KR100591704B1 - Process for producing gaseous product by catalytic gas phase reaction and apparatus for carrying out the process - Google Patents

Abstract

In the method and apparatus of the present invention, in the heating stage (HST), the compressed air (9) preheated and filled with the use material, such as o-xylene or naphthalene, comprises one heating unit (11) in the reactor housing (2). The catalyst body is first heated in a number of successive oxidation stages (I-V) with a catalyst body (15, 27, 29, 31, 33) and a cooling unit (21, 28, 30, 32) after heating to the starting temperature. And then through the cooling units 21, 28, 30, 32. Finally, the reaction gas 10 filled with PAA is supplied for desublimation from the reactor housing 2.

Description

FIELD OF THE INVENTION A method for producing a gaseous product by catalytic gas phase reaction and an apparatus for performing the method.

1 is a schematic vertical longitudinal sectional view of a reactor for oxidizing PAA from an air / use material-mixture.

FIG. 2 is a diagram showing the temperature variation of the mixture / reactant gas flowing through the reactor in relation to the reactor of FIG.

3 and 4 are enlarged views of the oxidation step of the reactor of FIG. 1 with catalyst body and cooling unit.

5 shows an enlarged view of another embodiment of the oxidation step of the reactor according to FIG. 1;

* Description of the symbols for the main parts of the drawings *

1: reactor 2: reactor housing

3: inlet cap 4: outlet cap

5: longitudinal section 6: pipe

7: explosion opening 8: explosion safety measures

9: mixture 10: reaction gas

11: heating unit

12, 17, 22, 38: frame plate

13, 14, 24, 25: connection

15, 27, 29, 31, 33, 35: catalyst

16, 37: frames 18, 23, 39: openings

19: wall

20, 26, 40-47: temperature measuring point

21, 28, 30, 32, 36: cooling unit

34: free field

The present invention relates to a method for producing a gaseous product by catalytic gas phase reaction and an apparatus for carrying out the method.

Products such as, for example, phthalic anhydride (PAA) are obtained by the intended partial oxidation of o-xylene or naphthalene or a mixture of the two used materials. The necessary oxygen is obtained from air, which is used simultaneously as a carrier gas. In today's typical device sizes, the amount of air preheated to about 180 ° C., suctioned and compressed, is between 20,000 and 100,000 Nm 3 / h. The materials of use are sprayed, vaporized or mixed in vapor form into a hot air stream preheated in front of the reactor.

Known reactors consist of pipe reactors. In the reactor, a mixture of air and used material is oxidized to PAA in the catalyst body. In this case, water, CO, CO ₂ , maleic anhydride, phthalide and the like are produced as undesirable by-products for PAA. The reaction is a strong exothermic reaction. Most of the heat generated in known pipe reactors is discharged to the outside via a liquid salt bath. The remainder of the heat is heated to about 380 ° C. and discharged in the form of reaction gas filled with PAA. This reaction gas is cooled to about 170 ° C. in a heat exchanger after exiting the reactor and then fed to the separator. PAA is obtained by desublimation in the separator.

Known pipe reactors have multiple exchanger pipes (about 5,000 to 25,000) between the upper gas inlet cap and the lower gas outlet cap. The exchanger pipe is filled with catalyst body over almost the entire length before the initial operation of the pipe reactor. To this end, inherent active catalyst materials are generally provided on ring or spherical ceramic supports.

At the top of the exchanger pipe, a mixture of air and used material, which is introduced into the pipe reactor, is heated to the reaction temperature through the hot exchanger pipe. Thereafter, oxidation occurs through a number of intermediate products to the desired product (PAA) and the undesirable byproducts described above. During this oxidation, the temperature in the exchanger pipe rises to a so-called "hot spot" and then drops back to the lower end of the exchanger pipe to approximately the temperature of the liquid salt bath surrounding the exchanger pipe. Reactant gas filled with PAA leaves the pipe reactor through a gas discharge cap located underneath.

In order to prevent excessive oxidation, which is undesirable in hot places and insufficient oxidation in cold places, the liquid salt bath cooling the exchanger pipe and reactor housing must be continuously repumped in a relatively complex manner and guided uniformly around all exchanger pipes. For this reason, the liquid salt bath can only have a very low temperature difference of about 3 °.

