DE102009031765B4 - Converter for carrying out exothermic catalytic reactions - Google Patents

Abstract

Converter for carrying out exothermic catalytic reactions with a body (1, 2) with at least one inlet (3) for feeding in the starting components and at least one outlet (4) for discharging the reaction products, with a reaction space in the lower part (2) of the body (25), which is delimited by an inner support structure (17) and an outer support structure (24), wherein a plurality of heat panels (8) are arranged in the reaction space (25), an inner cavity (17) being located within the inner support structure (17). 22), the inlet (3) being arranged in such a way that the starting components flow through the outer support structure (24) into the reaction space (25) and the outlet (4) is connected to the inner cavity (22), the lower one Part (28) of each heat panel (8) in the lower part (2) of the body is designed as a hollow body with a wedge-shaped base, the pointed part being directed to the central axis (21) of the body and where in the upper part (29) of each heating panel (8) made of ...

Description

The invention relates to the field of technological equipment for carrying out catalytic processes and can be used in the chemical, petroleum and other industries for carrying out exothermic catalytic reactions.

SU 852541 (1981) discloses a reactor intended to carry out reactions of polymerization and copolymerization of gaseous monomers. The mentioned reactor consists of a body with means for supplying and discharging a circulating gaseous medium, the starting components and the finished product, a shaft with mixing blades, which consist of heat pipes, heat exchanger and pump, wherein the heat pipes vertically and concentrically to the shaft in different radii are arranged to the rotation axis. The means for supplying and discharging the gaseous medium are arranged diametrically in the upper part of the reactor, with the upper ends of said heat pipes between said devices. Disadvantages of this known reactor are a design-related low efficiency and associated low yield of target product.

RU 2278726 C1 discloses a reactor for carrying out catalytic gas phase processes, which comprises a body, a device for supplying the starting components and a device for discharging the finished product, and a device for supplying or removing heat, which is designed in the form of a plurality of heat pipes, consists. This known reactor also contains a catalyst, which is applied to the heat pipes and / or the body as a coating. The heat pipes are arranged in the space of the carcass in a checkered manner and their entire surface, which is located in the catalytic zone, is chosen so that it ensures the supply or discharge of the amount of heat energy necessary for carrying out the catalytic process. Disadvantages of this known reactor are again a design-related low efficiency and low yield of target product.

EP 2062640 A1 discloses a reactor having plate-shaped heat exchange elements disposed radially about the central outlet. In the DE 60205645 T2 disclosed heat exchanger units consist of substantially rectangular, flat, box-shaped heat exchangers with an inner chamber for passing a heat exchange fluid. The heat exchange fluid is guided in the inner chambers in part circular. In DE 60109326 T2 and US 2003/0175184 A1 Reactors are shown with heat exchangers, in which several plate-shaped heat exchange elements are summarized.

DE 19754185 C1 discloses a reactor having heat exchanger plates formed as a thermal medium through which a cooling medium flows.

US 2005/0158217 A1 has a method for the observation, control and regulation of reactions of liquid reaction mixtures in reactors with thermal plates, which are flowed around by a heat transfer medium.

DE 2016614 A (filed April 8, 1971) discloses a cylindrical reactor for partial catalytic oxidation reactions. The gas mixture to be reacted enters axially into the central gas feed ( 1 ) and flows radially through a perforated plate or wire mesh in the filled with a catalyst circular sectors ( 2 ). The sectors ( 3 ) are plate heat exchangers through which cooling liquid is pumped in the axial direction. Due to the special spatial arrangement of the catalyst in the form of circular ring sectors, the heat exchange surfaces are adapted to the course of the reaction. The conversion and thus the heat of reaction is greatest at the entrance to the catalyst sectors, namely where the distance of the cooling surfaces is the lowest and thus the cooling effect is greatest.

EP 1 350560 A1 discloses a tubular reactor with axial flow direction. The reactor preferably contains mutually parallel heat exchange elements that are wedge-shaped.

The object of the invention is to provide a converter for carrying out exothermic catalytic reactions, which is characterized by an increased efficiency and an increase in the quality of the product produced.

The converter should be particularly suitable for carrying out catalytic exothermic reactions in the gas phase with a temperature regime which is almost isothermal in the reaction space.

This object is achieved by a converter according to claim 1. Advantageous embodiments are specified in the dependent claims.

The converter according to the invention for carrying out exothermic catalytic reactions has a body with at least one inlet for the feed of the starting components and at least one outlet for the discharge of the reaction products. The one or more feeds are preferred in the form of nozzles in the side wall of the carcass appropriate. The drain or the drains are preferably arranged in the lower part of the carcass.

