EP2928991A1

EP2928991A1 - Device and method for cracking gases

Info

Publication number: EP2928991A1
Application number: EP13805823.5A
Authority: EP
Inventors: Dragan Stevanovic; Thomas OEHMICHEN
Original assignee: Krones AG
Current assignee: Krones AG
Priority date: 2012-12-06
Filing date: 2013-12-06
Publication date: 2015-10-14
Also published as: DE102012111900A1; US20160059197A1; US9533274B2; CN104955924A; WO2014087000A1

Abstract

The invention relates to a device for cracking gases, comprising a supply line (1) for a gas containing carbon, by means of which the gas can be supplied to a first heat exchanger (5, 9) having a filling of a thermal storage mass, a first combustion chamber (6, 8), which is arranged downstream in the flow direction of the gas and which has in particular a controllable supply apparatus for another gas containing oxygen, by means of which supply apparatus the gas containing carbon is partially oxidized as a result of hypostoichiometric oxygen supply, and a reactor (7), which is arranged downstream of the first combustion chamber (6, 8) in the flow direction of the gas and which has a filling of a catalytically active material for catalytically cleaving impurities of the gas containing carbon. According to the invention, a second combustion chamber (6, 8), having an in particular controllable supply apparatus for a gas containing oxygen, by means of which supply apparatus the catalytically processed gas containing carbon is partially oxidized as a result of hypostoichiometric oxygen supply, is arranged downstream of the reactor (7) in the flow direction of the gas containing carbon, and a second heat exchanger (5, 9) having a filling of a thermal storage mass is arranged downstream of said combustion chamber in the flow direction of the gas, wherein the flow direction of the gas containing carbon can be reversed at least in a region that includes the first and second heat exchangers (5, 9), the first and second combustion chambers (6, 8), and the reactor (7).

Description

Apparatus and method for cracking gases

description

The present invention relates to an apparatus and a method for cracking gases, in particular gases from gasification processes of carbonaceous starting materials. In particular, a device for cracking gases with a feed line for a carbonaceous gas, by means of which the gas of a first bed of a thermal storage mass zuleitbar, a downstream in the flow direction of the gas disposed first combustion chamber having a controllable supply means for another, oxygen-containing gas , by means of which by substoichiometric oxygen supply partial oxidation of the carbonaceous gas takes place, and a subsequently arranged in the flow direction of the gas of the first combustion chamber reactor having a bed of a catalytically active material for the catalytic cracking of impurities of the carbonaceous gas provided.

Gases, in particular gases from gasification processes of carbonaceous starting materials, may be contaminated with substances which may not oppose an energetic use of the gas depending on the type of contamination, but prevent further material use of these gases for the production of eg methanol, diesel or gasoline. But even with an energetic use of these gases, the removal of these impurities may be necessary, for example, to prevent damage and / or deposits in a turbine or piston engine. Depending on the type of use, it may therefore be necessary to remove these impurities from the gases. Especially in the material use is very high demands on the Gas quality, since otherwise significantly reduce the service life of the catalysts used for the chemical conversion.

In particular, for gases produced by a gasification process of carbonaceous raw materials such as biomass, coal or plastic waste, impurities such as NH ₃ , HCN, H ₂ S, COS, halogens, alkalis, tars and others and dusts may be present, especially the mentioned tars in the removal are significant.

In particular, under a gasification process, the thermo-chemical gasification of carbonaceous feedstocks, e.g. Biomass, coal or plastic waste to understand.

In the following, tars are understood to be complex multicomponent mixtures of organic components, in particular cyclic and polycyclic aromatic hydrocarbons.

The loading of a gas obtained by a gasification process with tars may, in addition to the carbonaceous starting material, for example, also be dependent on the gasification conditions and the type of gasifier. The tar content in the gas stream may for example be between 1 and 100 g / m ³ . Measures for tar reduction in gases are already known from the prior art. These can basically be subdivided into primary and secondary measures. Primary measures are understood to mean techniques that are already used during the gasification process. Secondary measures are arranged downstream or downstream of the gasifier. The latter can be divided into two main categories: physical processes and cracking / reforming.

Physical gas cleaning measures include electrostatic precipitators, cyclones, filters, and water and oil based scrubbers. These methods have the disadvantage that a subsequent energetic and material recycling is not readily possible.