The heat received by the salt bath is discharged in the form of high pressure steam in the salt bath cooler outside of the reactor housing.

Since the mixture of air and used material and the reactant gas filled with PAA are explosive over the entire temperature range, the reactor housing must be protected by large and sensitive explosion safety measures in several places.

Since the pipe reactor is actually cooled by liquid salt of the same temperature, the best reaction temperature cannot be set in the prior art. Rather, depending on the catalyst, a typical temperature profile over the length of the pipe is formed, having a "hot spot" at about 40% of the length of the pipe. As a result, undesirable byproducts, excessive oxidation and very limited lifetimes of the catalyst are given.

To at least partly avoid this drawback, a pipe reactor with two rows of connected pipe reactors or a pipe reactor with two reaction zones and a separate salt bath cooling device is known (European patent applications 0 686 633 A1 and 0 453 951). A1). However, since the construction, manufacture and operation of such a pipe reactor is very complicated, it has not been practical to date. It is also technically very difficult to equally cool all the exchanger pipes in the reactor housing. As such, it can not be ruled out that a partially different reaction takes place in the thousands of exchanger pipes if known.

Another problem is filling the exchanger pipe with catalytic material. Since each exchanger pipe obtains the same amount of catalytic material and has the same pressure loss on the gas side, the filling must be done with extreme care. Thus, the costs for charging and testing (about 3-4 weeks) are very high and uneconomical.

In addition, as air in the pipe reactors is increasingly filled with the materials of use, it becomes more difficult and complicated to discharge the heat generated through the salt bath. This is because the heat of reaction increases proportionally as the air is filled with PAA.

In addition, high pressure losses on the air side and thus high ventilation costs are inevitable.

There is also a risk of leakage of the salt bath. In addition, known pipe reactors require long heating and cooling steps. In addition, inspection of pipe reactors involves a series of problems.

As mentioned above, if an undesirable by-product is increased, it must be complicated to remove by distillation. Therefore, in practice, a separate post-reactor is connected after the main reactor. In the post reactor some of the by-products are combusted and very little is converted to PAA. In general, the reactant gas from the main reactor is precooled in an intermediate cooler before entering the post reactor (DE 198 07 018 A1).

It is an object of the present invention to carry out and to produce a gaseous product by catalytic gas phase reaction, which is simple in terms of manufacturing technology and in operating technology, in which a high yield of product can be obtained with low by-products and high safety at the same time. It is to provide a device for.

This object with respect to the method is achieved by the features of claim 1.

According to the invention the whole reaction is subdivided into a number of stages in one reactor housing. First, the gas, which is preheated and filled with the used material, which enters the reactor housing, is heated to the best starting temperature in one heating stage. Following the heating stage, the gas is guided through the catalytic material in the first reaction stage. The first partial reaction takes place in the catalyst material. Then, the reaction gas partially filled with the product is cooled in the reaction step. That is, cooled to a temperature that ensures the best second partial reaction when flowing through the next catalytic material.

The number of reaction stages through which the reaction gas, increasingly filled with the product, can be 5 to 8 in practical operation. The contact time of the reactant gas and the catalyst material in the individual reaction stages may be the same or different. In addition, the number of reaction steps may vary in terms of catalyst and cooling, i.e., depending on the material used, the concentration of charge or the type of catalyst material used.

After the end of the reaction, the reaction gas filled with product is withdrawn from the reactor housing and supplied for cooling and subsequent desublimation or condensation.

The flow direction of the fill gas or the reactant gas in the reactor housing can be arbitrary. In particular, the flow direction is vertical or horizontal.

An important advantage of the present invention is that the liquid salt bath is omitted entirely. There is therefore no risk of spontaneous reaction and explosion of the salt and organic components of the reaction gas by leakage.

An important advantage of the present invention is that the yield of the product increases by several percent. This is because the amount of catalyst material controlled for each reaction step forms less by-products and more product at the best reaction temperature. Less by-products mean at the same time simpler distillation of the crude product and thus less investment and operating costs.

The amount of gas supplied to the reactor and the filling of the materials used may vary with wide limits because the catalytic material can be best used.

The multistage reaction according to the invention has the advantage of being more flexible than oxidation in a pipe reactor. Pipe reactors can only work best at one point. The cause lies in the salt bath temperature, which affects filling and yield. Also, once fixed catalyst body combinations cannot be varied. In contrast, the present invention always ensures the best operation in the individual reaction steps.

