EP2217685A1

EP2217685A1 - Method for desulfurizing ingredient materials containing olefin

Info

Publication number: EP2217685A1
Application number: EP08857251A
Authority: EP
Inventors: Thilo Von Trotha; Frank Urner
Original assignee: Uhde GmbH
Current assignee: ThyssenKrupp Industrial Solutions AG
Priority date: 2007-12-07
Filing date: 2008-11-18
Publication date: 2010-08-18
Also published as: MX2010006156A; US20100294697A1; CA2706003A1; BRPI0821022A2; WO2009071180A1; CO6300872A2; EA201070650A1; EA016478B1; CN101932676A; DE102007059243A1; ZA201003387B

Abstract

The invention relates to a method and a device for conducting the method for desulfurizing an ingredient gas containing olefin and hydrogen. Said gas may be mixed with additional hydrogen and is divided into at least two supply flows. The first supply flow is conducted separately into the reactor and arrives on a first catalyst bed comprising the catalyst pellets on a suitable retaining device or a grating. There, the supply stream is heated by the hydration reaction. After the first catalyst bed, additional ingredient gas is added, whereby the reaction gas is cooled and may therefore be conducted through a second catalyst bed. Additional catalyst beds and additional ingredient gas supply units may be provided after the second catalyst bed. The catalyst beds may be placed in the reactor in any desired number, type, and shape. By conducting the reaction in this manner, a product gas is obtained that substantially contains hydrosulfides only as a sulfur compound.

Description

Process for the desulfurization of olefin-containing starting materials

The invention relates to a process for the hydrogenation of olefin- and sulfur-containing material streams, such as occur frequently in oil refineries. By the process according to the invention, the sulfur compounds contained in these streams are completely or partially converted by hydrogenation into hydrogen sulfide and the olefins contained in these streams by hydrogenation in alkanes. The invention also relates to a device with which the method can be carried out and which is suitable for the implementation of said method steps.

In the refining of petroleum products, the products often contain sulfur-containing organic compounds that must be removed from the products. Almost all mineral oil products must meet specifications that require low sulfur content when used. This also applies to the gases obtained from petroleum refining. For the applications required, these gases usually have to be sulfur-free, since sulfur compounds are undesirable when used for heating or synthesis purposes.

Frequently occurring gases in refinery streams are light olefin gases, which essentially comprise ethenes, propenes or butenes. Examples include LPG (liquefied petroleum gas) or LPG. During the transfer via a hydrogenation catalyst, part of the olefins contained in the gas mixture and the organic sulfur compounds are hydrogenated with hydrogen likewise present in the gas, so that a gas mixture with an increased proportion of alkanes and hydrogen sulfide is obtained. Upon complete hydrogenation of the sulfur compounds, all organic sulfur compounds are converted to hydrogen sulfide. This can be completely removed from the gas mixture in a subsequent gas scrubbing, so as to obtain a sulfur-free feed gas. An equally common gas in refineries is hydrogen.

Many hydrodesulfurization processes for hydrocarbons are designed so that both liquids and gases can be desulphurized. The desulfurization of liquid hydrocarbon mixtures is well known and is carried out on an industrial scale. In modern petrol, the sulfur content may not exceed 150 mg / kg fuel to avoid acid sulfur emissions. The desulphurization problem is that you have to On the other hand, would like to lower the sulfur content of the product as much as possible, but on the other hand mithydrogenated in the hydrogenation and a large part of the olefins contained in the hydrocarbons. When using the hydrocarbons as fuel, olefins generally have a significantly higher knock resistance than simple alkanes. Since alkanes can be dehydrated again if necessary, one strives for a complete hydrogenation of the sulfur compounds, because the removal of sulfur for environmental reasons is a priority. The hydrogenation is therefore carried out with respect to the sulfur compounds with a stoichiometric excess of hydrogen. In order to bring the sulfur content of the fuels to the required value, several hydrodesulfurization stages are generally carried out in succession.

The desulfurization of gases is technically similar to the desulfurization of fuels. The desulphurisation of gases is also carried out in several successive stages. The existing hydrodesulphurisation processes can desulphurise olefin- and hydrogen-containing feed gases up to a few ppm residual sulfur content. The process of desulfurization is highly exothermic, especially in the presence of olefins, which is why the catalysts used often have low lives. The actual hydrogenation takes place in a fixed bed reactor, in which the gas is passed through so-called catalyst beds. These include a grate or a perforated bottom on which a supported, i. On a suitable inert solid applied catalyst is stored gas permeable. In contrast to fuels, a higher proportion of alkanes in gases after hydrogenation is less problematic.

