JP2001038195A - Reactor provided with heat-exchanger plate - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide the reactor having a heat exchanger plate, especially flow-technically preferable, freely adaptable to the temp. profile of different chemical reactions and capable of being easily produced in terms of structural technique. SOLUTION: This reacter 1 is provided with the heat-exchanger plates 2 through which a heat-transfer agent flows and arranged in the longitudinal direction of the reactor 1 away from one another, the feeder and discharge 5 and 6 for the heat-exchange agent with respect to the heat-exchanger plates 2 and an intermediate space between the heat-exchanger plates 2 through which a reaction medium flows. In this case, heat-exchanger plates 2 are radically arranged in the reactor 2 while securing the place for an internal space in the center.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

FIELD OF THE INVENTION The present invention relates to a cylindrical reactor with heat exchanger plates which are arranged at a distance from one another in the longitudinal direction of the reactor and to the use of this reactor.

[0002]

BACKGROUND OF THE INVENTION Reactors described in the generic term are known in the chemical reaction art, in particular for carrying out reactions having a high actual calorific value, in which exothermic and endothermic reactions are likewise performed. Is important. German Patent 1975
No. 4185 describes a reactor with a cylindrical reaction vessel, in which a heat exchange plate configured as a hot plate is perpendicular to the sieve bottom of the reactor. They are aligned with each other and arranged in parallel at a predetermined distance. Coolant flows through the heat exchange plate, which is supplied to the heat exchange plate via appropriate devices in the area of the lid of the container and through appropriate devices in the area of the bottom of the container. And discharged from the heat exchange plate. A gaseous reaction medium is introduced between the heat exchange plates in countercurrent to the coolant and is supplied in the region of the bottom of the container and discharged in the region of the lid of the container. A heat exchanger plate constructed as a heat thin plate makes it possible to realize a compact heat exchanger with a high heating areal density, but has the disadvantage that it must be adapted in particular to the inner wall of the vessel. In this case, however, it is not possible to use heat strips of only one structural dimension or a small number of different structural dimensions, for example two or three structural sheets.

[0003]

The object of the present invention, on the other hand, is that it can be easily manufactured structurally.
It is to provide a reactor equipped with a heat exchange plate.

In one configuration, the object of the present invention is to provide a reactor which is particularly favorable in terms of flow technology and which allows a flexible adaptation to the temperature profile of different chemical reactions.

[0005]

This solution consists of a heat exchange plate, through which the heat exchange agent flows, arranged at a distance from one another in the longitudinal direction of the reactor, a supply device for the heat exchange agent to the heat exchange plate and Starting from a cylindrical reactor with a discharge device and an intermediate space between the heat exchange plates through which the reaction medium flows.

Furthermore, this solution is characterized by the fact that the heat exchange plates are arranged radially in the reactor, while ensuring the location of a central internal space.

[0007] In one particular implementation variant, the solution is that the heat exchange plate is located away from the reactor wall while ensuring the location of the peripheral passage, and the reaction medium is radiated through the intermediate space of the heat exchange plate. Characterized by being guided in a direction.

A structurally simple and inexpensive solution for a reactor with a heat exchanger plate was found.

[0009] Cylindrical reactors generally have coatings at the two reactor ends, which are often configured in the form of a hemisphere,
A supply or discharge device for the reaction mixture and / or heat exchanger is provided. The cylindrical reactor may in principle be aligned at all positions, in which case
Vertical alignment is generally advantageous.

[0010] The heat exchange plate is a planar body having an internal space with a supply pipe and a discharge pipe, which is mainly of a small thickness compared to the area. This heat exchange plate is generally manufactured from a sheet, often a steel sheet. In use, however, special, especially corrosion-resistant, materials can be used, especially depending on the nature of the reaction medium and the heat exchanger. The supply or discharge device for the heat exchanger is generally located at the opposite end of the heat exchange plate, and according to the invention,
In the case of radial alignment of the heat exchange plates in a cylindrical reactor, it is particularly preferred to supply or discharge the heat exchange agent from the heat exchange plates via an annular conduit. In the case of vertical alignment of the cylindrical reactor, the heat exchange agent is supplied from the heat exchange plate via the lower annular conduit or discharged from the heat exchange plate via the upper annular conduit. The thing is
Particularly preferred.