The body forms the outer wall of the converter and is subsequently split functionally into a lower and an upper part. The body can be made in one piece, however, for ease of handling (assembly / disassembly) preferably in two or three parts (an upper, preferably in half-shell shape and a lower, the bottom in the form of a half-shell) made, preferably by flanges together are connectable. The body has at least one inlet for the supply of the starting components and at least one outlet for the removal of the reaction products.

In the lower part of the carcass is the reaction space in which the exothermic catalytic reaction takes place. The reaction space is bounded radially by an inner and an outer support structure. In the inner support structure is a cavity - the inner central tube - which serves for the discharge of the gaseous reaction product to the outside, via a nozzle in the lower part of the carcass. The conclusion down is formed by a bottom plate or mounted on this catalyst table. Through the bottom plate protrudes the inner central tube. At the top, the reaction space is limited by a cover, preferably a seal.

Between the outer support structure and the inner wall of the carcass preferably remains an outer cavity, which serves for the distribution of the starting components. In the wall of the carcass, the inlet is arranged so that the starting components preferably flow through the outer support structure via this outer cavity into the reaction space. The reaction space forms the reaction zone, d. H. in this the chemical reaction takes place. The reaction products then flow into the internal cavity (inner central tube) connected to the drain.

According to the invention, a plurality of heat panels are arranged inside the carcass on the catalyst table or directly on the bottom plate. For the purposes of this application, heat panels are generally understood as meaning a hollow element, preferably a bar or tubular element, or in another form for dissipating the heat of reaction from the reaction space.

The heat panels are mounted on the bottom plate and are additionally fixed in place by vertical partitions which are mounted on the bottom plate.

Each heat panel has a lower part which is located in the reaction space and an upper part which protrudes from the reaction space into the upper part of the carcass and is in operative connection therewith with a heat exchange device. The lower parts of the heat panels are used to absorb the heat from the reaction space in which the catalyst is located and the exothermic reaction takes place. The upper parts of the heat panels are operatively connected to heat exchange devices through which the heat is dissipated to the outside using a heat exchange medium.

The lower part of the heat panels is designed as a hollow body with a wedge-shaped base, wherein each of the pointed part is directed to the central axis (to the inner central tube) in the lower part of the body.

The invention relates to the converter, in the reaction space catalyst can be filled.

Between the wedge-shaped lower parts of the heat panels, the catalyst is filled. The catalyst is preferably poured. The described wedge-shaped panel construction ensures an optimal ratio of the surface of the heat panels to the catalyst volume, whereby the necessary temperature stability is ensured in the catalyst bed.

The reaction space is thereby outward, d. H. shell side towards the body, bounded by the outer support structure, which is fixed around the heat panels, d. H. the outer support structure surrounds both the catalyst and the heat panels. Supporting structure is generally understood to mean a structure which keeps the preferably poured catalyst in the form, i. H. which is impermeable to the catalyst, but through which a mass transfer is possible. The outer support structure is a gas-permeable, at least approximately cylindrical structure, preferably a net or grid or also a perforated vessel or a combination thereof.

The reaction space (catalyst bed and heat panels) is preferably arranged radially around the inner support structure, which limits the inner cavity (inner central tube). The reaction space is preferably cylindrical. Inside this cylinder is then the inner cavity (inner central tube), limited on the shell side by the inner support structure.

The inner support structure is preferably a perforated vessel or else a mesh or grid or a combination thereof, particularly preferably one perforated vessel which is confined to the reaction space by a net.

The perforated vessel is tightly closed at the top or is covered by a seal and possibly a net.

Both the inner and the outer support structure serve as support elements for the preferably poured catalyst and are (in the contact region to the catalyst) permeable to the starting components (starting materials) and the reaction products which are preferably present in the gas phase under the selected reaction conditions in the converter.

On top of the reaction space, d. H. Above the catalyst bed, the lower parts of the heat panels and the inner central tube is at least one cover. Through the cover protrude the upper parts of the heat panels. The cover is preferably a seal. The cover preferably has a high hydraulic resistance. The cover ensures that the reaction gases flow radially through the catalyst bed to the inner central tube. The seal preferably contains or consists of mats of thermally stable material. Through the seal, the gas flow from the outer wall of the converter to the central tube is guided radially through the catalyst bed, which is located between the heat panels, and through the inner central tube to the outlet in the lower part of the carcass.

In order to increase the efficiency of the converter, the catalyst is preferably incorporated not only between the heat panels but also between the heat panels and the inner and / or outer support structure. Particularly preferably, the heat panels are completely enclosed by the catalyst to the sides. The volume of the catalyst, which is located between the outer support structure and the heat panels, preferably does not exceed 15% of the total volume of the catalyst.

