particularly advantageous if the staggered Overlap heat exchanger plates at least partially.

According to a preferred embodiment, a reactor is provided which is constructed from two or more reactor sections, in particular removable, wherein the flow of the reaction medium between two successive ones Reactor shots are directed by suitable baffles. The single ones Reactor sections are constructed in the manner described above, i. H. especially with radially arranged heat exchanger plates and with feed and discharge devices for the Heat exchangers and the reaction medium. The individual reactor shots are by means of Flanges can be assembled as required. The flow of the reaction medium between two successive reactor shots is made by suitable baffles guaranteed that have a deflection and / or separation function. By appropriate choice of Number of baffles can be a multiple deflection of the reaction medium can be achieved.  

It is possible to have intermediate feed points on one or more of the reactor sections for the reaction medium, in particular via the peripheral channel. Thereby can advantageously optimize the conduct of the reaction and the temperature profile become.

It is possible to have a reactor with multiple reactor sections with a single one To design the heat exchange circuit. However, in a preferred manner two or more separate heat exchange circuits through the Heat exchanger plates may be provided. This can be an improved adjustment to different heat exchange requirements with progressive chemical reaction be achieved; it can be used, for example, in reactions that have previously been used two or more catalyst systems with different catalytic activity were carried out on a uniform catalyst system.

In a special embodiment, the central part of the reactor is in the upper area Inside a jet nozzle arranged and in the central interior a concentric Guide tube that extends essentially over the entire length of the reactor with the exception of the Extends reactor ends and a cross-sectional area in the range of one tenth to Has half the cross-sectional area of the reactor. Preferably in the reactor area a baffle plate may be arranged below the lower end of the concentric guide tube.

Such an embodiment is particularly suitable for carrying out reactions in Two- or three-phase systems are advantageous for intensive phase mixing is particularly important, preferably for the liquid phase oxidation of o-xylene. Through the constructive design, an internal loop flow is ensured, the predominant part of the reaction mixture, corresponding to two to thirty times, in particular five to ten times the volume flow of the externally pumped Reaction mixture the concentric guide tube from top to bottom and the annulus flows between the guide tube and the inner wall of the reactor from bottom to top. Such Reactors are, for example, in the unpublished German patent application DE 198 54 637.8. Due to the radial arrangement of heat exchanger plates in the  The reactor space between the central interior and the inside wall of the reactor mentioned reactors improved, especially with regard to Heat exchange properties.

According to a further preferred embodiment, the reactor can be used as Fluidized bed reactor to be designed. Due to the arrangement of radial heat exchanger plates in the fluidized bed can in particular Heat transfer can be improved.

The reactor according to the invention is particularly suitable for reaction media in the gas phase of Advantage. The fluidic advantages and the lower pressure loss come with it especially to wear.

The reactor according to the invention is particularly suitable for carrying out Gas phase reactions in the presence of a catalyst, especially a moving one Catalyst. Moving catalysts have the particular advantage over Fixed bed catalysts can be formed more finely divided, which makes the catalytic effective surface is larger.

However, it is also possible, in addition or as an alternative to a moving catalyst to apply the same as a coating on the heat exchanger plates of the reactor. The Coating of the heat exchanger plates can take place before or after their installation in the reactor respectively. If the heat exchanger plates are already installed, a suspension of the Catalyst pumped through the reactor. Through a particularly electrolytic The catalyst is deposited on the heat exchanger plates and then calcined, for example by a hot heat exchanger in the Heat exchanger plates or by means of a mobile roller gas station. Before installation in the The reactor can be coated by dipping or spraying. By the The use of coated heat exchanger plates ensures optimal dissipation of the Heat of reaction guaranteed.  

The reactor can be used particularly advantageously to carry out exothermic reactions, in particular of oxidation reactions, particularly preferably for the oxidation of Hydrocarbons, especially alkanes and alkenes are used, and for Production of acrolein, acrylic acid, ethylene oxide, propylene oxide, maleic anhydride, Phthalic anhydride or glyoxal.

Endothermic reactions can also advantageously be carried out, in particular Dehydrogenation, preferably propane dehydrogenation, styrene synthesis from ethylbenzene, the production of hydrocyanic acid from formamide and the production of vinyl formamide.

The invention is described below with the aid of exemplary embodiments and a drawing explained in more detail. The individual shows:

Fig. 1 shows a cross section through a first embodiment of a reactor according to the invention,

Fig. 1a shows a longitudinal section through a heat exchanger plate according to Fig. 1,

Fig. 2 shows a cross section through a preferred embodiment with additional heat exchanger plates,

Fig. 3 shows a cross section through a further preferred embodiment with two types of construction of additional heat exchanger plates,

Fig. 4a shows a longitudinal section through a preferred embodiment with peripheral channel and radial guidance of the reaction medium.

