Device and method for the pyrolysis of hydrogen-containing compounds

Abstract

The invention relates to a device (1) for generating hydrogen (H2) and solid carbon (11) by thermal decomposition of a feed gas (Z) containing hydrocarbons, the device comprising: a pyrolysis reactor (2) with a reaction chamber (3a) and a collection chamber (5a) arranged above the reaction chamber (3a), the reaction chamber (3a) containing a liquid high-temperature heat carrier (6); a reactor feed line (7) leading into the reaction chamber (3a); a feed (19) for the feed gas (Z), the feed (19) being fluidically connected to the reactor supply line (7); a heating device (4) in order to supply heat to the reaction chamber (3a); a discharge device (12), arranged in the collection chamber (5a), for discharging a substance mixture (S) from the collection chamber (5a); a separation device (37) arranged outside the pyrolysis reactor (2), the discharge device (12) being connected to the separation device (37) via a discharge line (14), and the separation device (37) being designed to separate the substance mixture (S) into at least the components of solid carbon (11) and hydrogen (H2) or a gas mixture containing hydrogen (H2); and also a compressor (23) for compressing the fluid supplied to the reactor feed line (7).

Description

[0001] DEVICE AND METHOD FOR PYROLYSIS OF HYDROGEN-CONTAINING COMPOUNDS

[0002] The invention relates to a device and a method for the pyrolysis of hydrogen-containing compounds.

[0003] To achieve climate protection goals, technological solutions that allow the continued use of fossil resources while simultaneously avoiding CO2 emissions are of particular interest. One promising technical solution enables the decarbonization of hydrogen-containing compounds, particularly hydrocarbons such as natural gas or methane, by converting the hydrogen-containing compound into at least pure solid carbon and hydrogen using a cracking / pyrolysis reaction. For methane, the basic formula is as follows:

[0004] CH4C + 2H2with AH = 74.5 kJ / mol

[0005] Temperatures above 500 °C are required to carry out this reaction, with the energy input being sufficient to break the strong molecular CH bonds (437 kJ / mol). Experimental analyses have shown that reaction rates of over 95% are achievable under thermodynamic equilibrium conditions at temperatures up to 1100 °C.

[0006] Document WO 2019 / 154732A1 discloses a method and a device for the pyrolysis of hydrogen-containing compounds using a liquid metal reactor. This known method and device are only partially suitable for the continuous processing of hydrogen-containing compounds on an industrial scale. Therefore, further improvement of the reaction control in the production of hydrogen by methane pyrolysis is required.

[0007] The object of the invention is to provide a more advantageous device or a more advantageous process for producing hydrogen from a hydrogen-containing compound, in particular from methane.

[0008] This object is achieved by a device having the features of claim 1. The dependent claims relate to further advantageous embodiments of the device. The object is further achieved by a method having the features of claim 13. The dependent claims relate to further advantageous method steps.

[0009] The object is achieved in particular with a device for producing hydrogen and solid carbon by thermal decomposition of a feed gas containing hydrocarbons, comprising a pyrolysis reactor with a reaction chamber and a collecting chamber arranged above the reaction chamber, wherein the reaction chamber contains a liquid high-temperature heat carrier, as well as comprising a reactor feed line opening into the reaction chamber, as well as comprising a feed for the feed gas, wherein the feed is fluidically connected to the reactor feed line, as well as comprising a heating device for supplying heat to the reaction chamber, as well as comprising a discharge device arranged in the collecting chamber for discharging a mixture of substances from the collecting chamber, as well as comprising a separation device arranged outside the pyrolysis reactor, wherein the discharge device is connected to the separation device via a discharge line,and wherein the separation device is designed to separate the substance mixture into at least the components solid carbon and hydrogen, or solid carbon and a gas mixture containing hydrogen, and comprising a compressor for compressing the fluid supplied to the reactor feed line.,

[0010] The object is further achieved in particular with a method for the direct thermal decomposition of a hydrogen-containing compound into solid carbon and hydrogen, in that a feed gas containing hydrocarbon is compressed, the compressed feed gas is then passed through a liquid high-temperature heat carrier and the feed gas is converted into a mixture of substances in the high-temperature heat carrier, the mixture of substances is collected above the high-temperature heat carrier in a collecting space, wherein the mixture of substances comprises at least the solid carbon and a gas mixture containing hydrogen, the mixture of substances is fed to a separation device downstream of the collecting space and the mixture of substances is depleted of solid carbon in the separation device, and the depleted mixture of substances and the solid carbon are discharged separately from the separation device.

