Reaction device, feed lance, and method for thermally decomposing organic compounds

Abstract

The present invention relates to a reaction device (100) for thermally decomposing organic compounds, in particular halogenated organic compounds, comprising: - at least one reaction chamber (102) which has a central longitudinal axis (104) and a main flow direction (106) which is oriented at least approximately in parallel with the central longitudinal axis (104); and - at least one reaction head for feeding at least one fuel and at least one oxidant into the at least one reaction chamber (102), at least one local reaction zone (128) in which the organic compounds can be decomposed being formed in the at least one reaction chamber (102), and the at least one reaction head being arranged at least in part in the at least one reaction chamber (102). The present invention also relates to a corresponding method for decomposing organic compounds, in particular halogenated organic compounds, and to a feed lance (112) for a reaction device (100).

Description

[0001] Reaction device, feed lance and method for the thermal decomposition of organic compounds

[0002] The present invention relates to a reaction device for the thermal decomposition of organic compounds. Furthermore, the present invention relates to a corresponding method for the decomposition of organic compounds. Furthermore, the present invention relates to a feed lance for a corresponding reaction device.

[0003] In this description and the appended claims, an organic compound is understood to mean in particular a halogenated organic compound and preferably an at least partially fluorinated organic compound.

[0004] In practice, various approaches are known for the treatment or post-treatment, in particular decomposition or decomposition, of organic compounds.

[0005] Such post-treatment of organic compounds is carried out, for example, in thermal afterburning plants or thermal exhaust gas purification plants, in which industrial exhaust gases or wastewater from industrial processes are post-treated.

[0006] One of these post-treatment approaches is the thermal decomposition of organic compounds, whereby decomposition towards the reaction product HF is preferably aimed for and thus decomposition towards toxic reaction products such as CF4 is to be avoided.

[0007] Important parameters in thermal decomposition, which can significantly influence the formation of the desired reaction products, are in particular the temperature and the H concentration, but depending on the post-treatment to be carried out, also, for example, a hydrogen fluoride concentration and / or a concentration of other compounds to be reacted.

[0008] In order to reduce the necessary reaction temperature during thermal decomposition and thus expose the corresponding plant or device to a lower temperature, catalysts can be used.

[0009] However, the reactions associated with the use of catalysts are often not very stable and are also sensitive.

[0010] Another approach could be a thermal plasma process, as described in the following article:

[0011] Sun, JW., Park, DW. CF4 decomposition by thermal plasma processing. Korean J. Chem. Eng. 20, 476-481 (2003).

[0012] However, the approach of a thermal plasma process is probably limited to low treatment capacity and higher costs.

[0013] In general, if organic compounds are to be thermally decomposed, very high temperatures and longer residence times are required, since compounds such as CF4 and C2F6, in particular, require very high temperatures for the decomposition reactions to occur. In addition to very high reaction temperatures, a sufficiently high H concentration is also necessary to ensure that the product reacts to HF and not to CF2O or even CF4.

[0014] In some reactions of organic compounds, the temperature can be increased with oxygen and hydrogen, whereas in other reactions the temperature can be decreased.

[0015] With regard to reaction temperatures, however, it should be noted that due to the limited durability or temperature resistance of the insulating material of the reaction device or burner device in question, a specified temperature level may not be exceeded in order to avoid causing damage, which is why the desired reaction product HF cannot be achieved in thermal afterburning plants using high temperatures alone.

[0016] For example, the minimum temperature at which the equilibrium constant exceeds 1 is approximately 1720 K for the following reaction equation:

[0017] CF4+ 2H24HF + C .

[0018] This minimum temperature of 1720 K is higher than the temperatures typically found in a combustion chamber of a thermal afterburner plant.

[0019] Therefore, as is generally known, H2O is added to the decomposition process of CF4 to increase the decomposition rate to HF, which can simultaneously reduce the CF4 concentration. In other words, the addition of H2O to a thermal decomposition process causes a shift in the decomposition rate from CHF to more HF, which in turn means that less CF4 is produced.

[0020] It should also be noted, however, that exhaust gases or liquid waste often contain a significant inert component, such as N2 or CO2. As a result, even in an exothermic reaction, the average temperature in the reaction zone can be lower than the average temperature within the reaction device or burner device.