According to the invention, the heat exchange plates are arranged radially in the reactor, ie along the radius of the reactor, while ensuring the location of the central internal space.

A center connected in a suitable manner to a supply pipe for the reaction medium to the intermediate space between the heat exchange plates or to a discharge pipe for the reaction medium from the intermediate space between the heat exchange plates. The interior space of can have in principle all geometric shapes, for example polygonal shapes, in particular triangular, square, preferably regular hexagonal or preferably regular octagonal shapes as well as essentially circular shapes .

Preferably, the heat exchange plate extends longitudinally of the reactor over the entire length of the essentially cylindrical reactor, excluding the reactor ends.

[0014] In one preferred embodiment, the heat exchange plates are arranged at a distance from the reactor wall while ensuring the location of the peripheral passages, wherein the reaction medium is radially passed through the intermediate space between the heat exchange plates. Be guided. The peripheral passage is preferably annular. This peripheral passage is used as a collection and / or distribution chamber for the reaction medium. The peripheral passages may be separated by a sieve in the form of a cylindrical jacket in the intermediate space between the heat exchange plates, and likewise a corresponding sieve separates the intermediate space between the heat exchange plates in the central internal space. May be. This arrangement is particularly advantageous when carrying out the reaction using a catalyst which is introduced into the intermediate space between the heat exchange plates and whose simultaneous removal with the reaction medium is avoided by a selection corresponding to the opening of the screen. It is suitable.

The radial guidance of the reaction medium can be effected centrifugally and / or centripetically, provided that only one direction is given for the radial flow behavior. The centrifugal behavior of the reaction medium is particularly preferred.

The radial flow behavior of the reaction medium between the radially arranged heat exchange plates has the advantage of low pressure losses. In the case of reactions which start under gas evolution, the pressure ratio during centrifugal behavior is particularly advantageous due to the outward increasing distance of the heat exchange plate.

In the case of the radial flow behavior of the reaction medium through the intermediate space between the radially arranged heat exchange plates, the heat exchange area used changes continuously. That is, the exchange area when the behavior of the reaction medium is centrifugal is reduced outwardly, and in the case of reactions in which the thermal profile changes, especially when the exothermic reaction decreases over the course of the reaction, Optimization of the heat exchange is guaranteed.

The radial extension of all the heat exchange plates is advantageously uniform, so that adapting the heat exchange plates to the inner vessel wall of the reactor is not necessary, but rather only one structural type. May be used.

The radial extension of the heat exchange plate is preferably in the range from 0.1 to 1 times the reactor radius, particularly preferably in the range from 0.4 to 0.9 times the reactor radius. .

The heat exchange plate is configured essentially in a plane. This does not mean that a completely flat formation is important, but rather that the heat exchange plate may be particularly curved, folded,
It may be bent or may be wavy. The heat exchanger plates are produced in a known manner, in particular by pressure molding or vacuum drawing.

[0021] The heat exchange plate may be provided with periodically shaped structural elements, especially corrugated plates. Structural elements of this kind are known as mixing elements in static mixing devices and are described, for example, in German Patent Application 19623.
051.9 and is currently used, in particular, for the optimization of heat exchange. In order to adapt to the required thermal profile, it is possible to provide a higher plate density in the outer region of the reactor compared to the inner region of the reactor, especially in the outer region of the reactor. The typical plate has a small radial extension compared to the rest of the heat exchange plate, and is advantageously 0.1 to 0.7 times, in particular 0.1 to 0.7 times, the radial extension of the remaining heat exchange plate It preferably has a radial extension in the range of 0.2 to 0.5 times. In this case, the additional plates may have equal dimensions to one another, but it is also possible to use additional plates of two or more structural types, in which case the structural types Are distinguished from each other by radial extension and / or length.

The additional heat exchange plates are preferably arranged symmetrically between the remaining heat exchange plates. This additional heat exchange plate can improve the adaptation of the respective chemical reaction to the temperature profile.

In one preferred embodiment, it is possible for the heat exchange plate to be formed in the form of a wedge, in particular a double wedge. According to this, the thin plate forming the heat exchange plate has a tapered end portion and a slightly wider end portion opposed thereto. Due to the radial arrangement of the heat exchange plates in the reactor, it is possible to ensure a well-shaped channel for the reaction mixture. It is likewise possible to provide heat exchange plates having the same radial extension or different radial extension. Particularly preferably, the heat exchange plate may be formed in a double wedge shape.