In cracking / reforming, a distinction is made between thermal cracking and catalytic cracking / reforming. For purely thermal cracking, cracking without Presence of a catalytically active substance, temperatures of at least 1000 ° C are necessary. For complete conversion of eg naphthalene even temperatures greater than 1400 ° C are necessary. The associated high energy demand is often associated with a loss of calorific value. Furthermore, the formation of undesirable by-products in the form of solid carbon deposits during thermal cracking can be significantly increased.

In catalytic tar removal, the tar is reacted on a catalytically active substance at temperatures of, for example, 800 to 900 ° C. As catalysts, for example natural minerals such as dolomite or olivines or synthetic catalysts such as Ni-steam reforming catalysts can be used. However, the latter do not have sufficient life due to deactivation by sulfur and / or high tar loadings.

From the prior art, therefore, various attempts are known to develop special tar reforming catalysts with a longer service life. An example has been presented in document WO 2009/132959.

A disadvantage of all cracking / reforming processes is the energy required to achieve the high reaction temperatures.

In order to be able to achieve these high temperatures, DE 10 2004 026 646, for example, has proposed a process for the thermal exhaust gas purification of, for example, dioxins or furans by combustion (that is to say by means of oxygen excess). A portion of the imported raw material is thus used as fuel and is no longer available for further energy or material use.

The patent DE 195 21 673 describes a method for regenerative exhaust air purification, are used in the two large and a small storage mass to heat the exhaust air before the pollutants are burned and cool again after combustion, in a next step, the waste heat for heating to use. This should also achieve higher energy efficiency.

Furthermore, it is possible to guide tar-loaded product gases over a cold, radial bed, so that it comes to a condensation of the tars. In a second step, air or oxygen is passed over this bed, causing the tars be oxidized. A disadvantage proves that only gases with low tar loads can be cleaned and that the tars are only used energetically.

The document WO 02/051965 describes a cracking process in a fixed bed reactor with reverse flow. In this case, a gas to be cracked is passed through a bed in a combustion chamber in which the temperature is maintained by adding oxygen. The gas is then discharged via a second bed of the combustion chamber. Due to the heat stored in the fixed bed and the periodic flow reversal, a high heat recovery is possible. In order to achieve a quasi-continuous operation, a third bed is also used for flushing.

A disadvantage of the presented in the document WO 02/051965 method proves insufficient at low temperatures selectivity to the desired cracking products, which manifests itself in a much higher tendency to form solid carbon deposits. This is especially important when heating the gas. The coking rate depends on a variety of parameters such as bulk material, tar composition and concentration, gas composition, temperature and residence time. The formation of coke leads in the long term to an increase in the pressure loss over the bed. Also, dusts contained in the gas can deposit on the bed, so that it can lead to an additional pressure loss here. Furthermore, the use of catalytic materials as a storage material is limited, as they often have to be used in a defined temperature window. Due to the temperature gradient in the bed only small volumes and low residence times are therefore possible.

The present invention has for its object to provide an apparatus and a method for the utilization of hydrocarbons available, which allow high efficiency and high efficiency. Furthermore, it is an object to further minimize the energy expenditure and the heat losses for cracking or reforming processes, as well as to improve the gas quality for subsequent processes. It is a further object to minimize the undesirable formation of tar by-products and to provide the ability to place a catalytically active substance in sufficient volume at an optimum reaction temperature within a gas cracking apparatus. Furthermore, a method is to be created, which largely re-supplied the required heat by a regenerative process to the process, as well as a device that allows such a process management.

These objects are achieved by a device for cracking gases with a supply line for a carbon-containing gas, by means of which the gas is fed to a first heat exchanger with a bed of thermal storage mass, a downstream in the flow direction of the gas arranged first combustion chamber, the - a particular controllable and preferably controllable - supply means for another, oxygen-containing gas, by means of which by substoichiometric oxygen supply partial oxidation of the carbonaceous gas takes place, and a downstream in the flow direction of the gas of the first combustion chamber reactor, a bed of a catalytically active material for the catalytic splitting of impurities of the carbon-containing gas dissolved, which is characterized in that in the flow direction of the carbonaceous gas to the reactor below a second combustion chamber with a particular st euerbaren and preferably adjustable feed device for an oxygen-containing gas, by means of which substoichiometric oxygen supply partial oxidation of the catalytically treated carbonaceous gas takes place, and this combustion chamber in the flow direction of the gas is subsequently arranged a second heat exchanger with a bed of thermal storage mass, wherein the flow direction of carbonaceous gas is reversible at least in a range which includes the first and second heat exchangers, the first and second combustion chambers and the reactor. Advantageously, the device has at least one valve, and particularly advantageously a plurality of valves, in order to reverse the said flow device.