[0021] Furthermore, it should be considered that exhaust gases or liquid waste in industrial processes are often not constant in terms of their composition and / or flow rate. Furthermore, exhaust gases or liquid waste may contain large amounts of non-reacting components such as N2, CO2, etc., and may also contain additional elements such as sulfur.

[0022] For the reasons mentioned above, the use of catalysts in thermal decomposition or the aforementioned plasma decomposition approach therefore appear to be unsuitable overall when it comes to efficiently and repeatably thermally decomposing or splitting organic compounds into HF. The high flow rates required also make the use of catalysts in thermal decomposition and the plasma decomposition approach impractical.

[0023] The general design of a thermal incinerator or direct fired thermal oxidizer (DFTO) typically consists of a reaction device with a reaction chamber and a reaction head, or a burner device with a burner head and a combustion chamber, providing a predetermined base temperature prevailing in the controlled reaction chamber.

[0024] In this description and the appended claims, the term "reaction device" refers to a device in which at least one substance, preferably a fuel such as natural gas, reacts with at least one oxidizer. The reaction can occur by combustion or flamelessly, which is why a burner device is intended to represent a specific reaction device.

[0025] The exhaust gases or wastewater to be decomposed can be fed into the reaction device directly via the reaction head or by means of additional lances into the reaction chamber.

[0026] If the flow rates are not too high, the exhaust gas or waste water can be injected via the reaction head.

[0027] Alternatively, the one or more lances can be installed and / or aligned so that the injected exhaust gas or wastewater impinges on the main flame at the burner head of a burner device. However, this can cause the main flame to become unstable or too cold. To ensure a specified process stability of the reaction device, the injections are preferably carried out via lances downstream of the burner head or downstream of the main flame. This allows the exhaust gas or wastewater to mix with the flue gas downstream of the burner head, and the desired reactions can be enforced.

[0028] Nevertheless, due to the variable or uncertain flow velocities of the exhaust gas or wastewater, the reaction temperature required for decomposition may be too low or there may be too few H atoms in the environment of the actual decomposition reactions to decompose organic compounds sufficiently towards the desired product HF.

[0029] In addition, additional combustion flames arranged in or extending into the reaction chamber or combustion chamber can increase HF production, but require greater structural effort.

[0030] The present invention is therefore based on the object of providing a reaction device with which an improved reaction mechanism for decomposing organic compounds, in particular halogenated organic compounds and preferably at least partially fluorinated organic compounds, can be realized.

[0031] This object is achieved according to the invention by a reaction device having the features according to claim 1.

[0032] The reaction device is used to decompose organic compounds in an industrial process, such as fluorinated compounds.

[0033] According to the invention, the reaction device comprises the following: at least one reaction chamber having a central longitudinal axis and a main flow direction oriented at least approximately parallel to the central longitudinal axis; and at least one reaction head for supplying at least one fuel and at least one oxidizer into the at least one reaction chamber, wherein at least one local reaction zone in which the organic compounds are decomposable is formed in the at least one reaction chamber, and wherein the at least one reaction head is arranged at least partially in the at least one reaction chamber.

[0034] The present invention is based on the fundamental idea of ​​creating a local reaction zone with a high temperature and a high H2O concentration within a reaction chamber or combustion chamber, in which at least one fuel reacts or is burned with at least one oxidizer, in order to achieve an improved reaction mechanism for the decomposition of fluorinated organic compounds (CHF) to HF. For this purpose, a feed lance is preferably provided, which has a feed volume and several separate feed pipes arranged in the feed volume. An H donor, such as H2, natural gas, liquefied petroleum gas, or methane, is introduced into the local reaction zone via at least one of these feed pipes to ensure that sufficient potential thermal or chemical energy is available. Consequently, the minimum volume required to form a sufficiently hot local reaction zone can be controlled via the feed.The organic compounds to be decomposed are also introduced into the local reaction zone via one or more separate feed pipes, whereas additional water vapor is introduced towards the local reaction zone via the feed volume of the lance so that sufficient H atoms are present in the local reaction zone.

[0035] It must be taken into account that the molecules of the organic compounds generally have a higher density than the other components supplied via the feed lance and can therefore flow deeper into the reaction chamber. Therefore, the design must ensure that, for example, the lighter H2O or the lighter natural gas as fuel are injected or sprayed into the local reaction zone in such a way that they can react with the molecules of the organic compounds in the local reaction zone.