[0011] The device according to the invention or the method according to the invention makes it possible to convert a hydrocarbon gas, preferably methane, into hydrogen and carbon on an industrial scale.

[0012] For the purposes of the present invention, the term "pyrolysis" refers to the thermal decomposition of hydrocarbons, for example methane, in an oxygen-free atmosphere.

[0013] In the device according to the invention, the pyrolysis reactor comprises a liquid metal reactor with a reaction chamber and a collecting chamber arranged above the reaction chamber, wherein the reaction chamber is designed to receive the liquid high-temperature heat transfer medium. The liquid metal reactor comprises an inlet for a feed gas or.a reaction gas, wherein the reaction gas is preferably introduced into the liquid metal reactor from below, wherein the liquid metal reactor preferably has a porous section or a series of openings which are arranged along the lower part of the liquid metal reactor in order to supply the reaction gas distributed over the internal cross-sectional area, preferably substantially uniformly distributed, to the liquid metal reactor from below, so that the supplied reaction gas flows through the liquid high-temperature heat carrier located in the liquid metal reactor and rises in the direction of the collecting space.

[0014] The term “high-temperature heat transfer medium” in the context of the present invention is to be understood as meaning a heat transfer medium with high thermal stability. The high-temperature heat transfer medium is preferably a metal or salt melt. Metal melts are preferred. The good heat transfer from the metal melt to the reaction gas is particularly advantageous. Another advantage is the possibility of carbon separation due to the density differences between the metal melt and carbon. The metal melt is preferably a metal or a metal alloy. A suitable metal melt is preferably selected from the group comprising lead-tin solders, lead-free solders, tin and / or magnesium. Lead-tin solders have low melting points and thus allow the formation of a homogeneous metal melt even at temperatures around 200 °C.For example, seepage solder with a composition of 63% tin and 37% lead and a eutectic point at 183 °C represents such a well-suited lead-tin solder. Within the scope of the invention, the high-temperature heat transfer medium is preferably not circulated. Particularly preferably, the high-temperature heat transfer medium is kept stationary; it is particularly preferably located only in the reaction chamber.

[0015] Further preferred is the use of catalytic additives to the high-temperature heat transfer medium, in particular to a metal melt, for example additions of bismuth, copper / nickel, or copper / silver. By using catalytic additives to a metal melt, the reaction temperature can be lowered or the reaction conversion increased. Furthermore, enriching the metal melt with formed carbon particles can also exert an autocatalytic effect. The conversion can be further increased by an additional catalytic effect of the metal melt.

[0016] In the process for producing hydrogen by thermal decomposition of a hydrogen-containing compound in the pyrolysis reactor, the hydrogen-containing compound supplied as reaction gas is brought into contact with the liquid high-temperature heat carrier, wherein the residence time of the reaction gas in the liquid high-temperature heat carrier is preferably adjustable.

[0017] Pyrolysis, in which the reaction gas is brought into contact with a liquid high-temperature heat transfer medium, has the advantage of good heat transfer from the molten metal to the reaction gas. The liquid high-temperature heat transfer medium, for example a melt, is mobile and allows flow through it, so that the gaseous hydrogen-containing compound, for example methane, moves in an upward motion through the melt and, through this movement, ensures constant renewal of the surface. The possibility of controlling the pressure and / or the amount of reaction gas supplied in the process according to the invention allows the convective heat input to be controlled or influenced in a controlled manner.The residence time of the gaseous hydrogen-containing compound in the liquid high-temperature heat transfer medium can be adjusted by the pressure of the supplied reaction gas and / or the quantity of the supplied reaction gas and / or the pressure prevailing in the collection chamber. Increasing the residence time has the advantage of significantly increasing the thermal decomposition conversion.

[0018] In a preferred embodiment, the pressure and / or flow rate is adjusted using a compressor and / or controllable valves. It may also prove advantageous to supply inert gases such as nitrogen or argon to the pyrolysis reactor to control the reaction.

