EP2451903B1 - Method for desulfurizing materials containing olefins by regulating the amount of olefins - Google Patents

Description

The invention relates to a process for the hydrogenation of olefin- and sulfur-containing material streams, as often occur, for example, in petroleum refineries. By means of the process according to the invention, the sulfur compounds contained in these streams are completely or partially converted into hydrogen sulfide by hydrogenation in a reactor and the olefins contained in these streams are completely or partially converted into alkanes by hydrogenation. The regulation of the process and in particular the temperature distribution in the reactor is achieved by controlling the olefin content in the feed streams to be fed into the reactor.

The WO 2009/071180 A1 describes a process for the hydrogenation of olefin-containing streams which contain organic sulfur compounds and which are converted into hydrogen sulfide during the hydrogenation. The hydrogenation allows the sulfur compounds to be removed from the material flow used by removing the hydrogen sulfide from the product gas as a mixture of substances obtained by gas scrubbing after the hydrogenation.

The feed streams are passed through a reactor which contains a plurality of successive catalyst beds in the gas flow direction in which a successive hydrogenation is carried out. The feed streams are typically a gas or a vaporized liquid. Behind each catalyst bed there is an inlet device for a further feed stream, with which further feed stream can be passed into the gas stream in the reactor. Since the catalyst beds and the gas stream in the reactor heat up again after each hydrogenation step, the temperature distribution in the reactor can be controlled by distributing the feed stream downstream of the individual catalyst beds. The addition of fresh feed stream after the respective catalyst bed cools the feed stream down again.

In this way it is possible to always carry out the hydrogenation in the optimum temperature range. This allows the catalyst to be kept at a temperature that corresponds to its optimum range of use. This procedure gives different flow rates behind the individual catalyst beds. This can lead to different pressure conditions in the reactor, which can be problematic depending on how the process is carried out. There is therefore the task of controlling the addition of the olefin downstream of the individual catalyst beds in such a way that it does not take place by regulating the flow rate.

The invention solves this problem by adding feed streams which contain precisely regulated olefin proportions. Since the gas stream and the catalyst bed in the reactor are only heated by the heat of reaction of the hydrogenation reaction of the olefins, the temperature distribution in the reactor can be regulated by adding feed streams with different olefin content. A feed stream is always to be understood as a gaseous material stream.

• ein olefin- und wasserstoffhaltiger gasförmiger Einsatzstrom (3b) durch einen Reaktor (7) geleitet wird, der einen hydrierenden Katalysator zur Entschwefelung (8b, 10b, 11b) enthält, und die in dem olefin- und wasserstoffhaltigen Einsatzstrom (1) enthaltenen organischen Schwefelverbindungen und Olefine ganz oder teilweise zu Schwefelwasserstoff und Alkanen hydriert werden, und
• der olefinhaltige Einsatzstrom (1) vor der Zuführung in den Reaktor (7) aufgeteilt wird, so dass man mindestens zwei Einsatzströme erhält (3, 4, 5), und
• der erste Einsatzstrom (3) über geeignete Vorrichtungen über den Kopf des Reaktors durch ein Katalysatorbett (8) im Reaktor (7) mit einer Teilmenge eines Katalysators zur hydrierenden Entschwefelung (8b) geleitet wird, und
• ein zweiter Einsatzstrom (4) seitlich hinter dem ersten Katalysatorbett in den Reaktor (7) und zu dem durch die erste Hydrierung erhitzten Reaktionsgemisch gegeben wird, und der so erhaltene Gasstrom durch ein zweites Katalysatorbett (10) im Reaktor geleitet wird, und
• der Anteil der Olefine in mindestens einem Einsatzstrom durch separate Zuführung von Olefinen oder Verdünnungsgas in die einzelnen Einsatzströme steuerbar ist, wobei die Temperatur in dem Reaktor (7) durch Regelung des Anteils von Olefinen in mindestens einem Einsatzstrom geregelt wird,
  dadurch gekennzeichnet, dass
• als Einsatzstrom (1) für die hydrierende Entschwefelung ein Gas eingesetzt wird, das zu einem wesentlichen Anteil Olefine mit 2 bis 6 Kohlenstoffatomen enthält, und
• die Reaktion der Hydrierung bei einer Temperatur von 250 bis 400 °C durchgeführt wird.