[0036] The terms "fuel", "fuel gas", "natural gas", "liquefied petroleum gas" and "methane" are used largely synonymously in this description and the appended claims, unless explicitly stated otherwise.

[0037] Furthermore, the terms "water vapor" and "steam" are used synonymously in this description and the appended claims unless explicitly stated otherwise.

[0038] In an advantageous embodiment, the reaction chamber can be angled, for example, in particular L-shaped. This allows the reaction chamber to be arranged in a space-saving manner in a hall, for example, and / or to prevent or at least reduce backflow, particularly in the direction of the reaction head. Furthermore, an L-shape or similar design can also protect downstream or downstream components from the resulting heat radiation.

[0039] The fuel-carrying pipe(s) of the feed lance can therefore be surrounded by the exhaust gas-carrying pipes, i.e. the feed pipes with organic compounds to be decomposed, or the fuel feed pipes are located on the "wind" or upstream side of the feed lance, i.e. they are subjected to the main flow emanating from the reaction head, so that the fuel is mixed into the zone of the injected or sprayed organic compounds by the main flow.

[0040] Furthermore, the cross-section of the feed lance and the cross-section of the feed pipes must be coordinated in such a way that there is sufficient space for the feed volume between the feed pipes to allow sufficient steam to pass through or through between the feed pipes to the local reaction zone.

[0041] It may also be advantageous if the reaction device has one or more nozzles, by means of which, in particular, additional water can be injected, preferably a) into the inlet or passage area of ​​feed lances into the reaction chamber and / or b) into an area within the reaction chamber directly adjacent to this inlet or passage area. This can serve, in particular, to apply a higher water concentration to the local reaction zone.

[0042] In order to achieve greater process stability and a sufficient decomposition quality of the organic compounds, a minimum flow of the fuel can be controlled via the feed lance alternatively or additionally, whereby the flow velocity of the fuel represents a process variable.

[0043] It may be preferred if the local reaction zone does not abut or adjoin the inner surface of the reaction chamber in order to prevent the insulation of the reaction chamber from being impaired.

[0044] It may be advantageous if the at least one reaction chamber is cylindrical and the at least one reaction head is arranged on a base surface of the at least one reaction chamber.

[0045] A cylindrical reaction chamber can preferably be understood as a hollow body comprising a lateral surface whose points are equidistant from a central longitudinal axis. This lateral surface is bounded in its longitudinal extent, i.e., along the central longitudinal axis, preferably by two circular cover surfaces that are congruent and aligned parallel to one another. Such a cylindrical reaction chamber is accordingly preferably defined by its length or height, i.e., the extent of the central longitudinal axis, as well as the radius of the cover surfaces. The length or height of the cylindrical reaction chamber is preferably greater than the radius of the cover surfaces.

[0046] However, a cylindrical reaction chamber can also be defined as an axially symmetric hollow body with a cross-section perpendicular to its axis of symmetry, for example a circular cross-section, and a length aligned along the axis of symmetry, wherein at least an average value of a distance of a circumferential line of the cross-section perpendicular to the axis of symmetry is smaller than the length of the body.

[0047] The reaction chamber should preferably be understood as the interior or inner cavity of the reaction device. Consequently, the reaction device can follow the shape of the reaction chamber and even be cylindrical. However, it is also possible for the reaction device to have a different shape, for example, due to the insulation surrounding or enclosing the reaction chamber.

[0048] It may also be advantageous if at least one feed lance is arranged on the at least one reaction chamber, in particular on a jacket wall of the reaction chamber, by means of which the local reaction zone can be formed.

[0049] In a further embodiment of the invention, it can be provided that the at least one feed lance comprises the following: at least one feed volume via which steam, in particular water vapor, can be fed into the local reaction zone; one or more first feed pipes which are arranged in the feed volume and via which organic compounds can be fed into the local reaction zone; and one or more second feed pipes which are arranged in the feed volume and via which fuel, in particular natural gas, can be fed into the local reaction zone. In a further embodiment of the invention, it can be provided that the at least one feed lance is oriented in a transverse direction which runs transversely, in particular perpendicularly, to the main flow direction.

[0050] It can further be provided that a) the one or more second supply pipes are arranged, with respect to the main flow direction, at least in sections upstream of the one or more supply pipes; and / or b) the one or more first supply pipes surround the one or more second supply pipes.