WO 9829520 A1 describes a process for the hydrogenation of hydrocarbons, in particular for the removal of sulfur compounds in a multistage reactor. A mixture of liquid and gaseous hydrocarbons is reacted in a reactor with a hydrogen-containing reaction gas over a hydrogenation catalyst. In a subsequent process step, the liquid are separated from the gaseous reaction products and the liquid constituents are subjected to renewed hydrogenation. The complete separation of the gaseous reaction products from the hydrocarbon streams takes place in a stripping column. In the separation of the gaseous components and the resulting hydrogen sulfide is obtained, which can be removed by known methods such as a gas scrubber. The hydrogenation reaction can be carried out as often as desired, until the sulfur content of the hydrocarbons obtained corresponds to the specification. In the hydrogenating desulfurization of gases, the catalyst required for the hydrogenation heats up much more than in the hydrogenation of liquids. The dissipation of the heat of reaction is a problem because gases have a significantly lower heat capacity than liquids. For this reason, it is necessary to use several stages for the hydrogenation in succession in the desulfurization of gases or to dilute them with a reflux. Although the use of a large number of reaction stages can minimize the content of sulfur in the product gases as far as possible, it also means a considerable increase in plant outlay and thus high investment costs, a greater space requirement and higher operating costs, for example for the operation of the return.

It is therefore an object to find a method that allows hydrogenation of olefin-containing feed gases for desulfurization with reduced effort and still allows safe handling of the hydrogenation by a reliable discharge of the heat of reaction. The process should make it possible to carry out the desulphurisation to the desired sulfur content without safety risks. The method should make use of commercially available catalysts and get along without expensive devices for cooling as possible.

The invention achieves this object by a reactor which contains a plurality of catalyst beds and has a renewed feed gas feed behind each catalyst bed. The first part of a feed stream is passed over the head into a hydrogenation reactor. The hydrogenating reaction heats up the feed gas. As a result of the subsequent admixing of feed gas, the further gas stream is cooled down to the gas temperature required for renewed hydrogenation, and renewed hydrogenation takes place. The control of the feed quantity of the feed gas behind the catalyst beds is regulated by valves which are located behind the gas distributor for the feed devices. The hydrogenation of the sulfur compounds gives the product hydrogen sulfide, which can be removed in a downstream gas scrubber. The number of catalyst beds is chosen so that the sulfur content in the product gas can be brought to the required value.

[0010] By feeding the feed gas for hydrogenation according to the invention, the reaction can be controlled so that tight temperature limits can always be met and, on the other hand, in combination with a suitable process for removing the hydrogen sulfide, a desirably low sulfur content can be set. The reactor for carrying out the hydrogenation may be in one piece and does without further devices for cooling the product gas. If the catalyst is applied to suitable carriers, then the carriers can be applied, for example, to gratings or bubble-cap trays, which allow a low-pressure-flow passage of the reaction gases. A multi-stage arrangement of the catalyst beds in a reactor allows the implementation in a smaller number of reactors, which is an economic advantage in the use of terrain.

[0011] A process for the hydrodesulfurization of olefin-containing feedstocks with a hydrogen-containing feed gas is claimed, wherein

Passing an olefin-containing and hydrogen-containing feed mixture through a reactor containing a catalyst suitable for hydrogenating desulfurization, and

The organic sulfur compounds contained in the olefin-containing and hydrogen-containing feed mixture are wholly or partly hydrogenated to hydrogen sulphide, and

All or part of the olefins contained in the feed mixture are hydrogenated to alkanes,

and is characterized in that

• the olefin-containing feed stream is divided before the feed into the reactor, so as to obtain at least two feed streams, and

The first feed stream is passed through suitable means through a catalyst bed in the reactor with a subset of a catalyst suitable for hydrogenating desulfurization, the reactive feed mixture heating up, and

A second feed stream is added laterally behind the first catalyst bed into the reactor and to the reaction mixture heated by the first hydrogenation so that the reaction mixture cools to a reaction temperature suitable for further hydrogenating desulfurization by mixing with the second feed stream;

• the reaction mixture thus obtained is passed with the gas stream in the reactor through a further subset of a catalyst suitable for hydrogenating desulfurization, so as to obtain a hydrogenated useful gas, its sulfur compounds or olefin compounds or Sulfur compounds and olefin compounds have been partially or completely converted by hydrogenation in hydrogen sulfide or alkanes.