In the scope of the process according to the invention, for example, catalytic oxidation of anthragen to anthraquinone is addressed.

A particularly preferred embodiment of the method according to the invention is presented in the features of claim 2. Getting a PAA is covered here.

In this case too, the preheated and filled compressed air which is introduced into the reactor housing is heated to the best starting temperature in one heating step. Following the heating step, air filled with the use material is guided through the catalytic material in the first oxidation step. A first partial oxidation takes place in the catalyst material. Then, the reaction gas partially filled with PAA is cooled in the oxidation step. That is, it is cooled to a temperature that ensures the best second partial oxidation upon passage of the next catalytic material.

The number of oxidation stages through which the reactant gas increasingly filled with PAA can be 5-8 in practical operation. The contact time of the reactant gas and the catalyst material in the individual oxidation stages may be the same or different. In addition, the number of oxidation stages may vary in terms of catalyst body and cooling, i.e., depending on the material used, the concentration of charge or the kind of catalyst material used.

After the end of the oxidation, the reaction gas filled with PAA is withdrawn from the reactor housing and supplied for cooling and subsequent desublimation.

For example, in order to always keep out of the explosive limits of the air / usable material-mixture, in accordance with the features of claim 3 the additional use materials are alternately characterized in the reactor housing in a way characterized by partial oxidation and subsequent cooling in the catalytic material. It can be fed into the reaction gas filled with PAA. The place of supply is preferably centered approximately in the flow path of the reactant gas in the reactor housing.

In order to prevent precipitation of the used material and / or PAA in the cold part of the reactor housing and to shorten the heating time at the start of the reactor, the reactor housing and the catalyst material can be heated before starting the reactor according to claim 4. This can be done by steam. However, oil or current may be used. If steam is used, the steam should have as high a pressure as possible. In this case, it is preferred that the high active catalyst material is provided in the first oxidation step after the heating step, so that the temperature required during starting is obtained by the heat of reaction. Using oil has the advantage of easy temperature control. In addition, heating oil may be used for distillation. In that case, only one common starting burner is provided for oil circulation.

Another preferred feature of the invention is set out in the feature of claim 5. Thus, the heat generated during cooling can be used to heat the air filled with the material used in the heating step. In this case, internal heat transfer takes place. For this purpose, suitable heat transfer oils are preferred.

The object of the invention with respect to the device is achieved by the features of claim 6.

According to this feature, a reactor housing having the same cross section in the direction of flow of preheated and filled gas, in particular air, is provided. The air filled with the used material first reaches the heating unit of the heating stage, where the air is heated to the best starting temperature. The heating unit can also be formed to act as a rectifier by its resistance. Thereby, the catalyst body of the first reaction stage, in particular of the oxidation stage, connected immediately after the heating unit, has an almost uniform air velocity and temperature over the entire cross section. This is also preferred for subsequent reaction steps.

In a number of reaction steps the catalyst body is alternately provided to the heating unit for partial reactions, in particular partial oxidation of the product, especially PAA, and to the cooling unit for cooling the reaction gas to the best reaction temperature of the subsequent catalyst body. The length of the various catalyst bodies may be the same or different.

According to claim 7, the inlet cross sections of the heating unit, the catalyst body and the cooling unit are designed to be the same size. Thus, a simple configuration of the catalyst body and the cooling unit is achieved, with a uniform gas velocity in all regions of the reactor housing, which is preferred for catalytic partial reactions, in particular partial oxidation.

Particularly preferred embodiments of the present invention are presented in the features of claim 8. According to this, the heating unit, the catalyst body and the cooling unit are formed in a modular manner and are replaceably integrated in the reactor housing. This modular design allows the catalyst body and the cooling unit to be embedded into a frame aligned with the cross section of the reactor housing, so that the same inlet cross section can be obtained for the catalyst body and the cooling unit. This involves a uniform gas velocity with a simple configuration.

The modular design allows the catalyst body, the cooling unit and the heating unit to be individually inserted through the frame into the reactor housing, so that the individual frames can be separated from the reactor housing and reinserted. Therefore, the management, washing and replacement of the catalyst material can be made very quickly. In addition, the modular design allows the module comprising the cooling unit to be replaced by a module with a catalyst body and vice versa at a later point in time when technical development takes place. In addition, a free field can be provided for later expansion or retrofitting in an economical manner. It is also possible to economically provide individual modules with catalyst bodies and / or cooling units so that replacements can be carried out in a short time if necessary within the scope of the invention.