[0051] This ensures that sufficient fuel is available in the local reaction zone to increase the reaction temperature. The water vapor supplied via the feed volume envelops the supplied fuel and organic compounds, ensuring that no hot strands from the local reaction zone touch the inner surface of the reaction chamber.

[0052] It may be advantageous if the local reaction zone can be formed at least approximately tangentially and / or at least approximately along an inner surface of the reaction chamber.

[0053] In a further embodiment of the invention, it can be provided that the reaction device comprises one or more fresh air lances by means of which fresh air can be introduced into the reaction chamber.

[0054] It may also be advantageous if the fresh air lances are arranged upstream and / or downstream of the at least one supply lance, relative to the main flow direction.

[0055] The fresh air supplied via the fresh air lances can be used to protect specific sections of the reaction chamber by lowering the local temperature, and the position or swirl direction of the local reaction zone can be influenced or varied. The flow of the fuel and oxidizer mixture supplied via the reaction head is generally highly constricted within the reaction chamber, which can be enhanced by ensuring that the components supplied via the at least one supply lance, such as steam, organic compounds, and fuel, preferably flow at least approximately tangentially into the reaction chamber.

[0056] It may be advantageous if the reaction head is designed as a swirl burner device. This preferably entrains the fuel and oxidizer during and / or immediately after feeding into the reaction chamber, increasing mixing.

[0057] The object is further achieved according to the invention by a thermal combustion plant which comprises at least one reaction device according to the invention.

[0058] Furthermore, the object is achieved according to the invention by a feed lance for a reaction device, in particular a feed lance for a reaction device for the thermal decomposition of organic compounds.

[0059] Such a feed lance comprises the following: at least one feed volume through which steam, in particular water vapor, can be fed; one or more first feed pipes arranged in the feed volume and through which organic compounds can be fed; and one or more second feed pipes arranged in the feed volume and through which fuel, in particular natural gas, can be fed.

[0060] One or more feed lances can not only be arranged or installed in and / or on the reaction device according to the invention, but are preferably suitable for retrofitting in existing reaction devices.

[0061] It may be advantageous if the feed lances arranged in and / or on a reaction device are interchangeable. A feed lance can be exchanged for a similar feed lance, ie, a lance with the same configuration of feed tubes, or a different feed lance, ie, for example, a lance having a different number of first and / or second feed tubes and / or first and / or second feed tubes of a different design.

[0062] The operation of such a feed lance results in a corresponding method for feeding steam, organic compounds and fuel into a local reaction zone of a reaction device.

[0063] The corresponding procedure includes the following steps, which preferably run in parallel:

[0064] Supplying steam, in particular water vapor, via the supply volume of a supply lance into the local reaction zone;

[0065] Feeding organic compounds into the local reaction zone via one or more first feed tubes of the feed lance arranged in the feed volume; and

[0066] Supplying fuel, in particular natural gas, into the local reaction zone via one or more second supply pipes of the supply lance, which are also arranged in the supply volume

[0067] Furthermore, the object is achieved according to the invention by a process for the thermal decomposition of organic compounds, in particular halogenated organic compounds.

[0068] The procedure includes the following steps:

[0069] Feeding at least one fuel and at least one oxidizer into a reaction chamber to form a controlled reaction flow along a main flow direction; and

[0070] Feeding organic compounds into the reaction chamber in a transverse direction to form a local reaction zone in which the organic compounds are decomposed.

[0071] It may be advantageous if the organic compounds are supplied to the reaction chamber via at least one supply lance. Furthermore, it may be provided that fuel and / or steam, preferably water vapor, is additionally supplied to the reaction chamber and / or the local reaction zone in the reaction chamber via the at least one supply lance.

[0072] It may also be advantageous if the local reaction zone is formed at least approximately tangentially and / or along an inner surface of the reaction chamber.

[0073] In a further embodiment of the invention, it can be provided that fresh air is supplied to the reaction chamber via one or more fresh air lances which are arranged upstream and / or downstream of the at least one supply lance with respect to the main flow direction, wherein the fresh air is preferably guided at least approximately tangentially into the reaction chamber.

[0074] The methods preferably have one or more of the features and / or advantages described in connection with the reaction device or the feed lance. Furthermore, the reaction device or the feed lance preferably have one or more of the features and / or advantages described in connection with the methods.

[0075] Further features and / or advantages of the invention are the subject of the following description and the drawings of exemplary embodiments.