In order to preheat the feed gas to the operating temperature necessary for the reaction, the first subset of the feed stream, which is fed via the head into the reactor, be provided with suitable devices. These may be, for example, gas or oil fired burners. To make the operation of a plant economically favorable, a heat exchanger is preferably used, which uses the heat of the hot product gas at the end of the reactor for heating the Einsatzga- ses. To start up the reactor, the feed stream or the reactor or the feed stream and the reactor can be preheated to the necessary hydrogenation temperature. It is also possible to supply a partial flow of hot feed gas. The temperature of the gas during the reaction is to perform the method according to the invention 150 to 500 ⁰ C. Preferably, the temperature in the Alloca- tion of the feed gas to the reactor 250 to 350 ⁰ C, and ideally 300 ° C. The preferred pressure for the practice of the invention is 0.1 to 10 MPa. Due to the hydrogenation, the temperature in the gas stream can rise to 350 to 450 ° C.

The proportion of feed gas, which is passed through the first reactor bed for hydrogenation, is preferably for carrying out the method according to the invention about 5 to 15 mass% of the feed gas. Depending on the sulfur content and expected hydrogenation heat, however, the proportion for the first reactor bed can also be lower or higher. The proportion of feed gas which is passed through the first reactor bed for hydrogenation, for carrying out the method according to the invention may be from 1 to 99% by mass of the feed gas, provided that the parameters have a starting effect. The number of catalyst beds in the reactor depends essentially on the sulfur and olefin content in the gas to be hydrogenated. Depending on the design, a reduced system space requirement may make the establishment of additional catalyst beds look favorable.

For carrying out the method, it is useful to direct the gas to be hydrogenated in downward flow through the reactor. In this case, the positioning of the catalyst particles in the catalyst bed can be more easily maintained. It is also possible in principle to direct the gas flow in an upward or sideways leading direction. For this purpose, however, special devices are necessary to avoid the fluidization of the catalyst bed. The higher the sulfur content or the olefin content or sulfur content and the olefin content in the reaction gas, the more catalytic beds are needed. If the sulfur content or the olefin content in the reaction is higher, for example, three catalyst stages can be installed in the reactor. When passing through a catalyst stage, the reaction gas heats up. Behind each catalyst stage is a new introduction device for cool reaction gas, which is mixed with the gas stream coming from the catalyst bed and thereby cools this down to a suitable temperature for further hydrogenation.

Any number of catalyst beds can be installed in the reactor. In this way it is possible to adjust the sulfur content of each feed gas to virtually any level by hydrogenation and purification. The organic sulfur compounds in the feed gas can be present in any form. The most common constituents of low molecular weight hydrocarbon gases are aliphatic mercaptans. Depending on the origin of the gases, however, cyclic or aromatic sulfur compounds may also be present in the gas.

The organic sulfur components are converted in the hydrogenation in hydrogen sulfide. This can be removed by gas washing processes from the product gas. Suitable gas scrubbing processes for purifying gases of hydrogen sulfide are well known to those skilled in the art of producing refinery gases. For example, washing processes with ethanolamines or alkylated polyalkylene glycols are suitable. By using such processes, the sulfur content of the product gas can be set below 100 ppb. However, it is also possible to produce a product gas having a higher sulfur content.

For a depletion of the hydrogen sulfide and chemical Absorbtionsverfahren can be used. A suitable absorbent is zinc oxide, for example. These methods are preferably used in combination with the method according to the invention. However, it is also possible to hydrogenate material streams with the method according to the invention and then to feed it to any further use. Finally, all processes which are capable of hydrogenating the sulfur fraction of olefin- and hydrogen-containing starting gases in a reactor by means of the arrangement of the catalyst beds according to the invention are suitable for carrying out the process according to the invention.

As feed gases are virtually all gases in question, which are sulfurous. Typical feed gases are refinery gases which are used as a fraction in the refining of Incurred oil. Examples include residual gases from refinery processes. These usually have an increased content of hydrocarbons having 2 to 6 carbon atoms. Examples of such gas mixtures are LPG ("/ jquefied petroleum gas"), liquefied gases or light gasoline, although it is of course also possible to use heavier hydrocarbon fractions if they are gaseous under the conditions used, for example, petrol or petroleum contained in higher olefins.