By this device, it is possible that the tar-charged gas via a bed in which can already take place first cracking reactions, a combustion chamber is supplied in which the temperature setting by - preferably - permanent, substoichiometric injection of oxygen-containing gases. In this combustion chamber is at least before the gas enters the reactor in which a catalytic cracking of impurities located in the gas is provided, at least partial thermal cracking of the tars contained in the gas possible. In the thermally treated and partially oxidized gas remaining tars and other impurities are catalytically cleaved by the bed located in the reactor of the catalytically active material. Subsequently, the gas can be supplied to a further combustion chamber, in which the temperature is brought again by sub-stoichiometric oxygen injection in a predetermined range or maintained in this area. From this second combustion chamber, the gas is - at least indirectly - discharged into a second heat exchanger.

It would be conceivable to dispense with the reactor and provide only a combustion chamber instead. However, the reactor preferably offers the possibility of supplying additional substances and in particular catalytically active substances (such as dolomite or nickel-containing substances or materials). Therefore, advantageously, the reactor has a supply device for supplying additional substances. The Applicant reserves the right to claim protection for such a reactorless design.

The first bed or the first heat exchanger preferably acts as a heat donor by which the temperature of the gas is increased even before flowing into the first combustion chamber. The second bed or the second heat exchanger preferably serves as a heat acceptor and is heated by the energy contained in the purified (and partially oxidized) gas. By supplying the cold raw gas to the first heat exchanger, this cools continuously, whereas the second heat exchanger is heated continuously by the supply of the hot clean gas. If the bed in the first heat exchanger is cooled below a minimum temperature and / or the bed in the second heat exchanger is heated to such an extent that the gas flowing through is not sufficiently cooled, the flow profile can be reversed by appropriate valve control, at least in the two beds and in the area between them. whereby a regenerative process is provided and thermal energy stored in the second bed is largely re-supplied to the process.

The bulk volumes of both beds are preferably designed so that the gas is heated at a heating rate of at least 2000 K / s, preferably 3000 K / s and more preferably greater than 4000 K / s. Thus, the residence time in the critical Temperature window in which the coking reactions take place minimized. This ensures that the coking rate is significantly reduced.

The device is suitable for carrying out a regenerative cracking process. For this purpose, a flow reversal must take place in certain time steps. This is preferably realized by corresponding valves in the gas lines. The double execution of beds and combustion chambers allows the gas - regardless of the direction of flow - can first pass through a bed and then through a combustion chamber before it enters the reactor. In the bed, the gas is preheated and brought in the combustion chamber by partial oxidation to the desired temperature and thereby impurities such. Tars already at least partially removed. Likewise, the gas can also be brought to a desired temperature, again independently of the direction of flow, after leaving the reactor and the endothermic cracking reaction carried out therein in another combustion chamber, again by partial oxidation. Finally, the heat energy present in the gas can be used to heat the heat storage medium in the second heat exchanger. On the one hand, the thermal energy for the cracking reactions can be provided by the two combustion chambers and by the heat of reaction released in each case due to the partial oxidation and, on the other hand, the heat losses of the plant can be compensated for.

In a preferred embodiment, at least one bed, but preferably both beds are at least partially flowed through radially by the gas. In this case, the bulk material is preferably surrounded by a cylindrical cold grid and a likewise cylindrical hot grid. For this purpose, conventional bulk material regenerators, as known from the prior art, can be used. Such regenerated bulk regenerators are therefore particularly suitable, as they allow high temperature gradients in the bed and thus high heating rates of at least 2000 K / s can be realized.

When the cold tar-containing gas flows through the heat accumulator, a portion of the dust contained in the gas is retained by the storage mass. In order to counteract the resulting increasing pressure distress, appropriate measures must be taken. It is therefore preferred that at least a part of a Storage mass of a bed of at least one heat exchanger for its purification - preferably discontinuously - particularly preferably pneumatically removable from the device and can be returned. In this case, the bulk material is preferably withdrawn from the bottom of the bulk material reactor, preferably transported pneumatically upwards and returned to the regenerator after cleaning. The adhering to the bulk dust can be separated, for example by means of a cyclone.