The volume of the catalyst, which is located between the inner support structure and the heat panels, preferably does not exceed 30% of the total volume of the catalyst.

The majority, preferably 55% to 85%, of the catalyst volume is thus located between the heat panels.

The distance between the individual heat panels (and thus the thickness of the catalyst layer between them) is preferably 8 mm to 200 mm.

According to the invention, the heat panels are connected to at least one heat exchange device (heat exchanger) in the upper part of the carcass. Each heat panel may preferably include a cylindrical heat exchange device. Alternatively, the heat exchange device is implemented as a unit for all the heat panels. In this alternative, the upper part of the body preferably forms a space for heat exchange, which is separated from the reaction space by an intermediate bottom. The heat exchange device serves to remove the excess heat of reaction from the reaction zone by transferring the heat to a heat exchange medium which passes through the heat exchange device or devices. The heat exchange medium enters the upper part of the body of the converter through an inlet port, passes through the heat exchangers or the heat exchange device in the upper part of the heat panels, absorbing the excess heat of reaction and evaporating, leaving the upper part of the body of the converter through an outlet nozzle. Preferably, the converter contains at least one outlet for the gaseous heat exchange medium.

If several heat exchange devices are used, the converter preferably contains collectors with which the heat exchange devices are connected to each other. In a collector, the gaseous heat exchange medium is collected from the individual heat panels to co-discharge it from the converter. Other collectors are preferably used to feed the heat exchange medium to the heat exchange devices and to dissipate the heat exchange medium used for rinsing.

The energy dissipated with the heat exchange medium can be used for different processes (for example for preheating the starting components or for the bottom heating of the rectification column for product separation). The upper part of the heat panels (heat exchange device) is tubular and preferably has an inner tube and a jacket. The heat exchange medium flows in the jacket. The bottom of the shell is continuously flowed through at low flow rate of the liquid heat exchange medium, or may also be during the reaction process in the jacket tubes, with a taking place after the reaction process draining to blow down and drain the jacket pipes. This ensures avoidance of accumulation of harmful admixtures (salts and others) in the heat exchange means.

The lower parts of the heat panels are executed in the reaction chamber as a hollow body, with a wedge-shaped base. The outer walls of the lower parts of the heat panels are in contact with the catalyst bed, which gives off heat. Inside the heat panels is a heat carrier, which absorbs the heat of reaction from the catalyst bed. The heat carrier vaporizes and preferably rises through pipes mounted inside the lower parts of the heat panels into the upper part of the heat panels, where it gives up its heat energy to a heat exchange medium located in the shell around the pipe of the upper part of the heat panels , As a result, the heat transfer medium itself becomes liquid again and flows back within the heat panel. Ie. The heat transfer medium is conducted in the heat panels in a closed circuit. The heat panels are constructed in their interior so that the returning heat transfer medium flows along the inner wall of the heat panels. For this purpose, the heat panels in the lower area contain fixtures, over which the returning heat transfer medium is distributed. Each heat panel preferably contains at least one tube which receives the gaseous, ascending heat transfer medium.

The heat transfer medium is dependent on the process temperature to be reached in the converter, i. H. the temperature in the reaction zone, selected. As a heat transfer medium not only classic heat transfer mediums such as liquid metals (eg., Sodium and cesium) or molten salts, but also simpler and cheaper as elemental sulfur, heat transfer medium based on mineral oil, such. B. long-chain alkanes, such as. As C12 (n-dodecane) can be used.

Water, thermal oil, ammonia or other heat exchange means can advantageously be used as the heat exchange medium.

Preferably, the heat panels are configured to receive and dissipate all of the heat energy transferred from the reaction zone via the heat transfer medium and the heat exchange medium, i. H. the heat exchange surface in the reaction zone (the contact surface of the heat panels to the catalyst) is dimensioned according to the heat energy to be absorbed. By the level of the heat exchange medium in the heat exchange devices, the amount of heat to be dissipated from the converter and thus ultimately the temperature in the reaction zone can be advantageously set.

The temperature difference between the temperature in the reaction zone (catalyst layer) and the temperature of the heat carrier in the interior of the heat panels in the region of the reaction zone is preferably set below 60 ° C., preferably below 30 ° C.