Prerequisite for use in the method according to the invention is merely that the gases are sulfur or olefinhaltig. The preferred gases for these purposes, however, contain both sulfur compounds and olefins. In particular, these gases generate in the hydrogenation large amounts of heat, so that a series connection of catalyst beds is necessary. The sulfur content of the feed gases can be arbitrarily high. Also, the olefin content or hydrogen content can be arbitrarily high. The feed gas can also be pre-cleaned before use, so that it only contains a lower sulfur content than when it was delivered.

Optionally, the feed gas should still be added to the hydrogen. This may be necessary in particular for a desired complete desulfurization. This can be added to the feed gas prior to use in the process according to the invention. But it is also possible to add the hydrogen after the distribution of the feed stream. It is also possible to add the hydrogen in the reactor, including gas mixing devices can be used. Finally, the hydrogen can be added to the reaction stream at any point to adjust the hydrogen content to the desired level.

[0022] Also claimed is an apparatus for carrying out the method according to the invention. In particular, a reactor with at least two catalyst beds suitable for hydrogenation with at least one feed device for fresh feed gas installed behind the first catalyst bed is claimed.

In particular, a device is claimed, which is characterized in that • a pipe for guiding the feed gas divides the feed gas stream into two gas streams, and

• the pipelines carrying the first feed stream are fed from the top into a multi-level catalyst bed. reactor, wherein the reactor contains at least two horizontally arranged catalyst beds, and

• in the gas flow between the first and the second catalyst bed, a second laterally leading into the reactor pipeline is installed, which can introduce the second feed stream in the downwardly leading gas stream, so that the feed mixture can flow through the second catalyst bed.

Prerequisite for the execution of the method according to the invention is that the overhead feed stream can be preheated, if he does not have the necessary for hydrogenation use temperature. Therefore, in a preferred embodiment, the device also has a heating device. These may be gas or oil fired burners. It is also possible to set up an electric or steam-driven preheating, which may be useful especially for smaller plants. In order to make the process economically favorable, heat exchangers which preheat the feed gas with the product gas heated by the hydrogenation process are present on the feed train for carrying out the process according to the invention for introducing the first subset of the feed stream. However, it is also possible to preheat the feed gas with other heated reaction products.

Depending on the sulfur content and the desired degree of hydrogenation, the reactor may also contain a plurality of catalyst beds. Thus, it is possible to use three or more or any number of catalyst beds instead of two catalyst beds. Behind each of the catalyst beds there may then be a device with which fresh feed gas can again be passed into the reactor. These can be spraying or dousing facilities, depending on whether it is a liquid or a gas. The devices for introducing the fresh reaction gas may be of any kind in order to ensure a turbulence-free and unturbulent gas flow. The spray or delivery heads may also include regulating means such as valves.

Also claimed is a device which is characterized in that

• the piping for the supply of the feed gas divides the feed stream into further gas streams, and • In the reactor further horizontally installed catalyst beds are installed, wherein

• In the reactor further pipelines laterally into the reactor are installed, which can introduce the other feed streams in the downwardly leading gas stream, so that the feed mixture can flow through the other catalyst beds.

In order to maintain correct operation, the amounts of cool feed gas must be accurately metered. This is the only way to precisely control the temperature in the reactor. For dividing the gas stream is located directly on the supply line for the fresh feed gas, a device for dividing the gas stream. Behind it are then valves, with which the supply of the gas to the individual Einsprühungs- or Eindüsungsvorrichtungen in the reactor is precisely controlled. Depending on the heating of the gas in the individual catalyst beds, this amount is then metered. Thus, the temperature in the reactor can be maintained within the prescribed temperature limits.

The supply amount of feed gas into the reactor is preferably controlled by the temperature. Therefore, temperature sensors or thermometers can be located anywhere in the reactor. Of course, the device according to the invention also includes the necessary control devices for control, it does not matter if they are electrical, electronic or mechanical nature. The regulation of the gas supply is also possible via other signals, for example via the sulfur or olefin content of the gas or a combination of these measured values.

The device according to the invention should preferably manage without cooling or heating devices. The addition should ideally be such that this is not necessary. However, if other process conditions are selected, the device may also include heating or cooling devices when necessary to establish optimal operation.

The catalyst beds are designed so that a good gas flow and a fast and effective reaction is possible. The catalyst is preferably on a carrier suitable for this purpose. The carriers are applied for execution, for example, as pellets, as Raschig rings or in the form of porous shaped bodies. Suitable materials for this are known to the person skilled in the art. For example, be ceramic or pressed molded aluminum oxide body. Also suitable are silicic acids. The carriers are preferably on close-meshed gratings, with which a suitable mounting of the catalysts in the reactor is possible. However, other suitable holding devices are also possible. The catalyst bed can be arranged as desired in the reactor. It is possible to mount the catalyst in a round or square fixture. It is also possible to arrange the catalyst bed concentrically to allow for improved gas flow. This is located in the catalyst bed a round or square recess.