What is claimed is a process for the desulfurization of olefin-containing feedstocks (1) by regulating the olefin content, with

• an olefin- and hydrogen-containing gaseous feed stream (3b) is passed through a reactor (7) which contains a hydrogenating catalyst for desulfurization (8b, 10b, 11b), and the organic sulfur compounds and contained in the olefin- and hydrogen-containing feed stream (1) Olefins are completely or partially hydrogenated to hydrogen sulfide and alkanes, and
• the olefin-containing feed stream (1) is divided before being fed into the reactor (7) so that at least two feed streams are obtained (3, 4, 5), and
• the first feed stream (3) is passed via suitable devices over the top of the reactor through a catalyst bed (8) in the reactor (7) with a partial amount of a catalyst for hydrogenated desulfurization (8b), and
• a second feed stream (4) is added laterally behind the first catalyst bed into the reactor (7) and to the reaction mixture heated by the first hydrogenation, and the gas stream thus obtained is passed through a second catalyst bed (10) in the reactor, and
• the proportion of olefins in at least one feed stream can be controlled by separately feeding olefins or diluent gas into the individual feed streams, the temperature in the reactor (7) being regulated by regulating the proportion of olefins in at least one feed stream,
  characterized in that
• a gas which contains a substantial proportion of olefins having 2 to 6 carbon atoms is used as feed stream (1) for the hydrogenating desulphurization, and
• the hydrogenation reaction is carried out at a temperature of 250 to 400 ° C.

Part of the total amount of olefin is fed in via the top of the reactor. The temperature at the top of the reactor is usually about 300 ° C., at which the hydrogenation reaction can be carried out well. The proportion of olefins in the first olefin-containing feed stream can advantageously be regulated by adding a low-olefin or an olefin-free diluent stream or both diluent streams to the first feed stream. This results in an olefin-containing feed stream.

The low-olefin and olefin-free feed streams can be added as a mixture, it being possible for these substances to be added separately in two separately regulated streams or in premixed form. By adding these two substance mixtures as diluent streams, it is then possible to set the desired proportion of olefins in the feed stream and, moreover, to control the temperature in the reactor. It is also possible, depending on the desired procedure, to introduce a further stream which contains a low-olefin or an olefin-free gas into the feed stream. The feed stream can then be further diluted in this way. The proportion of olefins in the first feed stream can also be increased by separately adding an olefin-rich stream to the first feed stream. In principle, the first feed stream used already contains olefins.

In one embodiment of the invention, a low-olefin and an olefin-free stream are added as a dilution stream to the first feed stream. In this way, the hydrogenation can be controlled via the olefin content in this stream so that it delivers a precisely defined amount of heat. The temperature downstream of the first catalyst bed is set in such a way that, when mixed with the second feed stream, it delivers precisely the temperature that is required for passage through the second catalyst bed.

It is possible to meter an olefin-rich stream into the feed stream, if this appears necessary, so that the proportion of olefins in the first feed stream is increased. This can be done temporarily or permanently. The olefin-rich stream can be added separately or premixed with another stream. Finally, an olefin-free, low-olefin and olefin-rich stream can be added separately to the first feed stream, so that this regulates the proportion of olefins in the first feed stream. Although if the metering is preferably carried out separately, a premix of these streams can also be metered in. The premixing can take place in any combination and in any proportion.

The reactor can also contain more than two catalyst beds. In a further embodiment of the invention, the material flow obtained in the reaction is passed through a third catalyst bed, whereby this and the gas flow passed through are heated. This means that after the second catalyst bed, a third feed stream is added laterally behind the second catalyst bed into the reactor to the material stream heated by the second hydrogenation and the gas stream for hydrogenation flows through a third catalyst bed after passing through the second catalyst bed.

For example, in one embodiment of the invention, behind the second catalyst bed, a third feed stream is added laterally behind the second catalyst bed into the reactor to the material stream heated by the second hydrogenation, and the material stream for the hydrogenation flows through a third catalyst bed after being passed through the second catalyst bed. It is possible to pass the stream obtained after passing through the third partial amount of the hydrogenating desulfurization catalyst through a further or several further partial amounts of a hydrogenating desulfurization catalyst and to add a further feed stream into the reactor laterally behind the catalyst beds.

In order to regulate the temperature distribution in this third catalyst bed as well, a low-olefin and an olefin-free stream are likewise fed into the feed line for the second feed stream behind the first catalyst bed. The proportion of olefins in this second feed stream can also be controlled through the admixture of the individual streams. This in turn makes it possible to control the temperature in the third catalyst bed. Here too, in one embodiment of the invention, it may be possible to additionally pass an olefin-rich stream of material into the reactor.