The ratio of the heat exchange surface in the reaction zone (ie the contact surface of the wedge-shaped lower part of the heat panels with the catalyst) to the catalyst volume is therefore dependent on the dissipated heat energy, ie the reaction to be carried out in the converter. The ratio of the heat exchange surface in the reaction zone to the catalyst volume is preferably at least 10 m ² / m ³ , more preferably 60 m ² / m ³ , and is preferably in the range of 10 m ² / m ³ to 250 m ² / m ³ , especially preferably 60 m ² / m ³ to 150 m ² / m ³ . An oversized heat exchange surface has no negative impact on the process.

The outer surfaces of the heat panels in the reaction zone are preferably coated with a layer of aluminum dioxide and / or enamel. The thickness of this layer (s) total preferably 0.1 to 2 mm, more preferably 0.2 to 1 mm, in particular 0.3 to 0.7 mm.

The heat exchange area of the heat exchange devices is preferably 3 to 10 times less than the surface area of the lower panel parts (heat exchange area in the reaction zone). This area corresponds to the possible contact area of the heat panels to the heat exchange medium. By the level of the heat exchange means, this can be advantageously varied and thus the temperature can be set in the converter.

Preferably, the converter additionally contains at least one temperature measuring device, preferably thermocouples. These are preferably introduced through nozzles in the upper region of the body of the converter. The temperature measuring devices are preferably in contact with the catalyst bed and allow the temperature measurement in the reaction zone. Preferably, the converter contains at least one temperature measuring device, more preferably 3 temperature measuring devices, which are distributed uniformly over the cross section and each measuring the temperature in the reaction zone in 3 different heights. The temperature measuring devices thus allow monitoring of the function of the heat panels and control of the temperature in the reaction zone. The temperature measuring devices enable fully automatic process control by automated control of the level of the heat exchange medium in the heat exchange devices.

The converter according to the invention is thus a reactor which, due to its special structure, is particularly suitable for an isothermal reaction regime is suitable, ie a reaction at a nearly constant temperature in the entire volume of the reaction space. Due to the direct contact of the heat panels with the catalyst layer, the heat produced by the exothermic reaction can advantageously be dissipated directly at the point of origin.

The structure of the converter according to the invention, in particular the arrangement of the heat panels and the catalyst, makes it possible to set an optimum ratio of the surface of the heat panels to the volume of the catalyst, whereby a temperature control near the isothermal conditions in the entire volume of the reaction space is ensured.

Advantageously, in the converter according to the invention, depending on the reaction for which it is used, different catalysts (for example a copper-containing catalyst for the synthesis of methanol from synthesis gas or a zeolite-containing catalyst for the conversion of methanol to gasoline) can be used. Due to the flexible structure of the carcass, which is composed of an upper and a lower part, it becomes possible to easily replace the catalyst (if necessary, the renewal of the catalyst after deactivation of the catalyst or when using the converter for another reaction).

Due to its high efficiency, in particular the higher product yield at higher throughputs in relation to the catalyst volume, it becomes possible for certain processes, in which a plurality of conventional reactors are used in series (eg in the process of methanol synthesis), three classic from the State of the art known reactors to replace by a converter according to the invention.

In addition, it becomes possible to make the converter very compact. For example, dimensions of the body of 1 to 3 m in diameter and heights of 2 to 20 m are possible. However, the size of the converter is determined by the process and throughput to be performed therein.

The almost isothermal reaction regime makes it possible to increase the yield of target product compared to the adiabatic reaction regime and at the same time to increase the product selectivity. Thus, fewer by-products are obtained, which significantly improves the effectiveness of the overall process.

Another object is therefore also the use of the converter according to the invention for carrying out chemical, catalytic reactions in the gas phase, preferably with almost isothermal reaction control. It finds application especially in the chemical and petroleum chemical industries.

The invention also relates to the use of the heat panels as an important component of the converter according to the invention. The heat panel is hollow inside and has the following components:

• a.) A lower part, which is designed as a hollow body with wedge-shaped base surface, whose lateral surfaces are formed as heat exchange surfaces,
• b.) an upper part, which is formed as a tube and is in operative connection with a heat exchange device or can be brought into operative connection, wherein the tube of the upper part is connected to the upper base of the lower part, so that in the lower part of vaporized heat transfer in the tube can rise and the condensed heat carrier from the tube can flow back into the lower part.

The lower part of the heat panels contains horizontal internals, through which the refluxing heat transfer medium is distributed and is constructed in its interior so that the refluxing condensed heat transfer flows to the inner wall of the panels down. The lower part of the heat panels preferably contains further tubes for the discharge of the vaporized heat carrier in the upper part.