Preferably, the storage mass (after the removal and cleaning described above) in a hot zone of a bed traceable. Since the storage mass is preferably taken from a cool zone of a bed, so a continuous exchange and thus a continuous cleaning of the storage mass is possible. In this case, a conveyor for conveying the storage mass is advantageously provided. Advantageously, a delivery opening for carrying out the storage mass is provided from at least one heat exchanger, and preferably also a feed opening in order to supply the storage mass of the device and in particular a heat exchanger and / or the reactor.

In an advantageous embodiment of the bulk material recirculation, air, diluted air or other oxygen-containing gases are used as the carrier stream. The oxygen can then react with the optionally adherent coke and / or other dusts or impurities to C0 ₂ . This ensures that coke residues are burned off during the transport phase. In a further advantageous embodiment of the bulk material recirculation, an additional container can be interposed for burning off the bed, in which the bulk material is first collected and in which the burnout preferably takes place discontinuously.

Since the heat in the presented method or in the corresponding device is regeneratively recovered, it may happen when switching the flow direction that not yet purified gas enters the lines of the already conditioned gas. Therefore, according to a particularly advantageous embodiment, the device has a third bed of thermal storage mass. Through this third heat storage bulk a flushing of the first and second bed is possible. This can be done, for example, by reversing the flow on the line section following the reactor in the flow direction of the gas (the gas thus now flows through this line in the direction of the reactor), the gas after However, the cracking leaves the reactor through the third bed and so no dust or other contaminants from the bed, which was previously used to heat the gas before being fed to the reactor, in the discharge line or product gas line or clean gas line can transport.

The storage mass of the third bed is preferably designed so that the pressure drop over this bed is the same size as the pressure drop over the first or second bed. Should the volume of the third bed not be equal to the first and second bed, the pressure loss can be equalized, for example, by adjusting the particle size of the third bed and / or by varying the particle geometry of the third bed.

A further preferred embodiment is characterized in that the third bed is constructed axially and that it is connected to the reactor. The reactor and the third bed may in particular be arranged in the same housing. It is preferred that the reactor is arranged with the reaction bed above the third bed. It may be advantageous that between the third bed (the third bed) and the reactor or the reaction bed, a further layer is arranged for isolation. For this purpose, a material with a low thermal conductivity is preferred. Advantageously, this insulation layer can be designed from honeycomb stones.

In a preferred embodiment, the third bed is so incorporated into a pipe system of the device that they irrespective of the direction of flow of the gas through the first and second bed and / or the first and second heat exchanger only of a purge gas and / or gas from the reactor can be flowed through. The switching between the beds is preferably realized so that the third bed is always acted upon only with hot or cold pure and / or purge gas. As a result, in this bed the adhesion of dust is avoided and / or the formation of coke suppressed as much as possible. As a result, the device and the method can be simplified and operated more cost-effectively, since in this (third) bed means for a circulation promotion (for dust removal) omitted. For the regenerative heat exchanger (the beds) come as a heat storage honeycomb or pebbles (also called Pebbles) in a fixed bed used. As an alternative to the balls, any kind of shapes can be used, such as calipers or Raschig rings. The diameter of the balls is freely selectable, whereby smaller balls increase the specific surface per volume, which has a positive influence on the heat transfer. The pebbles, honeycomb body or similar can be made, for example, from inert alumina (Al ₂ 0 ₃ ). It may be advantageous to mix the alumina pebbles with catalytically active substances, such as cobalt, nickel, chromium or their oxides or sulfides.

As an alternative to alumina, it is also possible, for example, to use limestone or dolomite as the heat storage medium whose catalytic properties are known. Furthermore, olivine is a suitable storage material, as this has in contrast to dolomite or limestone sufficient mechanical stability and abrasion resistance, so that it can be used for a circulation promotion.

As material for the reaction bed, all the above-mentioned catalytic materials and / or mixtures of these and / or mixtures of these with an inert material can be used. Thus, for example, Ni catalysts tend to coke heavily at high tar loadings> 2 g / Nm ³ , so that it may be advantageous to switch a layer of dolomite and / or olivine before and after this layer.

In a preferred embodiment, the device has a purge gas feed line, by means of which at least one bed or a heat exchanger, preferably all beds or heat exchangers, a purge gas can be fed. For example, cracked gas, cracked gas, inert gas or steam can be used. Cracked gas can be returned to the system via a blower, for example. Particularly preferred is water vapor.