[0019] The flow rate of the reaction gas in the high-temperature heat transfer medium can preferably be adjusted via the pressure difference between the pressure of the reaction gas fed into the reaction chamber and the pressure in the collecting chamber. In addition, it is possible to adjust the height of the reaction chamber or the fill level of the liquid high-temperature heat transfer medium or to design it such that a desired flow rate of the reaction gas in the melt is achieved. In preferred embodiments, the residence time of the gaseous hydrogen-containing compound in the liquid high-temperature heat transfer medium is in the range from 0.01 s to 1000 s, preferably in the range from 0.1 s to 100 s, and preferably in the range from 0.2 s to 10 s.

[0020] In preferred embodiments, the decomposition of the hydrogen-containing compound occurs at a temperature in the range of 500°C to 1500°C, preferably in the range of 900°C to 1400°C, and preferably in the range of 1000°C to 1200°C. Decomposition of the gas at a temperature of approximately 500°C is made possible, for example, by catalytic activity of the melt.

[0021] The required reaction heat is conveniently supplied by combustion of a small portion of the hydrogen produced or another fuel. Electrical heating of the reaction chamber can also be provided.

[0022] Preferred hydrogen-containing compounds are selected from the group comprising methane, ethane, higher hydrocarbons, hydrogen sulfide, ammonia, and / or mixtures thereof. For the purposes of the present invention, the term "higher hydrocarbons" refers to hydrocarbons from propane upwards, in particular alkanes and mixtures thereof. Suitable hydrocarbon mixtures include, for example, raw biogas or raw natural gas mixtures. Liquid hydrocarbons, such as oil, can also be readily used. Liquid hydrocarbons can be rapidly vaporized at the prevailing reaction temperatures. Preferred hydrogen-containing compounds are gaseous hydrogen-containing compounds at ambient temperature, in particular selected from the group comprising methane, ethane, hydrogen sulfide, ammonia, and / or mixtures thereof. Methane is a particularly preferred hydrogen-containing gas.

[0023] The device according to the invention enables pyrolysis by converting a hydrocarbon such as methane into hydrogen and carbon without producing environmentally harmful carbon dioxide. The carbon separated in this way accumulates above the high-temperature heat transfer medium, e.g. the molten metal, and is thus initially located in the collection chamber as part of a mixture of substances comprising at least hydrogen and carbon. In the process according to the invention, the mixture of substances comprising the carbon is removed from the collection chamber and fed to an external separation device downstream of the pyrolysis reactor, in which the mixture of substances is separated at least into carbon and a residual gas. The separation device preferably comprises a degassing vessel designed as a pressure vessel.Advantageously, an additional conveying gas is supplied to the collecting chamber, which in particular has the task of supporting the discharge of the carbon from the collecting chamber. Preferably, the pressure and / or the quantity and / or the flow rate and / or the point of action of the conveying gas is controlled in order to act on the carbon located within the collecting chamber in such a way that the carbon, which is preferably continuously being reformed on the surface, can be reliably removed from the collecting chamber and preferably conveyed into the downstream separation device. It may prove advantageous to provide an additional, preferably controllable compressor and / or a controllable valve in order to control the pressure and / or the quantity of the conveying gas supplied to the collecting chamber.

[0024] The invention is described in detail below using several exemplary embodiments.

[0025] The drawings used to explain the embodiments show:

[0026] Fig. 1 shows a schematically illustrated device of a first embodiment for the pyrolysis of hydrogen-containing compounds;

[0027] Fig. 2 shows a pyrolysis reactor in detail; Fig. 3 shows a separation device in detail; Fig. 4 shows a second embodiment of a device for

[0028] Production of hydrogen and solid carbon.

[0029] In principle, identical parts in the drawings are provided with identical reference symbols.