Preferred embodiment of the converter according to the invention:

In a preferred embodiment, the converter according to the invention has a body with a nozzle for supplying the starting components and a nozzle for discharging the reaction products. In the lower part of the body, there is a bottom plate on which a plurality of heat panels are arranged, in the upper part the mentioned heat panels are in operative connection with heat exchanging devices designed to allow the passage of a heat exchange medium through them Heat panels filled with the catalyst, which is bounded from the outside by a network as the outer support structure, which is attached to the heat panels and the catalyst bed therebetween, on the inside, the space occupied by the catalyst and heat panels, through a perforated vessel as limited inner support structure. Preferably, a net is mounted on the outer surface of the perforated vessel, which allows to fix the catalyst particles at the place of their use. The interior of this perforated vessel forms a hollow cylinder - the inner central tube - through which the flow formed gaseous reaction products to the outside.

About catalyst, heat panels and inner central tube is a seal with a high hydraulic resistance. In the preferred variant of the realization, the seal consists of mats of thermally stable material with a high hydraulic resistance, which forces the reaction gases to a radial flow through the catalyst bed in the direction of the central tube.

Preferably, the body comprises a lower part and an upper part, which are connected to each other by use of flanges, which ensures the ease of assembly / disassembly of the converter.

In the upper part of each heat panel may be arranged a cylindrical heat exchange device for removing the heat of reaction from the reaction zone. As a variant, the heat exchange device for dissipating the excess heat of reaction may be a unit for all the heat panels.

The heat panel has a wedge-shaped shape with the pointed portion facing the central axis of the body. Such a panel configuration ensures an optimum ratio of the surface area of the heat panels to the catalyst volume and ensures the necessary constant rate of flow in the catalyst.

The converter may additionally include thermocouples in the region of the heat panels inserted through sockets located on the body. The use of the mentioned thermocouples allows to control the temperature in the reaction zone.

Another object of the invention is the use of heat panels in a converter according to the invention, which are characterized by the following structure.

Preferred embodiment of the heat panels according to the invention:

The lower part of the heat panels has a cylindrical shape with a wedge-shaped base. Inside, the heat panel is hollow. It contains fixtures. Connected to the upper cover of the lower part of the heat panels is a pipe which, as the upper part of the heat panels, forms a unit together with the lower part of the heat panels. The surface of the lower part of these heat panels serves as a heat exchange surface between the reaction space located around the heat panels and the heat transfer medium inside the heat panels. The heat transfer medium in the interior of the heat panels absorbs the heat generated during an exothermic reaction, whereby it evaporates. The gaseous heat carrier rises inside the heat panels in built-in tubes upwards and collects in the attached to the lid of the heat panels tube. The tube is in its upper part with a heat exchange device in operative connection to which the amount of heat absorbed by the heat transfer in the reaction chamber, the heat transfer condenses, runs down the inner wall of the manifold and inside the lower cylindrical panel part via horizontal internals to a is drained flow on the inner wall and flows down. In the reaction space, the condensed heat carrier evaporates again by absorbing the heat of reaction.

Based on the following figures and embodiments, the invention will be explained in more detail without being limited to these.

In 1 is the side view (vertical section) of a converter according to the invention,

in 2 is a horizontal section of the converter through the reaction space,

in 3 is the horizontal section of a heat panel shown and

in 4 the vertical section of a heat panel and a heat exchange device is shown.

The in 1 and 2 shown converter for carrying out exothermic catalytic reactions is limited by a body consisting of a lower part 1 and from an upper part 2 is composed. The body has a central axis 21 , In the body are nozzles for feeding the starting components 3 and for the derivation of the reaction products 4 appropriate. The body is composed, with the lower part 1 with the upper part 2 by using flanges 5 and 6 connected is. In the lower part 1 the body of the converter is a bottom plate 7 which is the bottom of the reaction space 25 forms and on which heat panels 8th are located. Above the reaction space 25 are the upper parts of the heat panels with heat exchange devices 9 connected by which the heat exchange means for removing the heat energy from the heat panels 8th flows. The heat exchange medium passes through an inlet nozzle 10 into the collector for the heat exchange medium (eg feed water) 11 on, it continues to flow through the heat exchange devices 9 where it evaporates in gaseous form in the vaporized heat exchange medium collector 12 collects and then it passes through the outlet for the evaporated heat exchange medium 13 discharged in gaseous form. The rinse water collector 14 serves the collection of heat exchange means for flushing the lower parts of the heat exchange devices to avoid salt deposits, and the Spülwasseraustrittsstutzen 15 serves its derivative from the converter. Between the heat panels 8th which have a wedge-shaped form in the region of the reaction space (s. 3 ), is a catalyst 16 interspersed. The reaction space 25 including heat panels 8th , is on the outside (shell side) by a network as an external support structure 24 limited. The volume of the catalyst between the edge of the heat panels 8th and the outer support structure 24 is less than 15% of the total volume of the catalyst. Inside the reaction space 24 becomes an inner cavity 22 through a perforated vessel as an inner support structure 17 limited, which forms the inner central tube through which the reaction gases flow. This perforated vessel is also wrapped in a net to avoid entraining catalyst particles outward along with the reaction gas. The volume of the catalyst between the inner support structure 17 and the heat panels 8th is less than 30% of the total catalyst volume.