For use in the process according to the invention are catalysts, as are customary for hydrogenation reactions for hydrodesulfurization. For carrying out the process according to the invention, these are preferably nickel-containing, cobalt-containing or molybdenum-containing catalysts. However, other metals from Group VIIIb of the Periodic Table are also suitable. Also known are noble metals such as Pd or Pt or zeolites, with which a hydrogenating Desulfurierung can be performed. Of course, these metals or other metals can be used in the catalyst in any combination.

Furthermore, the device according to the invention can also comprise devices at any point which are necessary for maintaining optimum operation. These may be, for example, valves, pumps, gas distributors or gas conveyors. But these can also be sensors, thermometers, flow meters or analytical devices. These can be located anywhere in the device according to the invention.

The inventive method and apparatus of the invention allow the hydrogenating desulfurization of olefin-containing feed gases with little equipment and without expensive cooling or heating. Desulphurization is effective so that the sulfur content of the feed gas can be reduced to the ppb range (ppb: parts per billion, 10 ^{~ 7} mole percent). The process allows reliable and safe temperature control and handling of the process.

The device of the invention will be explained in more detail with reference to a drawing, wherein the embodiment is not limited to this drawing. FIG. 1 shows a reactor according to the invention by way of example with three catalyst beds for carrying out a hydrodesulfurization. The feed gas (1) comes from the reservoir and is divided by a gas distributor (2) into three feed streams (3,4,5). For each gas or liquid supply line, three valves (3a, 4a, 5a) for regulating the feed stream are installed. The first feed stream (3) is preheated by means of a heating device (6) or a heat exchanger (with heat flow, 6a) and introduced into the reactor (7) via the reactor head (3b) (8a). Ideally, the temperature when introducing the first stream is 300 ° C. The first feed stream meets there on the first catalyst bed (8) and heats up there. The catalyst bed (8) contains the catalyst (8b) on suitable carrier particles and a grid (8c) or other suitable holding device. The temperature at the outlet at the lower grid floor for the first catalyst bed (8) can be up to 390 ⁰ C. Behind the first catalyst bed (8) then further feed gas (9a) is introduced. As a result, the feed stream cools again, ideally to 300 ⁰ C. Thus, this stream meets the second catalyst bed (9) with catalyst (9b) on a holding device (9c). There, the gas stream heats up again by the hydrogenation reaction. To set the correct reaction temperature, further feed gas (10a) is then introduced behind the catalyst bed. The gas stream then meets again on a third catalyst bed (10) with catalyst (10b). The catalyst is held in the reactor by gratings (8c, 9c, 10c) or other holding devices. At the outlet of the reactor, a product gas (11) is obtained, which essentially contains only hydrogen sulfide as sulfur compound. The product gas (12) is carried out at the end of the reactor.

[0036] List of Reference Numerals

1 feed gas

2 gas distributor

3 First feed stream

3a valve for controlling the first feed stream

3b First feed stream passed over reactor head

4 Second feed stream a Valve for controlling the second feed stream

5 Third feed stream

5a valve for controlling the third feed stream

6 heat exchanger 6a heat flow

7 reactor

8 First catalyst bed a Gas supply devices for the first feed stream

8b catalyst particles in the first catalyst bed

8c holding device for the first catalyst bed

9 second catalyst bed

9a gas supply devices for the second feed stream

9b catalyst particles in the second catalyst bed

9c Holding device for the second catalyst bed

10 Third catalyst bed

10a gas supply means for the third feed stream

10b catalyst particles in the third catalyst bed

10c holding device for the third catalyst bed

11 gas flow

12 product gas

Claims

claims

1. A process for the hydrodesulfurization of olefin-containing feedstocks with a hydrogen-containing feed gas, wherein

characterized in that

• the reaction mixture thus obtained is passed with the gas stream in the reactor through a further subset of a catalyst suitable for hydrogenating desulfurization, so as to obtain a hydrogenated useful gas whose sulfur compounds and / or olefin compounds have been partially or completely converted into hydrogen sulfide or alkanes by hydrogenation ,

2. The method according to claim 1, characterized in that before or after the division of the feed stream, an addition of hydrogen takes place.