The stated object is further achieved by a method for cracking gases, in which a carbon-containing gas is first fed to a first heat exchanger with a bed of thermal storage mass, then fed to a first combustion chamber in which by substoichiometric oxygen supply (which in particular through a controllable and preferentially controllable feeder takes place) of a different oxygen-containing gas, a partial oxidation of the carbon-containing gas is carried out, and subsequently the carbonaceous gas is introduced into a reactor, which preferably has a bed of a catalytically active material for catalytic cracking of carbonaceous gas contaminants, wherein the carbonaceous gas is fed after treatment in the reactor of a second combustion chamber, in which by substoichiometric oxygen supply (which takes place in particular by a controllable and preferably controllable feeder) a partial oxidation of the carbonaceous gas, and coming from this combustion chamber by a second heat exchanger ( which preferably has a bed of a thermal storage mass), wherein the flow direction of the carbon-containing gas after a certain time interval at least in a region is reversed, which includes the first and second heat exchangers, the first and second combustion chambers and the reactor. The reversal preferably takes place by means of valves.

In a preferred variant of the method it is provided that during a flow reversal, a third storage mass is temporarily added, preferably in such a way that the gas flows through the third storage mass.

In a further preferred variant of the method, when passing the carbon-containing gas through at least one of the heat exchangers with beds of a storage mass, the carbonaceous gas passed through is heated at a rate of at least 2000 K / s, preferably at least 3000 K / s and more preferably at least 4000 K / s is heated.

Particularly advantageous in this process is the substantial decoupling of heating zone and reaction zone. As a result, the catalytically active substances can be accommodated in an amount sufficient to ensure high residence times in a temperature zone in which they are particularly active. In addition, by selective selection of the material of the storage mass, the coking rate during heating can be further reduced. Furthermore, the storage mass can be designed specifically for thermal requirements without having to consider reaction kinetic parameters. Preference is also given to a method for cracking gases in which the gas stream is fed to a high-temperature space, which consists of two combustion chambers in which the temperature is maintained by substoichiometric addition of oxygen and between which a reaction bed is arranged, take place at which substantially the cracking reactions and wherein advantageously the gas is regeneratively heated by means of two storage masses and cooled again, wherein the heating of inlet temperature to high temperature with a heating rate of at least 2000 K / s happens.

In this process, for the purpose of dust separation, part of the storage mass is preferably withdrawn discontinuously and cleaned and returned again. More preferably, for the purpose of dust separation, the promotion of the part of the storage mass is pneumatic. Even more preferably, carbon deposits adhering to the bulk material are burned off.

Preferably, the device is also distinguished by the fact that the third storage mass is accommodated in the same vessel in which the reaction bed is accommodated. More preferably, the third storage mass is acted upon only with hot cracked gas and purge gas.

Preferably, gas or water vapor cracked in the apparatus is used as the purge gas.

Further advantages, objects and characteristics of the present invention will be explained with reference to the following description of the appended drawing, in which an apparatus for cracking gases is shown by way of example. Components of the apparatus for cracking gases, which in the figures at least substantially coincide with respect to their function, can hereby be identified by the same reference numerals, these components not having to be numbered and explained in all figures.

Show it:

1 shows a schematic structure of a device for cracking gases,

Fig. 2 shows a preferred embodiment of the device with additional third bed and Fig. 3: a particular circuit form of the embodiment shown in Figure 2.

FIG. 1 shows a schematic structure of a device for cracking gases. 1 is also a flow chart of the process. Gas is supplied from a main supply line 1 via a valve 3 to the reactor either via the supply line V and via an exhaust line 2 "or after a flow reversal via a supply line 1" discharged via the exhaust pipe 2 '. Via a valve 4 and a main discharge line 2, the purified gas can be supplied to another use (not shown). The position of the valves 3 and 4 is - preferably periodically - changed.

The gas to be purified flows through a heat exchanger 5 with a bed in which it is heated at a rate of at least 2000 K / s, into a combustion chamber 6, after which it is fed to a reaction bed 7, in which the tars contained in the gas are reacted , Subsequently, the gas flows through a further combustion chamber 8 and a heat exchanger 9 with a bed of the reactor. The bed 5 serves as a heat donor, the bed 9 as a heat acceptor. When the flow reverses the bed 9 is used accordingly as a heat donor, while the bed 5 serves as a heat acceptor.

In the combustion chambers 6 and 8 oxygen-containing gas is injected substoichiometrically via the lines 10 and 1 1. This can be, for example, air or, with particular advantage, pure oxygen. As a result, a partial oxidation takes place, through which the heat losses of the system and the heat demand of the cracking reactions are covered.