The reaction space 25 and the inner cavity 22 be on the top by a seal 18 limited, which consist of mats made of a thermally stable material with a high hydraulic resistance. This seal 18 prevents the gaseous starting components from the space between the wedge-shaped parts of the heat panels 8th flow past or in from the inner support structure 17 limited internal cavity 22 (Central tube for discharging the reaction gases) or from the catalyst layer flow from below into the upper converter space. The seal 18 has tight passages for the heat panels 8th , The gaseous starting components thus flow only through the catalyst bed 16 that lie between the heat panels 8th located. Through the neck 19 are multi-zone thermocouples 20 performed to measure the temperature in the reaction space 25 , In the reaction room 25 the thermocouples run 20 directly through the catalyst bed 16 parallel to the central axis at a defined distance from the adjacent heat panels 8th ,

The operating principle of the converter with the heat panels 8th is as follows: In the converter gaseous starting components pass through the nozzle 3 on, they pass over the outer cavity 23 in the reaction space 25 , In the reaction room 25 If an exothermic reaction takes place, the reaction products emerge from the reaction space 25 through the inner support structure 17 in the inner cavity 22 and then step through the neck 4 from the converter. During the reaction, it is necessary for their normal course, from the reaction space 25 Dissipate heat. That's through the heat panels 8th guaranteed, which correspond in their nature "heat pipes" and contain a heat transfer medium, which evaporates by the supply of heat. Ie. the lower, wedge-shaped part of each heat panel 8th removes heat from the reaction zone in the catalyst bed 16 and guides them to the heat exchange devices 19 in the upper part 2 to the body. In the heat exchange device 19 then the heat is transferred to a heat exchange medium. The heat transfer condenses again and flows into the lower part of the heat panels 8th back. The heat exchange medium evaporates by the supplied heat energy and is then through the outlet pipe for the evaporated heat exchange medium 13 dissipated and used for other processes.

In 3 is an enlarged sectional view of the lower part of a heat panel 8th shown. The heat panels 8th has tubes inside 26 for the removal of the vaporized heat carrier. In the heat exchange device 9 This condenses again and then runs on the inner walls of the heat panel 8th back down. Furthermore, the heat panels 8th inside horizontal bracing 27 which mechanically stabilize the heat panels and the mechanical strength of the heat panels 8th at high pressures in the reaction space 25 guarantee.

In 4 Figure 3 shows the vertical section of a heat panel and a heat exchange device operatively connected to the heat panel. The heat panels consists of the lower cylindrical hollow body with wedge-shaped base 28 , on whose lid a vertical tube 29 is attached. Cylindrical hollow body 28 and vertical pipe 29 form a body with a uniform interior. This space is closed to the outside and contains in the cylindrical hollow body 28 Internals. Inside the body, consisting of cylindrical hollow body 28 and vertical tube 29 , is the heat carrier, which absorbs the released during the exothermic catalytic reaction heat. In this case, the liquid heat carrier evaporates and rises in a gas upward into the vertical tube 29 , Around the top of this vertical tube 29 is a jacket pipe 30 attached, which is part of the heat exchange device 9 is. In the jacket tube 30 is the heat exchange medium, which removes the heat from the heat carrier, which cools and condenses. The condensate of the heat carrier flows on the inner walls of the vertical tube 29 down into the cylindrical hollow body 28 of the heat panel 8th , where it is forced down by internals to drain on the inner walls. Subsequently, the heat carrier evaporates again and the process of evaporation and condensation of the heat carrier by heat absorption and heat dissipation is repeated, so that the heat carrier always in the circuit between the lower part of the heat panel 8th - The cylindrical hollow body 28 - and upper part of the heat panel 8th - the vertical pipe 29 - is located. The system is closed. The heat carrier remains inside the heat panel 8th ,

Exemplary Embodiment 1 Application of the Converter for the Methanol Synthesis

The synthesis of methanol is realized from synthesis gas (CO + H ₂ + H ₂ O + CO ₂ + Inerte) at a pressure of 30 to 70 bar and a temperature of 220 ° C to 290 ° C.