Finally, it is possible to pass the gas stream through any number of catalyst beds. A further stream of material can then be introduced laterally behind each catalyst bed which contains an olefin fraction with which the temperature of the subsequent hydrogenation can be optimally adjusted. This means that after passing through the third subset of the hydrogenating desulfurization catalyst, the stream of material obtained is passed through a further or several further subsets of one hydrogenating desulfurization catalyst is passed and a further feed stream is added laterally behind the catalyst beds into the reactor. It is possible to feed a low-olefin or olefin-free stream into the respective feed stream in order to deplete the corresponding feed stream of olefins if this is required. The olefin content of the corresponding feed stream can thus be regulated by metering in a stream. The metered addition can take place by separate streams of low-olefin / olefin-free material or as a premix.

Finally, it is possible to carry out an olefin enrichment by adding an olefin-containing stream. This can optionally take place behind any desired catalyst bed. Usually, however, this is not necessary. The said streams can be added as dilution streams in any combination and in any proportion.

The olefin-free gas is preferably hydrogen, methane or a mixture of these substances. The low-olefin gas is also preferably a gas which contains hydrogen or methane or both as the main component. However, it is also possible to add a different gas to the material flow supplied. These can be, for example, alkanes or carbon dioxide. Finally, the olefin-rich, the olefin-poor or the olefin-free stream can be mixed as desired. They also advantageously do not contain any undesired foreign gases.

The feed stream is preferably fed to the hydrogenation reaction via the top of the reactor. The proportion of the gas fed in via the top can in principle be as desired, but is preferably 1 to 99 percent by mass. Ideally, the flow rate of the gas fed in overhead is 5 to 15 percent by mass. Through the entire hydrogenation reaction, a feed stream can be obtained which contains a proportion of organic sulfur compounds of less than 100 ppb. The hydrogen sulfide can be removed by a subsequent gas scrub, so that an essentially sulfur-free gas is obtained.

The feed stream as feed stream for the hydrogenating desulphurization contains light olefins which are in gaseous form at the use temperature. These are in the C number range from 2 to 6.

The hydrogenation reaction is carried out at a temperature of 250 to 400 ° C. The feed stream is therefore preferably fed into the reactor at a temperature of 200 to 400.degree. In a particularly suitable reaction procedure, the feed stream is fed into the reactor at a temperature of 250.degree. C. to 350.degree. The respective temperature in the reactor then results from the corresponding reaction procedure. When a feed stream with a lower olefin content is fed in at the corresponding point, the reaction mixture cools down. By controlling the conduct of the reaction via the olefin content of the feed streams, the pressure in the reactor can be controlled much better. This is 0.1 to 10 MPa for a favorable type of design.

The heating of the feed stream to the temperature necessary for the reaction can take place at will. This can take place, for example, using burners or steam heating devices. However, the feed stream is preferably heated via heat exchangers. This can be done anywhere. The heated material flow in the reactor can serve as the heating medium for this. The heat exchangers can be heated at any point. This can be done, for example, on the individual feed streams. However, this can also take place on the material flows that are added to the feed flows. This can also be done on the feed stream that is fed into the reactor head.

In one embodiment of the process according to the invention, the process for hydrogenating desulfurization is followed by gas scrubbing or a separation for hydrogen sulfide. This can be of any type and can be carried out at any point in the process. For example, the process for hydrogenating desulphurization is followed by an adsorption process with a chemical adsorbent.

• eine Rohrleitung zur Führung des Einsatzstromes den Einsatzstrom in mindestens zwei Gasströme teilt, und
• die den ersten Einsatzstrom führende Rohrleitung von Kopfseite in einen mit mehreren waagrecht angeordneten Katalysatorbetten ausgerüsteten Reaktor führt, wobei der Reaktor mindestens zwei waagrecht angeordnete Katalysatorbetten enthält, und
• am Reaktor zwischen dem ersten und dem zweiten Katalysatorbett eine zweite seitlich in den Reaktor führende Rohrleitung installiert ist, die den zweiten Einsatzstrom in den nach unten führenden Stoffstrom einleitet, so dass der erhaltene Stoffstrom durch das zweite Katalysatorbett strömt, und
• die Rohrleitungen für mindestens einen Einsatzstrom Zuführungsleitungen für Stoffströme enthalten, mit denen sich der Anteil an Olefin im Einsatzstrom regeln lässt.