In order to achieve the highest possible heating rates of at least 2000 K / s, the beds 5 and 9 are preferably flowed through radially by the gas.

For cleaning, a portion of a bed can be discontinuously withdrawn, freed from adhering dust and then returned to the bed (not shown). Preferably, the transport of the bed takes place pneumatically, so that the dust is removed solely by the mechanical movement of the bulk material. In a preferred variant of the abovementioned embodiment, where appropriate adhering coke burned by means of oxygen-containing gases (eg air or diluted air).

The return of the discharged part of the bed (also not shown) is preferably realized so that the bulk material is introduced specifically in the hot zone of the bed, as close to the combustion chamber, so that still adhering coke in situ due to the prevailing reaction conditions there Will get removed.

FIG. 2 shows a preferred embodiment of the device with additional third bed 12.

In order to ensure a continuous mode of operation and to avoid contamination of the clean gas line 2, a flushing phase is necessary before the flow reversal. This is achieved by briefly using a third bed 12.

In Figure 2, the open valves 3 'and 4 "are white, the closed valves 3", 4', 4 "', and 14', 14" and 14 "'are marked black. In the illustrated circuit, the one supplied via main supply line 1 flows Gas stream over the bed 5, is thereby heated and thus passes into the combustion chamber 6. Herein, the temperature is controlled by the addition of oxygen and / or oxygen-containing gases .. The gas is then passed through a reaction bed 7, at which the tars are catalytically reacted. The gas stream is passed into a combustion chamber 8, in which the temperature is brought to the level in the combustion chamber 6 by adding oxygen again, in particular by covering the heat losses due to the endothermic cracking / reforming reactions is available for further processing steps.

To change the direction of flow must be briefly switched to a third bed 12 for the purpose of flushing. This can be carried out in a separate vessel, but particularly advantageous is the arrangement of the third bed 12 in the same vessel in which the reaction bed 7 is arranged. In this case, the third bed 12 also serves to fix the reaction bed 7. Particularly advantageously, for example, consisting of honeycomb stones layer 15 for isolation between the third bed 12 and reaction bed 7 is arranged. This will cause the loss High temperature heat from the reaction layer minimized by conductive and convective heat flows.

FIG. 3 shows a special circuit form of the embodiment shown in FIG. The bed 5 is acted upon via the purge line 13 with purge gas.

As already mentioned above, it should be prevented that impurities can pass from the heat exchangers 5, 9 into the clean gas flow 2 when the flow is reversed. One way to prevent this is possible by the valve circuit shown in Fig. 3. The product gas does not flow in the circuit shown through one of the first or second heat exchanger 5, 9 in the discharge line 2 but through the third bed 12. This is at no time exposed to the raw gas stream, so that contamination of the third bed 12 with dust or the like Deposits are prevented.

In order to prevent the bed 12 from heating up in the flushing times and thus reducing the efficiency of the installation, the valve 14 "'is to be opened for a certain period of time for reasons of heat balance, which is always possible if the bed 12 does not contain hot gas is flowed through.

Simultaneously with the discharge of the product gas through the third bed 12 and the opened valve 4 "'into the clean gas discharge line 2, the first heat exchanger 5 can be cleaned by opening the valve 14' with purge gas. not shown) of the bed.

After the bed of the first heat exchanger 5 has been cleaned, valve 4 "'can be closed and valve 3' opened, in the opposite direction of flow in the area of the heat exchangers 5, 9, the combustion chambers 6, 8, and the reactor 7 in the flow direction shown in FIG To achieve flow of the gas.

The Applicant reserves the right to claim all features disclosed in the application documents as essential to the invention, provided they are novel individually or in combination with respect to the prior art. LIST OF REFERENCE NUMBERS