The catalyst used is a copper-containing catalyst which is customarily used for methanol synthesis. The amount of catalyst used is 0.45 m ³ .

In the converter 24 heat panels are used as they are in 2 are shown.

Each heat panel has a zone of dissipation of the heat of reaction at the bottom. As a heat carrier n-dodecane is used here. In the upper area, each heat panel has a cooling zone connected to the heat exchange device. As a heat exchange medium here water of a temperature near boiling point is used. The heat of reaction is dissipated by the water vapor formed and used for other processes. The achieved steam pressure is 16 bar.

The temperature difference between the temperature in the reaction zone and the temperature of the heat carrier in the reaction zone is <40 ° C.

The total heat exchange area of all heat panels in the reaction zone (ie, the heat exchange area between the catalyst bed and the heat carrier in the heat panels) is 33 m ² .

The ratio of the heat exchange surface in the reaction zone to the catalyst volume is 60 m ² / m ³ .

The heat exchange surface in the reaction zone (i.e., the catalyst contact area) is coated with a layer of 0.2 mm of alumina and enamel having a thickness of 0.3 mm.

The heat exchange area in the area of the heat exchange device is 5.5 m ² . This corresponds to the possible contact surface with the heat exchange medium. By the level of the heat exchange medium, the amount of heat dissipated and thus the temperature in the reaction space of the converter can be adjusted.

Each heat panel has its own heat exchange device where steam is generated. The heat exchange devices are each arranged as a vertical tube with jacket tube in the upper region of the heat panels. All heat exchange devices are by a common collector for feed water, a collector for evaporated heat exchange medium and a rinse water collector with subsequent discharge of the rinse water through the Spülwasseraustrittsstutzen (s. 1 ) connected with each other.

The pressure inside the heat panel is up to 4 bar. The fixing of the heat panels serve partitions with notches of a diameter of 30 mm. The partitions are mounted vertically every 52 mm. The body has a diameter of 2 m and 3 m height.

Embodiment 2 Application of the converter for producing synthetic gasoline from crude methanol:

The synthesis is carried out at a pressure of 7-50 bar and a temperature in a range between 280 ° C to 420 ° C. In the example, the reaction of the synthesis of gasoline from crude methanol at a pressure of 7 bar and a temperature of 380 ° C and at a pressure of 48 bar and a temperature of 380 ° C is performed.

The catalyst used is a zeolite-containing catalyst, which is usually used for methanol gasoline production. The amount of catalyst used is 0.45 t.

In the converter 24 types elements are arranged, which in 2 are shown.

Each heat panel has a zone of dissipation of the heat of reaction at the bottom. The heat transfer medium used here is sulfur with added iodine. In the upper area, each heat panel has a cooling zone connected to the heat exchange device. As a heat exchange agent here water is used. The heat of reaction is dissipated by the water vapor formed and used for other processes. The achieved steam pressure is 64 bar.

The temperature difference between the temperature in the reaction zone and the temperature of the heat carrier in the reaction zone is <30 ° C.

The total heat exchange area of all heat panels in the zone of heat of reaction dissipation (ie, the catalyst contact area in the reaction zone) is 33 m ² . The ratio of heat exchange surface (contact surface to the catalyst) to the catalyst volume is again 60 m ² / m ³ .

The heat exchange area in the area of the heat exchange device is 5.1 m ² .

Otherwise, the converter, as described in Example 1, constructed.

The structure of the converter according to the invention makes it possible to set an optimum ratio of the surface of the heat panels to the volume of the catalyst, whereby a nearly isothermal temperature control is ensured with the necessary temperature stability in the catalyst.

LIST OF REFERENCE NUMBERS

1

lower part of the body

2

upper part of the body

3

Infeed for feeding the starting components

4

Procedure for the derivation of the reaction products

5

connecting flange

6

connecting flange

7

baseplate

8th

heat panels

9

Heat exchange device

10

Feed for the heat exchange medium

11

Collector for heat exchange medium

12

Collector for evaporated heat exchange medium

13

Outlet for the evaporated heat exchange medium

14

Spülwasserkollektor

15

Spülwasseraustrittsstutzen

16

catalyst bed

17

inner support structure (inner central tube)

18

poetry

19

Nozzle for the temperature measuring device

20

Temperature measuring device

21

central axis

22

inner cavity

23

outer cavity

24

outer support structure

25

reaction chamber

26

Tubes for vaporized heat transfer media

27

horizontal bracing

28

lower part of the heat panels (cylindrical hollow body with wedge-shaped base)

29

Upper part of the heat panels (vertical pipe)

30

Casing pipe (as part of the heat exchange device)