In the present invention, it is also possible to embed each catalyst body and each cooling unit into one frame and treat them as modules. According to claim 9, it is also possible to integrate the catalyst body and the cooling unit as a replaceable module by placing them in one frame in common. This reduces the required place, which entails shortening of the reactor housing and material savings.

It is not important in the present invention how the heating unit or cooling unit is formed, i.e. whether a heat exchanger with a plain end pipe or a heat exchanger with another suitable heat transfer surface is used, but according to the preferred embodiment of claim 10 The unit and the cooling unit are formed with a rib pipe-heat exchanger.

In accordance with the features of claim 11 a ring, ball or similar support provided with a catalytic material may be used as catalyst body.

Honey combs can be used according to claim 12, which has the added advantage of being able to be detached very quickly as a module.

The heat necessary for the additional preheating of the gas / use material-mixture in the heating unit can be withdrawn from at least one cooling unit which dissipates heat, which is arranged in a subsequent reaction step, in particular an oxidation step, according to claim 13. In this case, internal heat transfer takes place. For this purpose, suitable heat transfer oils can be used, for example with the advantage of simple temperature control. The hot heat transfer oil can also be used for heating during distillation. For this purpose, only one common oil circulation system with one common starting burner is required.

In the case of an explosion, explosion openings are provided at various places in the reactor housing, which are suitable for this according to claim 14, in order to avoid high pressure in the reactor housing. The size of the opening depends on the mixture composition, the temperature and the volume to be reduced. The explosion opening can be used as a manhole for the inspection, care and cleaning of the reactor housing at the same time by the removal of the inherent explosion safety means.

In order to ensure that the reactor housing is not unnecessarily enlarged by the explosion openings and to keep as little as possible the volume to be reduced, it is preferred that the explosion openings are arranged directly in the catalyst body according to claim 15. The explosion opening with explosion safety means preferably forms part of the frame with the catalyst body, which can be integrated into the reactor housing.

The reactor housing can be heated according to claim 16. This is particularly desirable to prevent the use material or product from settling in the cold housing part by shortening the heating time during starting. For this purpose, steam, oil or current can be used. For example, a heating pipe may be provided on the outer surface of the reactor housing, which may be provided with a suitable heat transfer medium.

Hereinafter, with reference to the embodiment shown in the accompanying drawings the present invention will be described in detail.

1 shows a reactor 1 which is part of an apparatus for obtaining phthalic anhydride (PAA), which is not shown in detail. The reactor 1 comprises an elongated reactor housing 2 having the same cross section across the remaining longitudinal section 5 except the inlet cap 3 and the outlet cap 4. Pipes 6 are mounted on the outer surface of the inlet cap 3, the outlet cap 4 and the longitudinal section 5 lying therebetween. The pipe 6 may be supplied with a suitable heat transfer medium such as oil.

In addition, as shown in FIG. 1, an explosion opening with explosion safety means 8 on the wall of the reactor housing 2 in the inlet cap 3, the discharge cap 4 and the longitudinal section 5 interposed therebetween. (7) is formed.

The reactor housing 2 is a mixture 9 composed of air introduced through the inlet cap 3 and the use material, such as o-xylene, and the reaction gas filled with PAA, which exits the reactor housing via the outlet cap 4 ( A heating unit 11 for heating the mixture 9 in the heating stage HST near the inlet cap 3 in the flow direction of 10). The heating unit 11 is formed in a ribbed heat exchanger which is formed in a modular manner and which can be inserted into a frame not shown in detail. The frame is detachably fixed around the opening 12a of the reactor housing 2 by the frame plate 12. Connections for the supply and discharge of heating medium to the heating unit 11 are shown by 13 and 14.

In the flow direction of the mixture 9, the catalyst body 15 is connected to the first oxidation stage I after the heating unit 11 at intervals. Catalyst body 15 comprises a catalytic material applied on a ring, ball, honey comb, or similar support. The catalytic material is filled in the catalyst body 15 embedded in the frame 16 (see FIG. 3). Thus, the catalyst body 15 is formed in a modular manner and is fixed around the opening 18 in the wall 19 of the reactor housing 2 by the frame plate 17.