A device is disclosed with which the method according to the invention can be carried out and which is characterized in that

• a pipeline for guiding the feed stream divides the feed stream into at least two gas streams, and
• the pipeline carrying the first feed stream leads from the top into a reactor equipped with a plurality of horizontally arranged catalyst beds, the reactor containing at least two horizontally arranged catalyst beds, and
• a second pipeline leading laterally into the reactor is installed on the reactor between the first and the second catalyst bed and introduces the second feed stream into the downward stream of material so that the material stream obtained flows through the second catalyst bed, and
• the pipelines for at least one feed stream contain feed lines for material flows with which the proportion of olefin in the feed stream can be regulated.

These are feed lines that enable an olefin-rich stream to be fed into the corresponding feed stream. This can be a feed line with which an olefin-rich stream is fed into the feed stream. In this case the olefin content in the feed stream increases and the temperature in the subsequent catalyst bed increases accordingly. However, these can also be feed lines for a low-olefin or olefin-free stream in order to reduce the olefin content of the feed streams accordingly. The feed lines for material flows can be located at any point on the reactor or in the feed lines for the feed streams. These can also be present in any combination.

In this way, the proportion of olefins in the feed streams can be precisely metered. In this way, the temperature in the reactor can also be precisely controlled. For dividing the gas flow, a device for dividing the feed flow is located directly on the feed line for the fresh feed. The device also includes valves with which the supply of the gas to the individual injection or injection devices in the reactor can be precisely controlled. Depending on the heating of the gas in the individual catalyst beds, the amount of substance supplied is then dosed. In this way, the temperature in the reactor can be kept within the prescribed temperature limits.

• die Rohrleitung zur Führung des Einsatzstromes den Einsatzstrom in drei oder mehr weitere Gasströme teilt, und
• in dem Reaktor in drei oder mehr weitere waagrecht installierte Katalysatorbetten installiert sind, wobei
• am Reaktor drei oder mehr weitere seitlich in den Reaktor führende Rohrleitungen installiert sind, die Einsatzströme in den nach unten führenden Stoffstrom einleiten können, so dass der erhaltene Stoffstrom durch die weiteren Katalysatorbetten strömen kann, und
• die Rohrleitungen für die weiteren Einsatzströme Zuführungsleitungen für olefinhaltige Stoffströme enthalten, mit denen sich der Anteil an Olefin im Einsatzstrom regeln lässt.

If the feed stream is passed through more than two catalyst beds, the reactor contains further catalyst beds. This also includes the corresponding additional feed devices for the feed and material flows. In this case a device is disclosed wherein

• the pipeline for guiding the feed stream divides the feed stream into three or more further gas streams, and
• are installed in the reactor in three or more further horizontally installed catalyst beds, wherein
• three or more further pipelines leading laterally into the reactor are installed on the reactor, which can introduce feed streams into the material stream leading downwards so that the material stream obtained can flow through the further catalyst beds, and
• the pipelines for the further feed streams contain feed lines for olefin-containing material streams, with which the proportion of olefin in the feed stream can be regulated.

The amount fed and the composition of the feed stream into the reactor are preferably controlled via the temperature as a parameter. Therefore, temperature sensors or thermometers can be located anywhere in the reactor. Heating devices or cooling devices with which the temperature can additionally be regulated can also be located at any point in the device. Of course, the device also includes the control devices required for control, regardless of whether they are electrical, electronic or mechanical in nature. The amount and composition of the supplied material flow can also be regulated via other signals, for example via the sulfur or olefin content of the gas or a combination of these measured values. For this purpose, measuring sensors can be located at any point in the supply lines or in the reactor.

The device is in principle already in the patent DE 102007059243 A1 shown. This differs from the present device in particular through the additional pipelines for olefin-containing feed streams. Furthermore, in the context of the present invention, the international application with the publication number WO 2008/148081 to get expelled.

The device can furthermore comprise devices at any point which are necessary to maintain optimal operation. These can be, for example, valves, pumps, gas distributors or gas delivery devices. However, these can also be sensors, thermometers, flow meters or analytical devices. These can be located anywhere in the device.

The method according to the invention and the device allow the hydrogenating desulfurization of olefin-containing gases with little equipment and without complex cooling or heating devices. The desulfurization is effective, so that the sulfur content of the feed stream in the subsequent gas scrubbing can be reduced to the ppb range (ppb: parts per billion, 10 ^-7 mol percent). The method allows reliable and safe temperature control and handling of the method. The process according to the invention results in a product gas which essentially only contains hydrogen sulfide as a sulfur compound.