[0076] The figures show:

[0077] Fig. 1 is a schematic, perspective view of a first embodiment of a reaction device according to the invention;

[0078] Fig. 2 is a schematic partial view of the first embodiment of Fig. 1;

[0079] Fig. 3 is a further schematic partial view of the first embodiment from Fig.

[0080] 1 ;

[0081] Fig. 4 is a schematic partial sectional view of the first embodiment of Fig. 3; Fig. 5 is a schematic perspective view of the first embodiment of Fig. 1 with a local reaction zone;

[0082] Fig. 6 is a schematic cross-sectional view of the first embodiment of Fig. 5; and

[0083] Fig. 7 is a schematic perspective view of a second embodiment of a reaction device.

[0084] Identical or functionally similar elements are provided with the same reference numerals in all figures.

[0085] Figures 1 to 6 show a first embodiment of a reaction device designated as a whole by 100.

[0086] The reaction device 100 essentially serves for the thermal decomposition of organic compounds, preferably at least partially fluorinated organic compounds, CHF for short.

[0087] The reaction device 100 includes a reaction chamber 102 and a reaction head (not shown).

[0088] The reaction chamber 102 has a central longitudinal axis 104 and a main flow direction 106, wherein the main flow direction 106 runs at least approximately parallel to the central longitudinal axis 104.

[0089] The reaction chamber 102 is preferably cylindrical, with the reaction head being arranged on one of the two base surfaces 108.

[0090] The reaction head serves to supply at least one fuel, such as natural gas, and at least one oxidizer, such as fresh air, into the reaction chamber 102, where the fuel and oxidizer react with each other in a controlled manner, preferably being combusted, and a reaction-dependent base temperature is established. The reaction head is at least partially arranged within the reaction chamber 102 or extends at least partially into it.

[0091] If the reaction device 100 is designed as a burner device, a main flame would be anchored at the burner head by the combustion of fuel and oxidizer, which would burn within the combustion chamber 102.

[0092] The reaction chamber 102 is preferably encased internally and / or externally by at least one insulation layer 110, which at least partially thermally shields or insulates the thermal combustion and decomposition processes in the reaction chamber 102 from the environment of the reaction device 100.

[0093] The reaction device 100 further comprises a feed lance 112, by means of which organic compounds, fuel and / or steam, in particular water vapor, can be fed into the reaction chamber 102 in a transverse direction 114, which is oriented transversely, in particular perpendicularly, to the main flow direction 106.

[0094] The feed lance 112, which is preferably tubular, extends through a jacket wall 115 of the reaction chamber 102 and the insulation layer 110.

[0095] The feed lance 112 comprises a feed volume 116.

[0096] Furthermore, the feed lance 112 comprises a plurality of first feed pipes 118 and a second feed pipe 120, which are arranged in the feed volume 116.

[0097] Organic compounds are supplied to the first feed pipes 118 via first inlet openings 122, whereas fuel, such as natural gas, methane or liquid gas, is supplied to the second feed pipe 120 via a second inlet opening 124.

[0098] Steam, preferably water vapor, is supplied to the feed volume 116 via a side opening 126. The organic compounds, the fuel, and the water vapor flow via the feed lance 112 into the reaction chamber 102, where they form a local reaction zone 128.

[0099] In the local reaction zone 128, therefore, not only the organic compounds to be decomposed are present, but also a fuel by means of which the reaction temperature is increased in a spatially limited manner, as well as sufficient hydrogen so that all the necessary conditions prevail for organic compounds to be decomposed into HF and for as little CF4 as possible to be formed.

[0100] The organic compounds flow through the first feed tubes 118 via first outlet openings 130 into the reaction chamber 102.

[0101] The fuel flows through the second supply tube 120 via a second outlet opening 132 into the reaction chamber 102.

[0102] The water vapor flows through the feed volume 116 via an end 134 of the feed lance 112 into the reaction chamber 102.

[0103] Preferably, the supplied water vapor envelops the fuel and the organic compounds.

[0104] The first outlet openings 130, the second outlet opening 132 and the end 134 of the feed lance 112 are adapted to the geometry of the inner surface 136 of the reaction chamber 102 and do not protrude beyond the plane of the inner surface 136 into the reaction chamber 102, whereby the flow within the reaction chamber 102 is not impaired or influenced by sections of the feed lance 112 protruding into the reaction chamber 102.