1, 1 ', 1 "main supply line, crude gas line

2, 2 ', 2 ", 2"' main discharge line, clean gas line

3, 3 ', 3 "raw gas valves

4, 4 ', 4 ", 4"' clean gas valve

5 First heat exchanger, storage mass, bed

6 First combustion chamber

7 reaction bed

8 second combustion chamber

9 Second heat exchanger, storage mass, bed

10 oxygen injection

1 1 oxygen injection

12 third storage mass, third bed

13 flushing line

14 ', 14 ", 14"' purge valve

15 insulating layer, e.g. honeycombs

Claims

claims

1 . Apparatus for cracking gases with a feed line (1) for a

carbon-containing gas, by means of which the gas is fed to a first heat exchanger (5, 9) with a bed of a thermal storage mass, a subsequently arranged in the flow direction of the gas first combustion chamber (6, 8), in particular a controllable feed device for another, oxygen-containing gas comprising, by means of which substoichiometric oxygen supply, a partial oxidation of the carbonaceous gas takes place, and a downstream in the flow direction of the gas of the first combustion chamber (6, 8) arranged reactor (7), a bed of a catalytically active material for the catalytic cracking of impurities of the carbonaceous Has gas,

characterized in that

in the flow direction of the carbon-containing gas to the reactor (7) below a second combustion chamber (6, 8) with a particular controllable

Feeding device for an oxygen-containing gas, by means of which

sub-stoichiometric oxygen supply is a partial oxidation of the catalytically treated carbon-containing gas is arranged, and this

Combustion chamber in the flow direction of the gas below a second

Heat exchanger (5, 9) is arranged with a bed of a thermal storage mass, wherein the flow direction of the carbonaceous gas is reversible, at least in a range of the first and second

Heat exchanger (5, 9), the first and second combustion chamber (6, 8) and the reactor (7) encloses.

2. Device according to claim 1, characterized in that the volume and / or the specific surface of at least one / of the heat exchangers,

Beds and / or storage mass (5, 9), preferably the volumes and / or the specific surface of both heat exchangers, beds and / or

Storage masses (5, 9) are designed so that the conductive carbon-containing gas with a heating rate of at least 2000 K / s, preferably at least 3000 K / s and more preferably at least 4000 K / s is heatable.

3. Device according to one of the preceding claims, characterized in that the heat exchangers, beds and / or storage masses (5, 9) are radially flowed through by the carbonaceous gas.

4. Device according to one of the preceding claims, characterized in that at least one part of a storage mass of at least one bed and / or a heat exchanger (5, 9) preferred for its purification

discontinuously, more preferably pneumatically from the heat exchanger (5, 9) is removable and recyclable.

5. Apparatus according to claim 4, characterized in that the storage mass is traceable to a hot zone of a bed.

6. Device according to one of the preceding claims, characterized in that it comprises a third bed (12) of a thermal storage mass.

7. The device according to claim 6, characterized in that the third bed (12) is so incorporated into a piping system of the device that they regardless of the direction of flow of the gas through the first and second bed and / or the first and second heat exchanger (5 , 9) can only be flowed through by a purge gas and / or gas from the reactor.

8. Device according to one of the preceding claims, characterized in that it comprises a purge gas supply line (13), by means of at least one

Bed and / or a heat exchanger (5, 9, 12), preferably all beds and / or heat exchangers (5, 9, 12), a purge gas can be fed.

9. Apparatus according to claim 7 or 8, characterized in that the purge gas is inert gas, water vapor and / or in the reactor (7) treated gas.

10. A method for cracking gases in the with a feed line (1)

carbon-containing gas is first fed to a first heat exchanger (5, 9) with a bed of a thermal storage mass, then a first combustion chamber (6, 8) is fed, in which by substoichiometric oxygen supply, a partial oxidation of the carbonaceous gas is carried out, and then the carbonaceous gas is introduced into a reactor (7),

characterized in that

the carbonaceous gas is fed after treatment in the reactor (7) a second combustion chamber (6, 8), in the substoichiometric

Oxygen supply for another, oxygen-containing gas, a partial oxidation of the carbon-containing gas is carried out, and from this combustion chamber, the gas is passed through a second heat exchanger (5, 9) with a bed of thermal storage mass, wherein the flow direction of the carbon-containing gas after a certain Time interval is reversed at least in a region which includes the first and second bed (5, 9), the first and second combustion chamber (6, 8) and the reactor (7).

1 1. A method according to claim 10, characterized in that during a

Flow reversal a third storage mass (12) is temporarily added.

12. The method according to claim 10 or 1 1, characterized in that

Passing the carbonaceous gas through at least one of

Heat exchanger (5, 9, 12) with beds of a storage mass, the carbon-containing gas passed through at a heating rate of at least 2000 K / s, preferably at least 3000 K / s and more preferably at least 4000 K / s is heated.

13. The method according to claim 10,

characterized in that the reversal of the flow direction is carried out by means of at least one valve and preferably by means of a plurality of valves.