In one particular embodiment, it is possible to provide at least one annular passage in the outer periphery of the reactor space with the heat exchange plates, in which the external heat An exchange plate is arranged in the radial direction.

One preferred reactor variant comprises a continuous catalyst deposit with a refill dome at the top of the reactor and a discharge at the bottom of the reactor. In this case, a filling of the catalyst is formed, which always guarantees a complete filling of the catalyst. In order to carry out the reaction, in particular under adiabatic conditions, it is possible to modify the reactor in such a way that no heat exchange plates are arranged in the catalyst deposit.

[0026] Particularly preferably, the outer heat exchange plates are arranged offset relative to the remaining heat exchange plates. This offset arrangement is particularly advantageous in the case of strongly exothermic reactions, in which case the ends of the offset heat exchange plates projecting between the two heat exchange plates cause the heat exchange plates to be interposed. Particularly high temperatures in the region are trapped. For this purpose, it is particularly advantageous that the displaced heat exchange plates are each at least partially overlaid.

According to one preferred embodiment, there is provided a reactor composed of two or more, especially removable reactor charges, in each case between two overlapping successive reactor charges. The flow of the reaction medium at is turned by a suitable turning disk. The individual reactor charges are provided with heat exchanger plates and feed and discharge devices for the heat exchanger and the reaction medium arranged in the manner described above, ie, in particular, in the radial direction. The individual reactor charges can be constituted by flanges as required.
The flow of the reaction medium between two overlapping successive reactor charges is ensured by a suitable diverting plate having a diverting and / or separating function. By a suitable choice of the number of turning plates, several turnings of the reaction medium can be achieved.

Providing one or more reactor charges with intermediate feed points for the reaction medium, especially on the peripheral passages,
It is possible. Thereby, the reaction behavior and the temperature profile can be advantageously optimized.

It is possible to form a reactor with multiple reactor charges, having only one heat exchanger circuit. Preferably, however, two or more separate heat exchanger circulations through the heat exchanger plate may be provided. Thereby, an improved adaptation to different heat exchange requirements with the progress of chemical reactions can be achieved, e.g. carried out using two or more catalyst systems which have hitherto had different catalytic activities. In the case of the reaction described above, a single catalyst system can be aimed at.

In one particular embodiment, an injection nozzle is located in the upper region of the central interior space in the reactor, and a concentric conduit is located in the central interior space; This concentric conduit extends essentially the entire length of the reactor, excluding the reactor end, and has a cross-sectional area in the area of one-tenth to one-half of the reactor cross-section . Preferably, a baffle may be located in the reactor area below the lower end of the concentric conduit.

Such an embodiment is preferred for carrying out the reaction in a two-phase or three-phase system, in which particularly strong phase mixing is particularly important, preferably for the liquid-phase oxidation of o-xylol. The structural embodiment ensures an internal annular flow, in which case the externally pumped reaction mixture is twice as large as 30 to 30 times.
The main part of the reaction mixture, which corresponds to a double, in particular 5 to 10 times the volume flow, flows through the concentric conduits from above and downwards and through the annular space between the conduits and the reaction inner wall from below and upwards. . Reactors of this kind are described, for example, in the unpublished German Patent Application 198 53 467.8. By arranging the heat exchanger plates radially in the reactor space between the central interior space and the reactor inner wall, the reactor described, in particular with regard to the heat exchange properties,
Has been improved.

[0032] According to another preferred embodiment, the reactor may be configured as a fluidized bed reactor. By means of the arrangement according to the invention of the radial heat exchange plates in the fluidized bed, in particular the heat transfer can be improved.

The reactor according to the invention is particularly advantageous for the reaction medium in the gas phase. In this case, the flow technical advantages and the low pressure losses are particularly advantageous.

The reactor according to the invention is particularly suitable for carrying out gas-phase reactions in the presence of catalysts, in particular mobile catalysts. In this case, the mobile catalyst has the advantage, in particular, of being able to be configured in a finely divided form compared to a fixed-bed catalyst, whereby the effective surface area for the contact action is increased.