[0030] Fig. 1 shows a device 1 for producing hydrogen H2 and solid carbon 11 by thermal decomposition of a feed gas Z containing hydrocarbons. The device 1 comprises a pyrolysis reactor 2 with a reaction vessel 3 comprising a reaction chamber 3a and with a collecting vessel 5 arranged above the reaction chamber 3a and comprising a collecting chamber 5a. The reaction chamber 3a is at least partially filled with a liquid high-temperature heat transfer medium 6. A reactor feed line 7 opens into the reaction vessel 3 or into the reaction chamber 3a. An inlet 19 for the feed gas Z is fluidly connected to the reactor feed line 7. A heating device 4 is arranged next to the reaction vessel 3 in order to supply heat to the reaction vessel 3 and thus to the reaction chamber 3a. A discharge device 12 arranged in the collecting space 5a serves to discharge a substance mixture S from the collecting space 5a of the collecting container 5.A separation device 37 arranged outside the pyrolysis reactor 2 and downstream of the pyrolysis reactor 2 in the flow direction of the substance mixture S is connected to the collecting chamber 5a via the discharge device 12 and the discharge line 14, so that the substance mixture S located in the collecting chamber 5a, and in particular the carbon 11 located in the collecting chamber 5a, can be fed to the separation device 37, and is preferably fed automatically. The separation device 37 is designed to separate the substance mixture S into at least the components solid carbon 11 and hydrogen H2, or into the components solid carbon 11 and a gas mixture containing hydrogen H2. The device 1 also comprises a compressor 23 for compressing the fluid supplied to the reactor feed line 7.

[0031] Figure 2 shows the pyrolysis reactor 2 shown in Figure 1 in an enlarged view. The discharge device 12 has the particular purpose of ensuring that the substance mixture S located within the collection chamber 5a, and in particular the carbon 11, is reliably and preferably continuously conveyed out of the collection chamber 5a. In an advantageous embodiment, the discharge device 12 comprises a plurality of collection pipes 12a with inlet openings 12b, which are arranged in the collection chamber 5a. Advantageously, the collection pipes 12a are lance-shaped, with inlet openings 12b directed towards the reaction chamber 3a. In a particularly advantageous embodiment, a gas supply line 8 opens into the collection chamber 5a, the purpose of which is in particular to assist the discharge of the carbon 11 from the collection chamber 5a.In a particularly advantageous embodiment, a gas distribution device 9 is arranged within the collection space 5a between the reaction space 3a and the inlet openings 12b of the discharge device 12, to which a conveying gas F is fed from the gas supply line 8 in order to preferably loosen the carbon 11 located in the collection space 5a by the inflowing conveying gas F and to feed it to the inlet openings 12.

[0032] As can be seen from Figure 1, a compressor 23 is advantageously provided which compresses at least the feed gas Z supplied via the feed 19. The reactor feed line 7 and preferably also the conveying gas feed line 8 are arranged downstream of the compressor in the flow direction of the supplied fluid. Between the compressor 23 and the reactor feed line 7 and / or the conveying gas feed line 8 there is preferably arranged a feed line 15, 15a, 15b which can also be passed through a preheater 16, for example. A first and / or a second valve 17, 18 can also be provided which can preferably be controlled by a control device (not shown), for example to control the pressure or the delivery rate of the feed gas Z conveyed into the reaction chamber 3a and / or to control the pressure or the delivery rate of the conveying gas F passed into the collecting chamber 5a.It may prove advantageous to change the pressure of the conveying gas 5 intermittently, e.g. by periodically switching the conveying gas flow on and off over a predetermined period of time, or by a sequence of pressure fluctuations in the conveying gas flow by appropriately switching the valve 18, in order to thereby swirl up the carbon 11 located in the collecting chamber 5a in particular and thereby assist the discharge of the carbon 11 from the collecting chamber 5a. It may also prove advantageous to connect an additional, preferably controllable compressor to the feed lines 15a, 15b in order to influence and in particular control the pressure difference of the gas between the feed line into the reaction vessel 3 and the collecting chamber 5a.

[0033] In the degassing vessel 25 arranged downstream of the pyrolysis reactor 2, the carbon 11 is separated from the supplied substance mixture S, preferably under pressure. As shown in Figure 1, the separation device 37 comprises a degassing vessel 25 designed as a pressure vessel, wherein the degassing vessel 25 comprises a degassing vessel interior 25a with a lower partial interior 25b and an upper partial interior 25c. The lower partial interior 25b opens into a lock 32 for discharging the preferably dust-like carbon 11. In the degassing vessel interior 25a, a particle filter 27 is advantageously arranged, which divides the degassing vessel interior 25a into the lower partial interior 25b and the upper partial interior 25c, such that the discharge line 14 opens into the lower partial interior 25b via the supply line 14a, wherein a gas outlet 29a arranged in the upper partial interior 25c feeds a gas discharge line 29.Controllable valves 24, 28 can also be provided. The gas outlet 29 preferably opens into a hydrogen separation device 30, which at least partially depletes the supplied fluid of hydrogen and feeds it to a hydrogen outlet 31. The hydrogen separation device 30 preferably comprises a device for pressure swing adsorption (PSA - Pressure Swing Adsorption) or a membrane for depleting the hydrogen. The outlet of the hydrogen separation device 30 could be released into the environment. The fluid depleted of hydrogen in the hydrogen separation device 30 is preferably fed to the pyrolysis reactor 2.Particularly preferably, the hydrogen-depleted fluid is recycled as a second gas feed 22 and preferably fed to the reaction vessel 3, advantageously by feeding the feed gas Z via the feed 19 and a first gas feed 21 together with the second gas feed 22 to the compressor 32. Advantageously, an inlet valve 20 is also provided between the first gas feed 21 and the feed 19. The hydrogen-depleted fluid could, starting from the hydrogen separation device 30, also be fed to a separate compressor (not shown), and the hydrogen-depleted fluid compressed in this way could advantageously be fed directly to the collecting chamber 5a via the second feed gas feed line 8.