31

catalyst table

Claims (13)

Converter for carrying out exothermic catalytic reactions with a body ( 1 . 2 ) with at least one inlet ( 3 ) for the supply of the starting components and at least one process ( 4 ) for the derivation of the reaction products, wherein in the lower part ( 2 ) of the carcass a reaction space ( 25 ), which is of an inner support structure ( 17 ) and an outer support structure ( 24 ) is limited, wherein in the reaction space ( 25 ) several heat panels ( 8th ) are arranged, wherein within the inner support structure ( 17 ) an inner cavity ( 22 ), wherein the feed ( 3 ) is arranged so that the starting components through the outer support structure ( 24 ) in the reaction space ( 25 ), and the process ( 4 ) with the inner cavity ( 22 ), the lower part ( 28 ) of each heat panel ( 8th ) in the lower part ( 2 ) of the carcass is designed as a hollow body with wedge-shaped base surface, wherein in each case the pointed part to the central axis ( 21 ) of the carcass and wherein the upper part ( 29 ) of each heat panel ( 8th ) from the reaction space ( 25 ) in the upper part ( 2 ) of the carcass and there with a heat exchange device ( 9 ) is in operative connection, wherein the upper part ( 29 ) of each heat panel ( 8th ) each with the lower part ( 28 ) of the heat panel ( 8th ), so that in the lower part ( 28 ) vaporized heat transfer medium in the upper part ( 29 ) and condensed heat carrier from the upper part ( 29 ) can flow back into the lower part, wherein the heat panels ( 8th ) are constructed in their interior so that the refluxing heat carrier flows along the inner wall of the heat panels and wherein the heat panels ( 8th ) in the lower part ( 28 ) horizontal installations ( 27 ), over which the returning heat transfer medium is distributed. Converter according to claim 1, characterized in that between the heat panels ( 8th ) Catalyst ( 16 ) is filled. Converter according to claim 1 or 2, characterized in that the heat panels ( 8th ) and the catalyst ( 16 ) in the lower part ( 1 ) of the body together form a hollow cylinder (preferably a straight hollow cylinder with preferably circular base). Converter according to one of claims 1 to 3, characterized in that the ratio of the heat exchange surface in the reaction space ( 25 ) to the catalyst volume is 10 to 250 m ² / m ³ . Converter according to one of claims 1 to 4, characterized in that in addition between the heat panels ( 8th ) and inner support structure ( 17 ) and / or outer support structure ( 24 ) Catalyst ( 16 ) is filled. Converter according to one of claims 1 to 5, characterized in that the catalyst volume which is located between the edge of the heat panels ( 8th ) and the outer support structure ( 24 ) is less than 15% of the total catalyst volume. Converter according to one of Claims 1 to 6, characterized in that the volume of the catalyst ( 16 ), which extends between the inner support structure ( 17 ) and the heat panels ( 8th ), not 30% of the total volume of the catalyst ( 16 ) exceeds. Converter according to one of claims 1 to 7, characterized in that the inner support structure ( 17 ) is formed from a perforated vessel, on the surface of a network is applied. Converter according to one of Claims 1 to 8, characterized in that the lower part ( 2 ) and the upper part ( 1 ) of the carcass by flanges ( 5 . 6 ) are connected. Converter according to one of claims 1 to 9, characterized in that the reaction space ( 25 ) and the inner cavity ( 22 ) upwards through a seal ( 18 ) Are completed. Converter according to one of claims 1 to 10, characterized in that it additionally temperature measuring devices ( 20 ) contained in the catalyst bed between the heat panels. Use of a converter according to one of claims 1 to 11 for carrying out chemical, catalytic reactions in the gas phase, in particular in the chemical and petroleum chemical industries. Use of a heat panel ( 8th ) which is hollow inside and has the following components: a.) a lower part ( 28 ), which as a hollow body with wedge-shaped base ( 28 ) is formed, whose lateral surfaces are formed as heat exchange surfaces, b.) an upper part ( 29 ), which is formed as a tube and with a heat exchange device ( 9 ) is in operative connection or can be brought into operative connection, wherein the tube of the upper part ( 29 ) with the upper base of the lower part ( 28 ), so that in the lower part ( 28 ) vaporized heat carrier can rise into the tube and condensed heat transfer medium from the tube into the lower part ( 28 ), whereby the heat panel ( 8th ) is constructed in its interior so that the refluxing heat carrier flows along the inner wall of the heat panel and wherein the heat panel ( 8th ) in the lower part ( 28 ) horizontal installations ( 27 ), via which the refluxing heat transfer medium is distributed, for a converter according to one of the preceding claims.

Images