However, it is also possible, in addition or alternatively to the mobile catalyst, to apply the same mobile catalyst as a coating on the heat exchange plate of the reactor. The coating of the heat exchange plate can take place before or after incorporation in the reactor. If a heat exchange plate is already incorporated, the catalyst suspension is pumped through the reactor. In particular, according to the electrolytic deposition method, the catalyst is deposited on a heat exchanger plate and subsequently, for example, by a hot heat exchanger in the heat exchanger plate or by a mobile roll gas station.
sstation). Coating can be carried out by dipping or spraying before incorporation into the reactor. The use of a coated heat exchanger plate ensures an optimal derivation of the heat of reaction.

Particularly preferably, the reactor can be used to carry out exothermic reactions, in particular oxidation reactions, particularly preferably for the oxidation of hydrocarbons, especially alkanes and alkenes, as well as acrolein, acrylic It can be used for the production of acids, ethylene oxide, propylene oxide, maleic anhydride, phthalic anhydride or glyoxal.

Furthermore, it is possible preferably to carry out exothermic reactions, in particular dehydrogenation, preferably dehydrogenation of propane, synthesis of styrene from ethylbenzol, production of hydrocyanic acid from formamide and production of vinylformamide.

Next, the present invention will be described in detail with reference to examples and drawings. In the drawings, like reference numerals and like or corresponding features are indicated.

[0039]

DETAILED DESCRIPTION OF THE INVENTION The cross-sectional view shown in FIG. 1 of one preferred reactor 1 according to the invention having a reactor radius R shows a radially arranged heat exchange with a radial extension r. FIG. 2 shows a plate 2, the stretching of which is symmetrically distributed on the cross section of the reactor, ensuring the location of a central internal space 7.

FIG. 1A shows a supply pipe 5 for a heat exchange agent.
2 shows a longitudinal section AA of the heat exchange plate 2 provided with a discharge pipe 6.

FIG. 2 shows, besides the heat exchange plate 2, an additional heat exchange plate 3 which is arranged symmetrically with a slight radial extension compared to the heat exchange plate 2.

FIG. 3 shows additional heat exchange plates 3, 4 each having a slight radial extension compared to the heat exchange plate 2 and having a symmetrical arrangement on the cross section of the reactor. 2 shows two different structural types.

FIG. 4A shows one longitudinal section according to a preferred embodiment with a peripheral passage 8. If necessary, a stay screen 13 may be provided.

FIG. 4B shows a cross section of the reactor described in FIG. 4A in a longitudinal section.

FIG. 5A schematically shows a reactor composed of a number of reactor charges, connected via a flange, in longitudinal section. The reaction mixture flows radially and alternately centrifugally or centripetically through the reactor, with a diverting disc 9 being arranged between the multiple reactor charges. The possibility of intermediate feeding of the reaction mixture is indicated by the left and right arrows.

FIG. 5 (B) is a cross-sectional view of the region AA of the reactor shown in FIG. 5 (A) in a longitudinal sectional view, and FIG. 5 (C) is a longitudinal sectional view. Region BB of the reactor described in FIG. 5 (A) of the plan view is shown in cross section.

The reactor, which is schematically shown in FIG. 6A in longitudinal section, is provided with two separate circulations of the heat exchanger, in which case the feed device 5 and the discharge device 6 are preferably annular It is configured as a passage.

The cross-sectional view in FIG. 6B (section AA in FIG. 6A) shows a preferred embodiment of the heat exchange plates 2, 3, 4 having different radial extensions.

FIG. 7A shows a continuous catalyst deposit 17.
Is schematically shown in longitudinal section. The catalyst is
It is introduced via a refill dome 18, in particular by being rocked by a vibrator. Due to the introduction via the refill dome, there is always a buffer of the catalyst, which is always ensured by a continuous filling of the catalyst. The catalyst deposit 17 is withdrawn from the reactor 1 via a suitable, in particular conical, discharge device 19 which is provided, if necessary, with a holding grid at the discharge of the catalyst. Around the reactor, one or more, especially annular, intermediate feed pipes 20 are provided for the reaction mixture.
May be provided. The reactor is preferably configured as a plug-in module, in which the entire contents, in particular the heat exchanger plates 2, 3, 4, 16 are, can be removed at any time by a suitable device, in particular a crane, so that it is easy to handle. It is configured as follows.

