DE102012223567A1 - Method for removing e.g. biomass formed from tar compounds during pyrolysis in fluidized bed reactor, involves performing gasification of pyrolysis residual substance with process gas for forming product gas - Google Patents

Abstract

The method involves performing pyrolysis of organic compound containing substance. The tar compounds are provided with pyrolysis gas and pyrolysis residual substance. The thermal decomposition of the tar compounds is performed. The decomposing products containing process gas is generated from the thermal decomposition of the tar compounds. The gasification of pyrolysis residual substance with the process gas is performed for forming product gas. The oxygen-containing gas is supplied. An independent claim is included for a reactor.

Description

The invention relates to a process for the removal of tar compounds formed as part of the pyrolysis of organic compounds from a pyrolysis gas.

The formation of tar compounds, d. H. Substantially high molecular weight or aromatic hydrocarbon compounds, in the context of the pyrolysis of organic compounds containing or formed from such substances (short organic substances), which are commonly referred to as biomass, is known.

Known processes for the pyrolysis of organic substances are carried out, for example, in fluidized-bed reactors in which pyrolysis of the organic substances takes place at temperatures between 500 and 1000 ° C., with tar compounds also being formed in addition to the product gases as described.

The tar compounds thus contained in the product gases produced during the pyrolysis regularly lead to problems, in particular due to clogging or contamination of lines, valves, filters and pressure losses of the product gas.

To remove tar formed in the pyrolysis of organic compounds from a pyrolysis gas separation steps, especially on gas scrubbing, or catalytic processes, in particular via catalytic reforming of the product gas, are common to date, which, however, are both complex in terms of equipment and process technology.

It is also problematic in this case that the energy content or calorific value of the originally high-energy or highly calorific product gas and thus the efficiency of the overall process are regularly reduced.

The invention is based on the problem of specifying an improved process for removing tar compounds formed from pyrolysis gas during the pyrolysis of organic compounds.

The problem is solved according to the invention by a method of the type mentioned, which by the steps: a) pyrolysis of organic compounds containing substances, wherein the tar compounds pyrolysis and pyrolysis are formed b) thermal decomposition of the tarry compounds contained in the pyrolysis, wherein producing a process gas containing decomposition products formed from the thermal decomposition of the tar compounds, c) gasifying the pyrolysis solids with the process gas to form a product gas.

In the following, substances containing organic compounds are abbreviated to organic substances. These are substances or mixtures of substances which are at least partially formed from organic compounds or include such. Examples of corresponding organic substances are comminuted wood parts, so-called wood chips or wood chips, wood dust, such. As sawdust, organic liquids such. As oils or sludges, or fossil fuels such. As coal or oil.

The inventive method is based on a three-step process, wherein in a first step, a pyrolysis of the organic substances, in particular with supply of at least one oxygen-containing gas and / or steam takes place, wherein the tar compound pyrolysis gas and pyrolysis are formed.

Pyrolysis compounds are all substances that arise during the pyrolysis of organic substances. These are usually carbon, d. H. in particular coke, and / or organic carbon compounds.

The proposed in an advantageous embodiment of the invention supply of an oxygen-containing gas, including z. As pure oxygen or an oxygen-enriched gas, in particular oxygen-enriched air is to be understood, causes a reduction in the formation of nitrogen compounds in the pyrolysis gas and further in the product gas obtained at the end of the process. Consequently, at the end of the process there is a high-energy or high-calorie product gas, which can be used, for example, to produce energy, for example in a gas turbine or a gas engine, or for chemical synthesis.

The pyrolysis residues, which are present essentially in the form of particles or dusts, z. B. separated into a separate reactor space, so that the pyrolysis gas is free or at least substantially free of solids.

As described, in addition to the advantageous supply of at least one oxygen-containing gas, steam may also be supplied in step a). The supply of water vapor allows a limitation or need-based adjustment of the temperature of the pyrolysis gas. About certain parameters, such. B. Amount, temperature and pressure, of the supplied water vapor can therefore be realized according to need adjustment of the temperature of the pyrolysis gas, which in particular also takes into account different compositions of the organic substances to be pyrolyzed. The supply of water vapor causes an increase in the proportion or concentration of water vapor or hydrogen in the pyrolysis gas.

The pyrolysis is preferably carried out in a temperature range of 500-950 ° C., in particular 600-900 ° C. In this temperature range, the pyrolysis can be done highly efficient. Other temperature ranges are basically possible. The specific temperature or the specific temperature range in which the pyrolysis is carried out depends in particular on the composition of the organic substances to be pyrolyzed. An upper limit of the temperature can be defined by the so-called ash softening point of the organic substances, which is typically in the range of 700-130 ° C. for corresponding organic substances.