The temperature measuring point 20 is disposed between the heating unit 11 and the catalyst body 15.

In the first oxidation stage I, the cooling unit 21 is detachably integrated in the reactor housing 2 at intervals from the catalyst body 15 (see FIG. 4). The cooling unit 21 consists of a rib pipe heat exchanger. The cooling unit 21 is fixed in a modular manner around the opening 23 provided in the wall 19 of the reactor housing 2 by the frame plate 22. Connections for the supply and discharge of cooling medium are shown at 24 and 25.

A second temperature measuring point 26 is provided between the catalyst body 15 and the cooling unit 21.

As shown in FIG. 1, the catalyst body 27 and the cooling unit 28 are subjected to the second oxidation step II step by step after the first oxidation step I having the catalyst body 15 and the cooling unit 21. ), The catalyst body 29 and the cooling unit 30 in the third oxidation stage (III), the catalyst body 31 and the cooling unit 32 in the fourth oxidation stage (IV), and the fifth oxidation stage. (V) is provided with a catalyst body 33 and a free field 34. The catalyst bodies 27, 29, 31 and 33 and the cooling units 28, 30 and 32 formed in a modular manner are attached to the frame plates 17, 22 according to FIG. It is thereby detachably fixed around the openings 18, 23 in the wall 19 of the reactor housing 2. Of course, the lengths of the catalyst bodies 15, 27, 29, 31, and 33 placed in the flow direction are formed differently. In an embodiment, the catalyst materials of catalyst bodies 15, 27, 29, 31 and 33 are formed identically. The cooling units 28, 30 and 32 are formed as rib pipe heat exchangers similarly to the cooling unit 21 and have connections 24 and 25 to the heating medium.

In addition, as shown in FIG. 3, between the catalyst bodies 27 and 31 and the cooling units 21, 28 and 32 connected thereto in the wall 19 of the reactor housing 2. Instead of the explosive openings 7 in which such explosive openings 7 can be arranged directly on the catalyst bodies 15, 27, 29, 31 and 33 as indicated by the broken lines. In this case, the explosion opening 7 is arranged in the frame plate 17.

1, 3 and 4, the catalyst bodies 15, 27, 29, 31 and 33 and the cooling units 21, 28, 30 and 32 are spaced at a constant interval from each other. While the catalyst body 35 and the cooling unit 36 are modularized as an oxidation step VI in a single frame 37 in FIG. 5, while being arranged in turn and detachably integrated in the reactor housing 2. It is supported and fixed around the opening 39 provided in the wall 19 of the reactor housing 2 by the frame plate 38. Thus, the catalyst body 35 and the cooling unit 36 can be taken out of the reactor housing 2 together and integrated again.

1 and 2 together, fluctuations in gas temperature appear from when the mixture 9 is introduced into the inlet cap 3 until the reaction gas 10 is discharged through the discharge cap 4.

The mixture 9 is introduced into the reactor housing 2 at a temperature of about 180 ° C. When passing through the heating unit 11 the mixture 9 is brought to a temperature of about 270 ° C. Since this temperature is sufficient as the starting temperature, the best partial oxidation can be achieved at about 380 ° C. in the catalyst body 15 of the subsequent first oxidation step (I).

The reaction gas, now partially filled with PAA, now flows through the cooling unit 21 of the first oxidation stage I, where it is recooled to about 300 ° C. This results in a temperature which again ensures the best partial oxidation in the catalyst body of the subsequent second oxidation step (II).

The temperature fluctuations according to FIG. 2 are characterized in that the respective cooling units 28, 30 and 32 connected after the catalyst bodies 27, 29 and 31 are the next catalyst bodies 29, 31. ) And (32) are again provided to ensure the best partial oxidation, and finally indicate that the reaction gas 10 filled with PAA is discharged from the discharge cap 4 at a temperature of about 380 ° C.

A third oxidation step (i) between the first oxidation step (I) and the second oxidation step (II), between the second oxidation step (II) and the third oxidation step (III), Between the third and fourth oxidation stages (IV), between the third and fourth oxidation stages (IV), between the third and fourth oxidation stages (IV), and The temperature measurement point following the fifth oxidation step (V) is represented by (40)-(47).