FIGS. 7 (B) and 7 (C) are longitudinal sectional views of regions AA and B of the reactor described in FIG. 7 (A).
-B are shown in cross-sectional views. By arrows, the flow of the reaction mixture is shown from inward to outward in FIG. 7 (B) and outward to inward in FIG. 7 (C).

FIG. 8A shows a continuous catalyst deposit 17.
Another preferred embodiment of the reactor according to the invention, having an intermediate feed line 20 for the reaction mixture, is schematically shown in longitudinal section. Unlike the embodiment shown in FIGS. 7 (A) to 7 (C), no heat exchange plate is provided in the catalyst deposit. Such an embodiment is particularly advantageous in the case of an adiabatic reaction operation, for example in the case of the styrene process.
In addition to the heat exchange plate 16 arranged in the annular passage 15, the heat exchange plate 2 can be arranged in the central internal space 7,
In particular, as indicated by the solid line with the arrow in the figure, the heat exchange plate 2 is arranged with the central inner area empty to guide the reaction mixture in the turning area for the reaction mixture. be able to. It can clearly be seen that no heat exchange plates are arranged in the region of the catalyst deposit 17 as shown in the cross-sectional views of FIGS. 8 (B) and 8 (C). The internal heat exchange plate 2 is provided only when necessary.

FIG. 9 schematically shows a reactor with an internal annular flow of the reaction medium in longitudinal section. This reaction medium is
Introduced via a nozzle 10 which may be immersed in a concentric conduit 11 or terminate above the conduit, between the central inner tube and the reactor inner wall in the internal annular flow Guided into space. This annular flow configuration is supported by baffles 12 which are arranged in particular in the region of the bottom of the reactor.

FIG. 10 shows a longitudinal section of the fluidized bed reactor shown schematically. A distribution plate 14 is arranged in the region of the bottom of the vessel, on which a fluidized bed for supplying a reaction gas via the lower end of the reactor is formed. Heat exchange plates 2 are arranged in the fluidized bed in the radial direction.

FIG. 11A schematically shows in a longitudinal section a special embodiment designed as a bubble column reactor having a distribution member 21 in the lower region of the reactor 1. The distribution element is designed as a porous medium, in particular as a frit, or as a perforated plate. The function of this distribution member may be to take over the plug-in tube with pores in the tube wall. By means of the arrows, the supply of gas in the lower central area of the reactor 1 and the discharge of gas in the upper central area are evident, and the reactor 1 above the distribution member 21
The supply of liquid in the lower region and the discharge of liquid in the upper region of the reactor at the periphery is evident. FIG. 11 (B)
(Section AA in FIG. 11 (A)) illustratively shows radially arranged heat exchange plates 2, 3 having different radial extents.

FIG. 12 shows a longitudinal section of another special embodiment of the crystallization apparatus. The mixture to be crystallized is introduced via a supply line 23 into the inner region of the concentric conduit 11, where a stirrer 22 is arranged. The stirring shaft can be provided from above, as shown in the drawing, but it is in principle also possible to arrange the stirring shaft from below in the reactor. Below the heat exchange plate 2 arranged in the radial direction, a coarse particle extraction pipe 24 is provided.
Is provided around the reactor 1, and a fine particle take-out tube 25 is provided.

FIGS. 13 to 15 show, in cross-section, a special embodiment of the reactor according to the invention with a wedge-shaped heat exchanger plate. As already mentioned above, heat exchange plates are generally manufactured from thin plates. The lamellas need not be strictly parallel, but can instead be wedge-shaped with tapered ends and opposed slightly wider ends. The heat exchange plate thus configured can be mounted in a reactor in a particularly advantageous radial arrangement. In this case, particularly preferred is
A well-defined channel for the reaction mixture is formed between the heat exchange plates. Moreover, producing such wedge-shaped heat exchange plates is technically simple and inexpensive.

As shown in FIG. 13, the entire wedge-shaped heat exchange plate 2 may be formed identically, but according to the description of FIG. Apart from the heat-exchange plate 2 having a large spread, it is also possible to provide an additional heat-exchange plate 3 with a slight radial spread.

FIG. 15 shows a specially designed wedge-shaped heat exchanger plate 26 which is formed in the form of a double wedge and allows a particularly favorable guidance of the reactant mixture. It is.