The device is explained in more detail with reference to a drawing, the embodiment not being restricted to this drawing.

FIG. 1 shows an example of a reactor with three catalyst beds for carrying out hydrogenation desulphurisation. The feed stream (1) is divided into three feed streams (3, 4, 5) by a gas distributor (2) . The feed stream usually already contains the necessary amount of olefins. For each gas or liquid supply line, three valves (3a, 4a, 5a) are installed to regulate the feed flow. The first feed stream (3) is preheated with 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 the first stream is introduced is 300 ° C. The first feed stream meets the first catalyst bed (8) there and is heated there. The catalyst bed (8) contains the catalyst (8b) on suitable carrier particles and a grid (8c) or another suitable holding device. The temperature at the outlet at the lower grid floor for the first catalyst bed (8) can be up to 390 ° C, but is typically 370 ° C. The temperature in this first catalyst bed is regulated via the flow rate of the first feed stream (3b). The first catalyst bed (8) is heated by a higher proportion of olefins in the first feed stream. The olefin fraction can in turn be regulated via various streams (9a, b, c) , which are passed into the first feed stream (3) here, for example, as a diluent gas stream. This is an olefin-rich stream (9a), a low-olefin stream (9b) or an olefin-free stream (9c). If, for example, a feed stream (3a) with a higher olefin content is required, more of the olefin-rich stream (9a) is fed in. When using a low-olefin feed stream (3) , more of the low-olefin stream (9b) or the olefin-free stream (9c) is fed. For readjustment, olefin can be metered in by metering in an olefin-rich stream (9a) . In this way, the temperature in the first catalyst bed (8) can be easily controlled. This procedure is also possible with the other feed streams (4, 5) . For example, a further dilution stream (4) is introduced into a second feed stream (10a) after the first catalyst bed (8) without further regulation. As a result, the material flow cools down again, ideally to 300 ° C. This stream thus meets the second catalyst bed (10) with catalyst (10b) on a holding device (10c). There, the stream of material is heated up again by the hydrogenation reaction. To set the correct reaction temperature, a further feed stream (11a) is then introduced downstream of the catalyst bed (8) . The resulting stream then meets a third catalyst bed (11) with catalyst (11b) . The catalyst is held in the reactor by grids (8c, 10c, 11c) or other holding devices. At the outlet of the reactor, a product gas (12) is obtained which essentially only contains hydrogen sulfide as a sulfur compound. The product gas is discharged (13) at the end of the reactor (7 ). With the thermal energy of the feed stream (6a) , the first feed stream (3b ) is preheated here, for example, via a heat exchanger (6) . The thermal energy of the feed stream (1) is also used (14a) to preheat the low-olefin material stream (9b) via a heat exchanger (14) , which is fed into the first feed stream (3) . The feed stream (3) can, if necessary, be further heated via a further heat exchanger (14b) to set the temperature. The individual material flows (9a, b, c) can be regulated via valves (15a, b, c) . Typical reactor temperatures are indicated on the side.

List of reference symbols

1

Feed stream (containing olefin)

2

Gas distributor

3

First input stream

3a

Valve for regulating the first feed stream

3b

First feed stream passed through the reactor head

4th

Second input stream

4a

Valve for regulating the second feed stream

5

Third feed stream

5a

Valve for regulating the third feed stream

6th

Heat exchanger for heating up the first feed stream

6a

Heat flow from the feed stream for heating the first feed stream

7th

reactor

8th

First catalyst bed

8a

Gas supply devices for the first feed stream

8b

Catalyst particles in the first catalyst bed

8c

Holding device for the first catalyst bed

9a

Olefin-rich material flow

9b

Low-olefin material flow

9c

Olefin-free material flow

10

Second catalyst bed

10a

Gas supply devices for the second feed stream

10b

Catalyst particles in the second catalyst bed

10c

Holding device for the second catalyst bed

11

Third catalyst bed

11a

Gas supply devices for the third feed stream

11b

Catalyst particles in the third catalyst bed

11c

Holding device for the third catalyst bed

12

Product gas

13

Product gas extraction

14th

Heat exchanger for heating up the low-olefin material flow

14a

Heat flow from the feed flow to the heating of a material flow

14b

Heat exchanger for heating up the first feed stream

Claims (19)

1. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins, wherein

   • an olefin- and hydrogen-containing gaseous feed stream (3b) is passed through a reactor (7) containing a hydrogenating catalyst for desulfurization (8b, 10b, 11b) and the organic sulfur compounds and olefins present in the olefin- and hydrogen-containing feed stream (1) are entirely or partially hydrogenated to form hydrogen sulphide and alkanes, and

   • the olefin-containing feed stream (1) is divided to give at least two feed streams (3, 4, 5) before introduction into the reactor (7), and

   • the first feed stream (3) is conveyed, via suitable devices via the top of the reactor, through a catalyst bed (8) in the reactor (7) containing a partial amount of a catalyst for hydrogenative desulfurization (8b), and

   • a second feed stream (4) is introduced laterally downstream of the first catalyst bed into the reactor (7) and introduced into the reaction mixture which has been heated by the first hydrogenation, and the resulting gas stream is passed through a second catalyst bed (10) in the reactor, and

   • the proportion of the olefins in at least one feed stream is controllable by means of separate introduction of olefins or diluent gas into the individual feed streams, where the temperature in the reactor (7) is regulated by regulating the proportion of olefins in at least one feed stream,
   characterized in that

   • a gas which contains a significant proportion of olefins having from 2 to 6 carbon atoms is used as a feed stream (1) for the hydrogenative desulfurization, and

   • the hydrogenation reaction is carried out at a temperature of from 250 to 400°C.
2. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to Claim 1, characterized in that the proportion of olefins in the first olefin-containing feed stream (3b) is regulated by addition of a low-olefin diluent stream (9b) or an olefin-free diluent stream (9c) or of both diluent streams to the first feed stream (3).
3. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to either Claim 1 or 2, characterized in that the proportion of olefins in the first feed stream (3b) is increased by separate addition of an olefin-rich stream (9a) to the first feed stream (3).
4. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 3, characterized in that, downstream of the second catalyst bed (10), a third feed stream is introduced laterally downstream of the second catalyst bed into the feed stream (10a) which has been heated by the second hydrogenation in the reactor and the stream flows, for the purpose of hydrogenation, through a third catalyst bed (11) after passage through the second catalyst bed (10).
5. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 4, characterized in that the stream (12) obtained after passage through the third partial amount (11) of the hydrogenating desulfurization catalyst is conveyed through a further partial amount or through a plurality of further partial amounts of a hydrogenating desulfurization catalyst and a further feed stream is introduced laterally into the reactor downstream of the catalyst beds.
6. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to Claim 5, characterized in that the proportion of olefins in the feed streams (3, 4, 5) is regulated by addition of a low-olefin stream (9b) or an olefin-free (9c) stream or a combination of these streams (9b, 9c) to the feed streams.
7. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 6, characterized in that the olefin-free (9c) or low-olefin (9b) stream is a hydrogen-containing stream.
8. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 6, characterized in that the low-olefin (9b) or olefin-free (9c) stream is a methane-containing stream.
9. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 6, characterized in that the low-olefin (9b) or olefin-free (9c) stream is a hydrogen- and methane-containing stream.
10. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 9, characterized in that the first feed stream (3) introduced into the top of the reactor is preheated.
11. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 10, characterized in that the proportion of the first gas stream (3) introduced into the top of the reactor is from 1 to 99% by mass of the total feed stream (1) .
12. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 11, characterized in that the proportion of the first gas stream (3) introduced into the top of the reactor is from 5 to 15% by mass of the total feed stream (1) .
13. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 12, characterized in that the feed stream (1) is introduced at a temperature of from 200 to 400°C into the reactor (7).
14. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 12, characterized in that the feed stream (1) is introduced at a temperature of from 250 to 350°C into the reactor (7) .
15. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 14, characterized in that the hydrogenative desulfurization is carried out at a pressure of from 0.1 to 10 MPa.
16. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 15, characterized in that the heating of the feed stream (3, 4, 5) is effected at any position by heat exchange with the hydrogenated feed stream.
17. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 16, characterized in that the heating of an olefin-rich stream (9a), a low-olefin stream (9b) or an olefin-free stream (9c) is effected at any position by heat exchange (6a) with the hydrogenated feed stream (13) .
18. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 17, characterized in that the process for hydrogenative desulfurization is followed by a gas scrub or a removal of hydrogen sulphide.
19. Process for desulfurizing olefin-containing starting materials (1) by regulating the proportion of olefins according to any of Claims 1 to 18, characterized in that the process for hydrogenative desulfurization is followed by an adsorption process using a chemical adsorbent.

Images