1 also shows the inlet cross section for catalyst bodies 15, 27, 29, 31 and 33 and the inlet to cooling units 21, 28, 30 and 32. Indicates that the cross sections are identical. As a result, the frame 16 is given the same design and a very simple modular configuration, thus providing partial oxidation by the catalyst in the catalyst materials in the catalyst bodies 15, 27, 29, 31 and 33. There is a uniform speed.

The same property applies when the oxidation step (VI) according to FIG. 5 is used.

The method and apparatus according to the invention are simple in manufacturing technology and in operating technology, and provide high yields of products with low by-products and high safety.

Claims (16)

In a method for producing gaseous phthalic anhydride (PAA) by catalytic gas phase reaction of o-xylene, naphthalene or mixtures thereof, the preheated and filled gas with o-xylene, naphthalene or mixtures thereof is contained in the reactor housing. In the heating stage of is heated to the starting temperature, and then concentrated through the catalyst material first concentrated through phthalic anhydride in a plurality of successive reaction stages and then cooled, and then the reaction gas filled with phthalic anhydride is removed from the reactor housing Process for producing phthalic anhydride, characterized in that it is supplied for sublimation or condensation. The compressed air (9) according to claim 1, which is preheated and filled with o-xylene, naphthalene or mixtures thereof to obtain phthalic anhydride (PAA) by catalytic gas phase oxidation of o-xylene, naphthalene or mixtures thereof. Is heated to the starting temperature in one heating stage (HST) in the reactor housing (2) and then first guided through the catalytic material while concentrating to PAA in a plurality of successive oxidation stages (I-VI), and then cooling And then a reaction gas (10) filled with PAA is supplied for desublimation from the reactor housing (2). The additional o-xylene, naphthalene or mixtures thereof is fed into the reaction gas filled with PAA in a manner characterized by alternating partial oxidation in the catalytic material and subsequent cooling in the reactor housing (2). Characterized in that the method. The process according to claim 2 or 3, characterized in that the reactor housing (2) and the catalytic material are heated prior to the start of the reactor (1). 4. Process according to claim 2 or 3, characterized in that the heat generated during cooling is used for heating the air (9) filled with o-xylene, naphthalene or mixtures thereof in the heating stage (HST). Apparatus for carrying out the method according to any one of claims 1 to 3, characterized in that the reactor housing has the same cross section in the flow direction of the gas (9) preheated and filled with o-xylene, naphthalene or mixtures thereof. 2) a heating unit 11 for heating the gas 9 to the best starting temperature first, followed by a plurality of catalyst bodies 15, 27, 29, 31, 33, 35 for the partial reaction of phthalic anhydride in turn. ) And a cooling unit 21, 28, 30, 32, 36 for cooling the reaction gas 10 filled with phthalic anhydride to the best reaction temperature of the subsequent catalyst bodies 27, 29, 31, 33, 35. Apparatus characterized in that connected in sequence step by step. The inlet cross section of the heating unit 11, the catalyst bodies 15, 27, 29, 31, 33, 35 and the cooling units 21, 28, 30, 32, 36 are of equal size. Device characterized in that. The heating unit (11), the catalyst bodies (15, 27, 29, 31, 33, 35) and the cooling units (21, 28, 30, 32, 36) are formed in a modular manner and are replaceable. Device integrated into the reactor housing (2). 7. The device according to claim 6, characterized in that the catalyst body (35) and the cooling unit (36) connected after it are joined in a replaceable cavity module. Device according to claim 6, characterized in that the heating unit (11) and the cooling unit (21, 28, 30, 32, 36) are formed with a rib pipe-heat exchanger. 7. A device according to claim 6, wherein a ring, sphere or similar support provided with the catalyst material is used for the catalyst body (15, 27, 29, 31, 33). 7. An apparatus according to claim 6, wherein a honeycomb provided with a catalytic material is used for the catalyst body (15, 27, 29, 31, 33). Device according to claim 6, characterized in that the heating unit (11) is heat exchangeably coupled with at least one cooling unit (21, 28, 30, 32, 36). Device according to claim 6, characterized in that the reactor housing (2) has an explosion opening (7) with explosion safety means (8). 15. The device according to claim 14, wherein the explosion opening (7) is arranged in the catalyst body (15, 27, 29, 31, 33). Device according to claim 6, characterized in that the reactor housing (2) can be heated.

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