[Brief description of the drawings]

FIG. 1 is a cross-sectional view (FIG. 1A) showing a first embodiment of a reactor according to the present invention, and a vertical cross-sectional view (FIG. 1A) of a heat exchange plate shown in FIG. 1 (B)).

FIG. 2 is a cross-sectional view showing a preferred embodiment having an additional heat exchange plate.

FIG. 3 is a cross-sectional view showing another preferred embodiment having two types of additional heat exchange plates.

4 is a longitudinal sectional view showing a preferred embodiment having a peripheral passage and a guide member for guiding a reaction medium in a radial direction (FIG. 4);
(A)), and AA of the embodiment described in FIG.
FIG. 4 is a cross-sectional view along the line (FIG. 4 (B)).

FIG. 5 is a longitudinal sectional view (FIG. 5 (A)) showing another preferred embodiment having multiple reactor charges, and FIG. 5 (A).
FIG. 5 is a cross-sectional view of the reactor taken along line AA of FIG.
(B)), and BB of the reactor described in FIG. 5 (A).
FIG. 5 (C) is a cross-sectional view taken along the line.

FIG. 6 is a longitudinal sectional view showing another preferred embodiment having multiple circulation paths of the heat exchange agent (FIG. 6 (A)), and FIG.
FIG. 7 is a cross-sectional view (FIG. 6 (B)) of the reactor described in (A), taken along line AA.

FIG. 7 is a longitudinal sectional view showing another preferred embodiment having an intermediate supply pipe and a catalyst deposit (FIG. 7 (A)), FIG. 7 (A).
FIG. 7 is a cross-sectional view taken along line AA of the reactor described in FIG.
FIG. 8 (B)) and a cross-sectional view (FIG. 7 (C)) of the reactor shown in FIG. 7 (A) along the line BB.

FIG. 8 has an intermediate feed tube and catalyst deposits, but without heat exchanger plates in the catalyst deposits,
8 (A), a cross-sectional view (FIG. 8 (B)) of the reactor shown in FIG. 8 (A) along the line AA, and FIG. FIG. 9 is a cross-sectional view (FIG. 8 (C)) of the reactor described in (A), taken along line BB.

FIG. 9 is a longitudinal sectional view showing another preferred embodiment having an internal annular flow of the reaction medium.

FIG. 10 is a longitudinal sectional view showing another preferred embodiment as a fluidized bed reactor.

11 is a longitudinal sectional view (FIG. 11 (A)) showing another preferred embodiment as a bubble column reactor, and a transverse sectional view taken along the line AA of the reactor shown in FIG. 11 (A) ( (Fig. 11 (B))
It is.

FIG. 12 is a longitudinal sectional view showing another preferred embodiment of the crystallization apparatus.

FIG. 13 is a cross-sectional view showing another preferred first embodiment having a wedge-shaped heat exchange plate.

FIG. 14 is a cross-sectional view showing another preferred second embodiment having a wedge-shaped heat exchange plate.

FIG. 15 is a cross-sectional view showing another preferred third embodiment having a wedge-shaped heat exchange plate.

[Explanation of symbols]

1 reactor, 2, 3, 4, 16 heat exchange plate, 5, 2
3 supply pipe, 6 discharge pipe, 7 central internal space,
8 peripheral passage, 9 turning disk, 10 nozzle, 1
1 concentric conduit, 13 stagnation screen, 14 distribution plate, 15 annular passage, 17 catalyst deposit, 18
Refill dome, 19 discharge device, 20 annular intermediate supply pipe, 21 distribution member, 22 stirrer, 24, 2
5 Coarse particle extraction tube, 26 wedge-shaped heat exchange plate, R
Reactor radius, r Radial stretching

 ──────────────────────────────────────────────────続 き Continued on the front page (72) Inventor Gerhard, Olberto Germany, 69221, Dosenheim, Frankenweg, 11 (72) Inventor Uwe, Stabel Germany, 67166, Otterstadt, Paperstrasse, 31 (72) Inventor Peter, Zener Germany, 67071, Ludwigshalfen, Erich-Kestner-Strasse, 15

Claims (20)