FIG. 4b is a cross-section through the embodiment shown in longitudinal section in Fig. 4a,

FIG. 5a is a further preferred embodiment in longitudinal section with a plurality of reactor sections,

Fig. 5b shows a cross section in the range AA through the reactor shown in longitudinal section in Fig. 5a,

Fig. 5c is a cross-section in the region by the BB in Fig. Reactor shown in longitudinal section 5a,

FIG. 6a shows a further preferred embodiment, in longitudinal section, with a plurality of heat-exchange medium circuits,

Fig. 6b shows a cross section in the range AA through the reactor shown in longitudinal section in Fig. 6a,

Fig. 7a, a further preferred embodiment, in longitudinal section, with intermediate feed, as well as the catalyst bed,

Fig. 7b shows a cross section in the range AA through the reactor shown in longitudinal section in Fig. 7a,

Fig. 7c shows a cross-section in the region by the BB in Fig. Reactor shown in longitudinal section 7a,

Fig. 8a is a further preferred embodiment, in longitudinal section, with intermediate feed and catalyst bed, wherein no heat exchanger plates are arranged in the catalyst bed,

FIG. 8b a cross-section in the range AA through the reactor shown in longitudinal section in Fig. 8a,

Fig. 8c is a cross-section in the region by the BB in Fig. Reactor shown in longitudinal section 8a,

Fig. 9 shows another preferred embodiment with internal loop flow of the reaction medium and

Fig. 10 shows a further preferred embodiment as a fluidized bed reactor,

FIG. 11a, a further preferred embodiment, in longitudinal section as a bubble column reactor,

Fig. 11b is a cross-sectional view of the illustrated in Fig. 11a, in longitudinal section reactor,

Fig. 12 shows another preferred embodiment in longitudinal section, as a crystallizer and

Fig. 13-15 cross sections through further preferred embodiments with wedge-shaped heat exchanger plates.

In the figures, the same reference numerals and the same or corresponding Characteristics.

The cross section shown in FIG. 1 of a preferred reactor 1 according to the invention with the reactor radius R shows radially arranged heat exchanger plates 2 with radial extension r, which are distributed symmetrically over the reactor cross section and leave a central interior space 7 free.

Fig. 1a shows a longitudinal section AA through a heat exchanger plate 2 with supply line 5 and discharge line 6 for the heat exchange medium.

FIG. 2 shows, in addition to the heat exchanger plates 2 , symmetrically arranged additional heat exchanger plates 3 with a smaller radial expansion than the heat exchanger plates 2 .

Fig. 3 shows two different types of construction of additional heat exchanger plates 3, 4 each having a smaller radial extent relative to the heat exchanger plates 2 and symmetrical arrangement over the cross section of the reactor.

Fig. 4a shows a longitudinal section through a preferred embodiment with peripheral channel 8. If required, retaining sieves 13 can be provided.

FIG. 4b shows a cross section through the reactor shown in longitudinal section in FIG. 4a.

In Fig. 5a a built-up of several connected via flanges reactor sections reactor in longitudinal section is shown schematically. The reaction mixture flows radially, alternately centrifugally or centripetal through the reactor, suitable deflection disks 9 being arranged between the reactor sections. The possibility of intermediate feeding of the reaction mixture is indicated by arrows at the side.

In Fig. 5b is a cross-section through the in Fig. 5a reactor shown in longitudinal section in the range AA and in FIG. 5c in the area BB.

The reactor shown schematically in longitudinal section in FIG. 6a has two separate heat exchange medium circuits, the feed devices 5 and the discharge devices 6 advantageously being designed as ring channels.

The cross-sectional view in FIG. 6b (section AA) shows a preferred embodiment with heat exchanger plates 2 , 3 , 4 of different radial dimensions.

A reactor with a continuous catalyst bed 17 is shown schematically in longitudinal section in FIG. 7a. The catalyst is introduced via a filling dome 18 , in particular shaken in by means of a vibrator. Due to the introduction via a filling dome, a catalyst buffer is always present, which always ensures a continuous filling with catalyst. The catalyst bed 17 is drawn off from the reactor 1 if necessary via suitable, in particular conical, emptying devices 19 , preferably with holding grids on the catalyst outlet. It is possible to provide one or more in particular annular intermediate feeds 20 for the reaction mixture on the circumference of the reactor. The reactor is preferably designed in such a way that the entire internals, in particular the heat exchanger plates 2 , 3 , 4 , 15, are designed as a plug-in module and can be pulled out at any time with a suitable device, in particular a crane, and are therefore accessible.