3. The method according to any one of claims 1 or 2, characterized in that the first, given in the top of the reactor feed stream is preheated.

4. The method according to any one of claims 1 to 3, characterized in that the proportion of the first, guided in the top of the reactor gas stream is 1 to 99 percent by mass of the total feed gas stream.

5. The method according to any one of claims 1 to 3, characterized in that the proportion of the first, guided in the top of the reactor gas stream is 5 to 15 percent by mass of the total feed gas stream.

6. The method according to any one of claims 1 to 5, characterized in that the received after passing through the first subset of the hydrogenating desulfurization catalyst useful gas are passed through another or through several further subsets of a hydrogenating desulfurization catalyst.

7. The method according to any one of claims 1 to 6, characterized in that the residual amount of organic sulfur compounds in the resulting useful gas is less than 100 ppb.

8. The method according to any one of claims 1 to 7, characterized in that a gas is used as the feed gas for the hydrodesulfurization, which contains a substantial proportion of olefins having 1 to 6 carbon atoms.

9. The method according to any one of claims 1 to 7, characterized in that a gas is used as the feed gas for the hydrogenating desulfurization, which contains a higher proportion of higher olefins.

10. The method according to any one of claims 1 to 9, characterized in that the hydrodesulfurization is carried out at a temperature of 150 to 500 ° C.

11. The method according to any one of claims 1 to 10, characterized in that the feed gas is passed at a temperature of 200 to 400 ⁰ C in the reactor.

12. The method according to any one of claims 1 to 10, characterized in that the feed gas is passed at a temperature of 250 to 350 ⁰ C in the reactor.

13. The method according to any one of claims 1 to 12, characterized in that the hydrodesulfurization is carried out at a pressure of 0.1 to 10 MPa.

14. The method according to any one of claims 1 to 13, characterized in that the heating of the feed gas takes place by heat exchange with the hydrogenated useful gas.

15. The method according to any one of claims 1 to 14, characterized in that adjoining the process for hydrogenating Desulfurierung a gas scrubber or a separation for hydrogen sulfide.

16. The method according to any one of claims 1 to 14, characterized in that adjoins the process for hydrogenating Desulfurierung an absorption process with a chemical absorbent.

17. Device, characterized in that • a pipe for guiding the feed gas divides the feed gas stream into two gas streams, and

The header line leading the first feed stream leads from the top side into a reactor equipped with a plurality of horizontally arranged catalyst beds, wherein the reactor contains at least two horizontally arranged catalyst beds, and

18. The apparatus according to claim 17, characterized in that there is a device for supplying hydrogen before or after the means for dividing the gas stream.

19. The device according to any one of claims 17 or 18, characterized in that there is a heating device on the pipeline for the first feed mixture before the reactor.

20. The apparatus according to claim 19, characterized in that it is in the apparatus for heating the first feed mixture to a heat exchanger, which heats it with the Nutzgas.

21. Device according to one of claims 17 to 20, characterized in that

• the piping for the supply of the feed gas divides the feed stream into further gas streams, and

• in the reactor further horizontally installed catalyst beds are installed, wherein

On the reactor further pipelines laterally leading into the reactor are installed, which can initiate the further feed streams in the downwardly leading gas stream, so that the feed mixture can flow through the other catalyst beds.

22. Device according to one of claims 17 to 21, characterized in that there are measuring devices for the temperature at the gas introduction positions in the reactor and in front of and behind the catalyst beds.

23. Device according to one of claims 17 to 22, characterized in that at the gas supply lines for the feed gas valves for controlling the gas flow, the amount of gas and the ratio of the individual feed gas feeds are in the reactor.

24. Device according to one of claims 22 and 23, characterized in that are connected to the temperature sensors and the valves control devices which regulate the flow of gases as a function of the signals of the temperature sensors.

25. Device according to one of claims 17 to 24, characterized in that the catalyst comprises nickel-containing compounds.

26. Device according to one of claims 17 to 25, characterized in that the catalyst is present on carriers in the form of pellets, Raschig rings or porous shaped bodies and the catalytically active material is applied to these moldings.

27. The device according to claim 26, characterized in that the carrier consist of pressed alumina or pressed silica.

28. Device according to one of claims 17 to 27, characterized in that the catalyst on a grid or other suitable

Holding device, which is mounted in the reactor is located.

29. The device according to claim 28, characterized in that the grid o- of the holding device for the catalyst is round or square.

30. Device according to one of claims 28 or 29, characterized in that the grid or the holding device for the catalyst is provided with a round or angular recess.