[0105] The cross-section of the second feed pipe 120 is preferably smaller than the cross-section of the first feed pipes 118.

[0106] As can be seen particularly in Figs. 2 and 3, the second supply pipe 120 is arranged, at least in sections, upstream of all first supply pipes 118 with respect to the main flow direction 106. The steam is preferably supplied at a temperature of 150°C, and the base temperature in the reaction chamber 102 is in the range of 1000°C to 1300°C, preferably 1100°C to 1200°C.

[0107] Simulation results show that when pure fluorinated organic compounds are fed into the reaction chamber 102 via the feed lance 112, approximately 97% HF and 3% CF4 are produced in the decomposition reaction, which is preferably a combustion reaction.

[0108] Using steam, the proportion of HF can be increased to 99.5% and the proportion of CF4 can be reduced accordingly to 0.5%.

[0109] If methane is added to the water vapor at a flow velocity of approximately 10 m / s, the HF content during decomposition increases to 99.8% and the CF4 content decreases to 0.2%.

[0110] Increasing the methane flow velocity to 20 m / s during feeding leads to a further increase in the HF content to almost 99.9% and accordingly to a CF4 content of 0.1%.

[0111] Fig. 6 shows that the local reaction zone 128 introduced into the reaction chamber 102 via the feed lance 112 is initially formed along the inner surface 136, thereby causing a swirling flow around the central longitudinal axis 104.

[0112] The organic compounds, the fuel and the water vapor preferably flow approximately tangentially into the reaction chamber 102.

[0113] While the flow velocity of the fuel and oxidizer supplied via the reaction head in the main flow direction 106 is, for example, 5 m / s, the flow velocity of said swirl flow is preferably 15 m / s.

[0114] Fig. 7 shows a second embodiment of a reaction device 100 according to the invention. The second embodiment differs from the first embodiment in that the reaction device 100 has four fresh air lances 138.

[0115] Two of these fresh air lances 138, which form a first pair 140 and preferably have a smaller cross-section than the two remaining fresh air lances 138, are arranged, relative to the main flow direction 106, between the feed lance 112 and the base surface 108 of the reaction chamber 102, on which the reaction head is arranged.

[0116] The fresh air lances 138 of the first pair 140 are located at least approximately opposite one another with respect to the central longitudinal axis 104, and the fresh air lances 138 are arranged offset from one another with respect to the main flow direction 106.

[0117] By means of the first pair 140, fresh air is supplied or guided into the reaction chamber 102 in order to reduce the temperature, particularly in the zones within the reaction chamber 102 which border on the base area 108, and thus to protect components of the reaction chamber 102.

[0118] The fresh air is introduced into the reaction chamber 102 via the fresh air lances 138, preferably tangentially.

[0119] The fresh air lances 138 of a second pair 142 are arranged downstream and upstream of the supply lance 112 with respect to the main flow direction 106 and are also arranged at least approximately opposite one another.

[0120] By means of the second pair 142 of fresh air lances 138, the swirl flow induced by the local reaction zone 128 along the inner surface 136 can be varied with respect to the main flow direction 106. List of reference symbols

[0121] reaction device

[0122] Reaction chamber central longitudinal axis

[0123] Main flow direction

[0124] Floor area

[0125] Insulation layer

[0126] Feed lance

[0127] Transverse direction

[0128] Shell wall

[0129] Feed volume first feed pipe second feed pipe first inlet opening second inlet opening

[0130] Side opening local reaction zone first outlet opening second outlet opening

[0131] End of the feed lance

[0132] Inner surface of the combustion chamber

[0133] Fresh air lance first fresh air lance pair second fresh air lance pair

Claims

Patent claims 1. A reaction device (100) for the thermal decomposition of organic compounds, in particular halogenated organic compounds, comprising: at least one reaction chamber (102) having a central longitudinal axis (104) and a main flow direction (106) oriented at least approximately parallel to the central longitudinal axis (104); and at least one reaction head for supplying at least one fuel and at least one oxidizer into the at least one reaction chamber (102), wherein at least one local reaction zone (128) in which the organic compounds are decomposable is formed in the at least one reaction chamber (102), and wherein the at least one reaction head is arranged at least partially in the at least one reaction chamber (102).