FIGS. 7b and 7c show cross sections in the region AA and BB through the in Fig. Reactor shown in longitudinal section 7a. The flow of the reaction mixture is shown by arrows in FIG. 7b from the inside to the outside and in FIG. 7c from the outside to the inside.

In Fig. 8a shows a further preferred embodiment is shown of a reactor according to the invention schematically in longitudinal section, with continuous catalyst bed 17 and with intermediate feed points 20 for the reaction mixture. In contrast to the embodiment shown in FIGS. 7a to 7c, no heat exchanger plates are provided in the catalyst bed. Such an embodiment is particularly advantageous in an adiabatic reaction, for example in the styrene process. In addition to the heat exchanger plates 16 arranged in the ring channel 15 , it is possible to arrange heat exchanger plates 2 in the central interior 7 , in particular in the deflection areas for the reaction mixture, as shown in the figure by the lines with the arrow, leaving a central interior area for guiding the Reaction mixture. It can be clearly seen from the cross-sectional representations in FIGS. 8b and 8c that no heat exchanger plates are arranged in the region of the catalyst bed 17 . The inner heat exchanger plates 2 are provided only when needed.

In Fig. 9, a reactor with internal loop flow of the reaction medium is shown schematically in longitudinal section. The reaction medium is introduced via a nozzle 10 , which can be immersed in the concentric guide tube 11 or can also end above it, and is conducted in an internal loop flow in the space between the concentric inner tube and the inner wall of the reactor. The formation of the loop flow is particularly supported by a baffle plate 12 arranged in the region of the reactor floor.

Fig. 10 shows a longitudinal section through a schematically illustrated fluidized bed reactor. A distributor plate 14 is arranged in the region of the tank bottom, on which a fluidized bed is formed when the reaction gas is supplied via the lower end of the reactor. Heat exchanger plates 2 are arranged radially in the fluidized bed.

FIG. 11a shows schematically a longitudinal section through an opening formed as a bubble column reactor with a particular embodiment of the distributor 21 in the lower region of the reactor 1, the manifold as a porous medium, in particular frit or is for example designed as a perforated bottom. Plug-in pipes with holes in the pipe walls can also take over the function of the distributor. Arrows indicate the supply of gas in the lower central region of the reactor 1 and the discharge in the upper central region and the supply of liquid in the lower region of the reactor 1 , above the distributor 21 and the discharge in the upper reactor region, on the periphery. The cross-sectional view in FIG. 11b (section AA) shows an example of radially arranged heat exchanger plates 2 , 3 with different radial dimensions.

A further special embodiment, as a crystallizer, is shown in longitudinal section in FIG . The mixture to be crystallized is introduced via a feed 23 into the inner region of the concentric guide tube 11 , where a stirrer 22 is arranged. As shown in the figure, the stirrer shaft can come from above, but it is also fundamentally possible to arrange the stirrer shaft in the reactor from below. A coarse grain discharge 24 is provided below the radially arranged heat exchanger plates 2 , and a fine grain discharge 25 is provided on the periphery of the reactor 1 .

In Figs. 13 to 15 are cross-sections through particular embodiments of Inventive according reactors designed wedge-shaped heat exchanger plates. As already stated above, heat exchanger plates are usually made from sheet metal. These do not have to be arranged strictly parallel; on the contrary, a wedge-shaped design with a pointed end and an opposite, somewhat wider end is also possible. Heat exchanger plates designed in this way can be accommodated particularly advantageously in a radial arrangement in the reactor. The formation of largely uniform flow paths for the reaction mixture between the heat exchanger plates is particularly advantageous. In addition, the production of such wedge-shaped heat exchanger plates is technically simple and inexpensive.

As shown in Fig. 13, all of the wedge-shaped heat exchanger plates 2 can be formed uniformly, but it is also possible, as shown in Fig. 14, in addition to the heat exchanger plates 2 with the greatest radial expansion, additional heat exchanger plates 3 with less radial expansion to provide.

In Fig. 15 particularly formed wedge-shaped heat exchanger plates 26 are shown that are designed double-wedge-shaped and enable a particularly advantageous guidance of the reactant mixture.