[Claims] A heat exchange plate (2, 3,
4), supply and discharge devices (5, 6) for the heat exchanger to the heat exchange plates (2, 3, 4) and of the heat exchange plates (2, 3, 4) through which the reaction medium flows. In a cylindrical reactor (1) having an intermediate space between the heat exchange plates (2,
A cylindrical reactor (3) with a heat exchange plate, characterized in that the reactors (3, 4) are arranged radially in the reactor (1), while ensuring the location of the central internal space (7). 1). 2. Reactor according to claim 1, characterized in that the heat exchange plate extends over the entire length of the essentially cylindrical reactor (1) except for the reactor end. (1). 3. The heat exchange plates (2, 3, 4) are arranged at a distance from the reactor wall while ensuring the location of the peripheral passages (8), and the reaction medium is provided with heat exchange plates (2, 3, 4) 3. The reactor (1) according to claim 1 or 2, characterized in that it is guided radially through the intermediate space of (1). 4. The radial stretching (r) of all the heat exchange plates (2, 3, 4) is uniform and 0.1 to 1 times the radius (R) of the reactor, in particular of the reactor. Radius (R) of 0.4-0.
Reactor (1) according to one of the claims 1 to 3, characterized in that it is 9 times. 5. The reactor (1) according to claim 1, wherein the heat exchange plates (2, 3, 4) are essentially planar. 6. The heat-exchange plate (2, 3, 4) is provided with periodically shaped structural elements, particularly corrugated plates. The reactor (1) according to any one of the preceding claims. 7. The density of the heat exchange plates (2, 3, 4) in the outer region of the reactor is higher than in the inner region of the reactor, in particular additional heat exchange in the outer region of the reactor. The plates (3, 4)
The radial stretching (r) is small compared to the remaining heat exchange plate (2), and is preferably between 0.1 and 0.2 mm for the radial stretching of the remaining heat exchange plate (2). 7. Reactor (1) according to any one of claims 1 to 5, characterized in that it is in the range of 0.2 to 0.5 times. 8. The additional heat exchange plate (3, 4) has two or more structural types, these structural types being distinguished from one another by radial extension. A reactor (1) according to claim 7. 9. The heat exchange plate according to claim 1, wherein the heat exchange plate is formed in the form of a wedge.
The reactor (1) according to any one of claims 1 to 8. 10. At least one annular passage (15) is provided in the outer periphery of the reactor space provided with the heat exchange plates (2, 3, 4), in which the outer passage is provided. Reactor (1) according to one of the preceding claims, characterized in that the heat exchange plates (16) are arranged radially. 11. Reactor (1) according to claim 10, characterized in that the outer heat exchange plates (16) are arranged offset relative to the heat exchange plates (2, 3, 4). . 12. A continuous catalyst deposit (17) is provided in the upper region of the reactor (1) together with a refill dome (18), and a discharge device (19) is provided below the reactor (1). Reactor (1) according to one of the preceding claims, characterized in that it is provided in a side region. 13. Reactor (1) according to claim 12, characterized in that no heat exchange plates (2, 3, 4) are arranged in the region of the catalyst deposit (17). 14. The flow of the reaction medium between two or more reactor charges, each consisting of two or more particularly removable reactor charges, is provided by a suitable deflecting disk (9). Reactor (1) according to one of the preceding claims, characterized in that it is turned. 15. The reactor (1) according to claim 14, characterized in that there are provided two or more separate heat exchanger circulations through the heat exchanger plates (2, 3, 4). 16. A nozzle (1) is provided in a central internal space (7).
0) and a concentric conduit (11) are arranged, said concentric conduit extending essentially the entire length of the reactor (1) excluding the reactor end, and (1)
Reactor (1) according to one of the preceding claims, characterized in that it has a cross-sectional area in the region of one-half to one-half of the cross section of the reactor. 17. Reactor (1) according to claim 16, characterized in that a baffle (12) is arranged in the reactor area below the lower end of the concentric conduit (11). 18. Reactor (1) according to claim 1, characterized in that it relates to a fluidized bed reactor. 19. The method according to claim 1, wherein the gas-phase reaction is carried out in the presence of a catalyst.
Use of a reactor (1) according to claim or claim 18. 20. Performing an exothermic reaction, in particular an oxidation reaction, particularly preferably the oxidation of hydrocarbons, especially alkanes or alkenes, and of acrolein, acrylic acid, ethylene oxide, propylene oxide, maleic anhydride, phthalic anhydride or glyoxal. Use of a reactor (1) according to any one of claims 1 to 18 for the production.