2. Reaction device (100) according to claim 1, characterized in that the at least one reaction chamber (102) is cylindrical and the at least one reaction head is arranged on a base surface (108) of the at least one reaction chamber (102).

3. Reaction device (100) according to claim 1 or 2, characterized in that at least one feed lance (112) is arranged on the at least one reaction chamber (102), in particular on a jacket wall (115) of the reaction chamber (102), by means of which the local reaction zone (128) can be formed.

4. Reaction device (100) according to claim 3, characterized in that the at least one feed lance (112) comprises the following: at least one feed volume (116) via which steam, in particular water vapor, can be fed into the local reaction zone (128); one or more first feed tubes (118) which are arranged in the feed volume (116) and via which organic compounds can be fed into the local reaction zone (128); and one or more second feed pipes (120) which are arranged in the feed volume (116) and via which fuel, in particular natural gas, can be fed into the local reaction zone (128).

5. Reaction device (100) according to claim 3 or 4, characterized in that the at least one feed lance (112) is aligned in a transverse direction (114) which runs transversely, in particular perpendicularly, to the main flow direction (106).

6. Reaction device (100) according to one of claims 3 to 5, characterized in that a) the one or more second feed pipes (120) are arranged, with respect to the main flow direction (106), at least in sections upstream of the one or more feed pipes (118); and / or b) the one or more first feed pipes (118) surround the one or more second feed pipes (120).

7. Reaction device (100) according to one of claims 1 to 6, characterized in that the local reaction zone (128) can be formed at least approximately tangentially and / or at least approximately along an inner surface (136) of the reaction chamber (102).

8. Reaction device (100) according to one of claims 1 to 7, characterized in that the reaction device (100) comprises one or more fresh air lances (138) by means of which fresh air can be introduced into the reaction chamber (102).

9. Reaction device (100) according to claim 8, characterized in that the fresh air lances (138) are arranged upstream and / or downstream of the at least one supply lance (112) with respect to the main flow direction (106).

10. Feed lance (112) for a reaction device (100), in particular for a reaction device (100) for the thermal decomposition of organic Connections, for example for a reaction device (100) according to one of claims 1 to 9, wherein the feed lance (112) comprises the following: at least one feed volume (116) via which steam, in particular water vapor, can be fed; one or more first feed pipes (118) which are arranged in the feed volume (116) and via which organic compounds can be fed; and one or more second feed pipes (120) which are arranged in the feed volume (116) and via which fuel, in particular natural gas, can be fed.

11. A method for supplying steam, organic compounds and fuel into a local reaction zone (128) of a reaction device (100) by means of at least one supply lance (112) according to claim 10, the method comprising the following steps: Supplying steam, in particular water steam, via the at least one supply volume (116) of the at least one supply lance (112) into the local reaction zone (128); Feeding organic compounds into the local reaction zone (128) via the one or more first feed tubes (118) of the at least one feed lance (112) arranged in the feed volume (116); and Supplying fuel, in particular natural gas, into the local reaction zone (128) via the one or more second supply pipes (120) of the at least one supply lance (112) which are arranged in the supply volume (116).

12. Thermal combustion plant comprising at least one reaction device according to one of claims 1 to 9.

13. A process for the thermal decomposition of organic compounds, in particular halogenated organic compounds, the process comprising the following steps: Feeding at least one fuel and at least one oxidizer into a reaction chamber (102) to form a controlled reaction flow along a main flow direction (106); and feeding organic compounds into the reaction chamber (102) in a transverse direction (114) to form a local reaction zone (128) in which the organic compounds are decomposed.

14. The method according to claim 13, characterized in that the organic compounds are fed to the reaction chamber (102) via at least one feed lance (112).

15. The method according to claim 13 or 14, characterized in that additional fuel and / or steam, preferably water vapor, is supplied to the reaction chamber (102) and / or the local reaction zone (128) in the reaction chamber (102) via the at least one supply lance (112).

16. Method according to one of claims 13 to 15, characterized in that the local reaction zone (128) is formed at least approximately tangentially and / or along an inner surface (136) of the reaction chamber (102).

17. The method according to any one of claims 13 to 16, characterized in that fresh air is supplied to the reaction chamber (102) via one or more fresh air lances (138) which are arranged upstream and / or downstream of the at least one supply lance (112) with respect to the main flow direction (106), wherein the fresh air is preferably guided at least approximately tangentially into the reaction chamber (102).

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