Claims (20)

1. Cylindrical reactor ( 1 ) with spaced apart, in the longitudinal direction of the reactor ( 1 ), arranged heat exchanger plates ( 2 , 3 , 4 ), through which a heat exchange medium flows, with feed and discharge devices ( 5 , 6 ) for the heat exchange medium the heat exchanger plates ( 2 , 3 , 4 ) and with spaces between the heat exchanger plates ( 2 , 3 , 4 ) through which a reaction medium flows, characterized in that the heat exchanger plates ( 2 , 3 , 4 ) leaving a central interior space ( 7 ) are arranged radially in the reactor ( 1 ). 2. Reactor ( 1 ) according to claim 1, characterized in that the heat exchanger plates extend substantially over the entire length of the cylindrical reactor ( 1 ) with the exception of the reactor ends. 3. Reactor ( 1 ) according to claim 1 or 2, characterized in that the heat exchanger plates ( 2 , 3 , 4 ) are arranged at a distance from the reactor walls, leaving a peripheral channel ( 8 ) and that the reaction medium radially through the spaces between the heat exchanger plates ( 2 , 3 , 4 ) is performed. 4. Reactor ( 1 ) according to one of claims 1 to 3, characterized in that the radial extension (r) of all heat exchanger plates ( 2 , 3 , 4 ) is the same and preferably 0.1 to 1 of the reactor radius (R), particularly preferably 0.4 to 0.9 of the reactor radius (R). 5. Reactor ( 1 ) according to one of claims 1 to 4, characterized in that the heat exchanger plates ( 2 , 3 , 4 ) are substantially straight. 6. Reactor ( 1 ) according to one of claims 1 to 5, characterized in that periodically profiled structural elements, in particular corrugated tarpaulins, are arranged in the heat exchanger plates ( 2 , 3 , 4 ). 7. Reactor ( 1 ) according to one of claims 1 to 5, characterized by a higher density of heat exchanger plates ( 2 , 3 , 4 ) in the outer reactor area compared to the inner reactor area, in particular by additional heat exchanger plates ( 3 , 4 ) in the outer reactor area with less radial expansion (r) compared to the other heat exchanger plates ( 2 ), preferably with a radial expansion in the range from 0.1 to 0.7, particularly preferably 0.2 to 0.5, of the radial expansion of the other heat exchanger plates ( 2 ). 8. Reactor ( 1 ) according to claim 7, characterized by two or more types of additional plates ( 3 , 4 ) wherein the types differ from each other by their radial extent. 9. Reactor ( 1 ) according to one of claims 1 to 8, characterized by a wedge-shaped, in particular double wedge-shaped design of the heat exchanger plates ( 2 , 3 , 4 ). 10. Reactor ( 1 ) according to one of claims 1 to 9, characterized by at least one ring channel ( 15 ) on the outer circumference of the reactor chamber equipped with the heat exchanger plates ( 2 , 3 , 4 ), with radially arranged outer heat exchanger plates ( 15 ). 11. Reactor ( 1 ) according to claim 10, characterized in that the outer heat exchanger plates ( 15 ) with respect to the heat exchanger plates ( 2 , 3 , 4 ) are arranged offset. 12. Reactor ( 1 ) according to one of claims 1 to 11, characterized by a continuous catalyst bed ( 17 ) with filling dome ( 18 ) in the upper region of the reactor ( 1 ) and emptying device ( 19 ) in the lower region of the reactor ( 1 ). 13. Reactor ( 1 ) according to claim 12, characterized in that in the region of the catalyst bed ( 17 ) no heat exchanger plates ( 2 , 3 , 4 ) are arranged. 14. Reactor ( 1 ) according to one of claims 1 to 11, characterized in that it is constructed from two or more in particular removable reactor sections, and that the flow of the reaction medium between two successive reactor sections is directed by suitable baffles ( 9 ). 15. Reactor ( 1 ) according to claim 14, characterized by two or more separate heat exchange medium circuits through the heat exchanger plates ( 2 , 3 , 4 ). 16. Reactor ( 1 ) according to one of claims 1 to 9, characterized in that a nozzle ( 10 ) and a concentric guide tube ( 11 ) is arranged in the central interior ( 7 ), which extends essentially over the entire length of the reactor ( 1 ) extends with the exception of the reactor ends and has a cross-sectional area in the range from one tenth to half of the cross-sectional area of the reactor ( 1 ). 17. Reactor ( 1 ) according to claim 16, characterized in that a baffle plate ( 12 ) is arranged in the reactor area below the lower end of the concentric guide tube ( 11 ). 18. Reactor ( 1 ) according to one of claims 1 to 9, characterized in that it is a fluidized bed reactor. 19. Use of the reactor ( 1 ) according to one of claims 1 to 15 or 18 for carrying out gas phase reactions in the presence of a catalyst, in particular a moving catalyst. 20. Use of the reactor ( 1 ) according to any one of claims 1 to 18 for carrying out exothermic reactions, in particular oxidation reactions, particularly preferably for the oxidation of hydrocarbons, in particular alkanes or alkenes, and for the production of acrolein, acrylic acid, ethylene oxide, propylene oxide, maleic anhydride , Phthalic anhydride or glyoxal.