[0034] Figure 3 shows the separation device 37 and in particular the lock 32 in detail. The lock 32 comprises a first closable opening 32a, an intermediate space 32c and a second closable opening 32b, wherein these openings 32a, 32b can be controlled to open and close by a first and second pivotable cover 32d, 32e, respectively, so that the carbon 11 located in the lower region of the degassing container 25 can be fed to the storage container 33, and the pressure present inside the degassing container 25 can nevertheless be maintained. The intermediate space 32c is preferably provided with a pressure relief device and has, for example, a discharge line 34 and a valve 35 arranged downstream.It may also prove advantageous to provide an inert gas supply 38 and a valve 39, particularly to supply the carbon 11 to the lock 32 with the aid of the inert gas supplied via the inert gas supply 38. Suitable inert gases include nitrogen or carbon dioxide.

[0035] The method according to the invention for the direct thermal decomposition of a hydrogen-containing compound into solid carbon II and hydrogen H2 is carried out in such a way that a hydrocarbon-containing feed gas Z is compressed, the compressed feed gas Z is subsequently passed through a liquid high-temperature heat carrier 6 and the feed gas Z is converted into a substance mixture S in the high-temperature heat carrier 6, the substance mixture S is collected above the high-temperature heat carrier 6 in a collecting space 5a, wherein the substance mixture S comprises at least the solid carbon II and a gas mixture containing hydrogen H2, the substance mixture S is fed to a separation device 37 arranged downstream of the collecting space 5a and the substance mixture S is depleted of solid carbon II in the separation device 37, wherein the depleted substance mixture S and the solid Carbon 11 is removed separately from the separation device 37.

[0036] Preferably, hydrogen H2 is subsequently depleted from the discharged, depleted substance mixture S, wherein the hydrogen H2-depleted substance mixture S is preferably fed to the pyrolysis reactor 2, and in particular to the liquid high-temperature heat carrier 6 located therein.

[0037] Preferably, the hydrogen H2-depleted mixture S is compressed before it is subsequently fed to the liquid high-temperature heat carrier 6.

[0038] Preferably, a conveying gas F is fed to the material mixture S accumulating in the collecting chamber 5a in such a way that at least a portion of the solid carbon 11 located in the collecting chamber 5a is fed to the separation device 37 by the acting conveying gas F. Preferably, the pressure, the conveying quantity and / or the point of action of the conveying gas F flowing into the collecting chamber 5a is changed or modulated over time, and the solid carbon 11 located in the collecting chamber 5a is thereby swirled up in order to support the feed of the carbon into the discharge device 12.

Claims

Patent claims 1. Device (1) for producing hydrogen (H2) and solid carbon (11) by thermal decomposition of a feed gas (Z) containing hydrocarbons, comprising: - a pyrolysis reactor (2) with a reaction chamber (3a) and a collection chamber (5a) arranged above the reaction chamber (3a), wherein the reaction chamber (3a) contains a liquid, preferably stationary, high-temperature heat transfer fluid (6); - a reactor feed line ( 7 ) leading into the reaction chamber (3a ); - an inlet (19) for the supply gas (Z) , wherein the inlet (19) fluid is conductively connected to the reactor inlet (7); - a heating device (4) to supply heat to the reaction chamber (3a); - a drainage device arranged in the collection chamber (5a) (12) for draining a mixture of substances (S) from the collection chamber (5a) ; - a separation device (37) arranged outside the pyrolysis reactor (2), wherein the discharge device (12) is connected to the separation device (37) via a discharge (14), and wherein the separation device (37) is configured to separate the substance mixture (S) into at least the components solid carbon (11) and hydrogen (H2) or a gas mixture containing hydrogen (H2); and a compressor (23) for compressing the fluid supplied to the reactor feed line (7). Device according to claim 1, characterized in that the high-temperature heat transfer medium (6) is a molten metal or a molten salt. Device according to claim 1 or 2, characterized in that the discharge device (12) comprises a plurality of collecting tubes (12a) with inlet openings (12b) arranged in the collecting chamber (5a). Device according to claim 3, characterized in that the collecting tubes (12a) are lance-shaped, with inlet openings (12b) oriented towards the reaction chamber (3a). Device according to any one of the preceding claims, characterized in that a gas supply line (8) opens into the collecting chamber (5a). Device according to claim 5, characterized in that a gas distribution device (9) is arranged between the reaction chamber (3a) and the inlet openings (12b) of the discharge device (12), which is supplied by the gas supply line (8).Device according to claim 5 or 6, characterized in that the reactor inlet line (7) and the gas supply line (8) are arranged downstream of the compressor (23) in the direction of flow of the supplied fluid. Device according to any of the preceding claims, characterized in that the separation device (37) comprises a degassing vessel (25) designed as a pressure vessel, and that the degassing vessel (25) is pre-. The device comprises a degassing vessel interior (25a) with a lower interior sub-compartment (25b) and an upper interior sub-compartment (25c), wherein the lower interior sub-compartment (25b) opens into a sluice (32) for the discharge of the solid carbon (11). The device according to claim 8 is characterized in that a particle filter (27) is arranged in the degassing vessel interior (25a), which divides the degassing vessel interior (25a) into the lower interior sub-compartment (25b) and the upper interior sub-compartment (25c), that the discharge (14) opens into the lower interior sub-compartment (25b), and that a gas outlet (29a) arranged in the upper interior sub-compartment (25c) feeds a gas discharge (29). The device according to claim 9 is characterized in that the gas discharge (29) opens into a hydrogen separation device (30), which at least partially depletes the supplied fluid of hydrogen.Device according to claim 10, characterized in that the hydrogen-depleted fluid is fed to the pyrolysis reactor (2). Device according to claim 11, characterized in that the hydrogen-depleted fluid is fed from the hydrogen separation device (30) to the compressor (23). Method for the direct thermal decomposition of a hydrogen-containing compound into solid carbon (11) and hydrogen (H2), by: - a supply gas (Z) containing hydrocarbons is compressed; - the compressed supply gas (Z) is subsequently passed through a liquid, preferably stationary, high-temperature heat transfer medium (6), in particular through a molten metal or a molten salt, and the supply gas (Z) is converted into a mixture of substances (S) in the high-temperature heat transfer medium (6); - the mixture (S) is collected above the high-temperature heat transfer medium (6) in a collection chamber (5a), wherein the mixture (S) comprises at least the solid carbon (11) and a gas mixture containing hydrogen (H2); - the mixture (S) is fed to a separation device (37) downstream of the collection chamber (5a) and the mixture (S) is depleted of solid carbon (11) in the separation device (37); and - the depleted mixture (S) and the solid carbon (11) are separately discharged from the separation device (37). A method according to claim 13, characterized in that hydrogen (H2) is subsequently extracted from the discharged, depleted mixture (S), and that the hydrogen (H2)-depleted mixture (S) is fed to the liquid high-temperature heat transfer fluid (6). A method according to claim 14, characterized in that the hydrogen (H2)-depleted mixture (S) is compressed and subsequently fed to the liquid high-temperature heat transfer fluid (6). A method according to one of claims 13 to 15, characterized in that a conveying gas (F) is supplied to the mixture of substances (S) accumulating in the collecting chamber (5a) in such a way that at least a part of the solid carbon (11) located in the collecting chamber (5a) is dissolved by the acting gas. The process gas (F) is supplied to the separation device (37). The method according to claim 16, characterized in that the pressure, the flow rate and / or the point of action of the process gas (F) flowing into the collection chamber (5a) is changed over time, and the solid carbon (11) located in the collection chamber (5a) is thereby stirred up.

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