The remaining during the pyrolysis given process parameters such. As pressure, feed rate of organic substances, flow rate of the pyrolysis gas, etc., are in particular determined depending on the specific composition of the organic substances to be pyrolyzed.

Appropriately, the pyrolysis gas flows through at least one separation device for separating any solids contained in the pyrolysis gas, such as. B. contained in the pyrolysis pyrolysis. As a separation device, for example, an electrostatic separation device connected to an electrical voltage source can be used which enables an electrostatic separation of solids contained in the pyrolysis gas.

In the second step of the process according to the invention, a thermal decomposition of the tar compounds contained in the pyrolysis gas, in particular under repeated or optionally first supply of at least one oxygen-containing gas. In this case, a process gas formed from the thermal decomposition of the tar compounds, in particular low molecular weight, organic, containing decomposition products is generated. In the second step, therefore, a thermal decomposition ("thermal cracking") of the tar compounds into corresponding organic decomposition products is essentially carried out. In other words, the substantially high molecular weight tar compounds are thermally transformed into low molecular weight decomposition products such. B. low molecular weight gaseous hydrocarbons, decomposed or degraded. For this purpose, a higher temperature than in pyrolysis is basically required, which z. B. is realized by the supply of oxygen-containing gases and / or water vapor. The process gas generated in the second step therefore has due to the comparatively high, required in the second step, d. H. high thermal energy compared to the first step of higher temperatures.

The limitation of the temperature by the ash softening point of the organic substances described in connection with the first step of the method according to the invention is no longer present in the second step. Accordingly, the thermal decomposition of the tarry compounds contained in the pyrolysis gas is advantageously carried out in a temperature range of 900-1300 ° C, especially 950-1200 ° C.

The temperature increase required after the first step can, as mentioned, be realized in particular by the supply of at least one gas containing oxygen and / or water vapor.

In the third step of the process according to the invention takes place, in particular thermally induced, gasification of the organic pyrolysis, d. H. in particular, the coke formed after the pyrolysis of the organic substances, with the process gas to form a product gas. A typical product gas contains z. 25-50% hydrogen, 10-40% carbon monoxide, 10-35% carbon dioxide, the composition being such that the total content of the compounds does not exceed 100%.

The high thermal energy of the process gas as well as the amount of water vapor supplied in the first step and / or second step is used here to produce a gasification, ie. H. in particular steam gasification, to carry out the pyrolysis, whereby the product gas is formed. The product gas is, as essentially also the process gas used for its gasification, free or at least largely free of tar compounds.

The steam gasification of the pyrolysis residues is an endothermic process which allows the thermal energy contained in the hot process gas to be converted into chemical energy contained in the product gas. Consequently, the temperature of the product gas formed by gasification of the pyrolysis with the process gas is comparatively low. The process according to the invention therefore permits a high cold gas efficiency which results from the ratio of those pyrolyzed in the beginning organic energy bound substances and the energy bound in the product gas, reach.

It is also conceivable that the endothermic gasification of the pyrolysis solids carried out in the third step of the process according to the invention is carried out thermodynamically, i. H. in particular by setting a certain temperature, a targeted formation of hydrocarbon-containing or formed from hydrocarbons value gases such. As methane allowed. Contains the product gas hydrocarbons, such. As methane, it is z. B. particularly suitable for subsequent use as fuel gas in a gas turbine.

As mentioned, the product gas is high energy or high caloric and can be used for different purposes, such. B. are used for energy production such as in a gas turbine or a gas engine or for chemical synthesis.

Overall, the method according to the invention thus opens up a possibility, starting from the pyrolysis of organic substances, of producing a product gas which is free or at least substantially free of tar compounds or other comparable high molecular weight hydrocarbons. This is possible due to the thermal decomposition provided in the second step of the process according to the invention in which the tar compounds formed in the pyrolysis of the organic substances and contained in the pyrolysis gas are possible.

The invention further relates to a reactor for removing tar compounds formed from pyrolysis gas during the pyrolysis of organic compounds. The reactor is designed in particular for carrying out the method described above.

The reactor has three reactor spaces communicating with each other. Here, a first reactor space for pyrolysis of organic compounds containing materials, in particular with supply of at least one oxygen-containing gas and / or water vapor, wherein a tar compound pyrolysis gas and organic pyrolysis are formed formed. A second, subsequent to the first reactor chamber or downstream reactor space is for thermal decomposition of the tarry compounds contained in the pyrolysis gas, in particular with supply of at least one oxygen-containing gas and / or water vapor, wherein a generated from the thermal decomposition of the tar compounds decomposition products containing process gas is generated , educated. A third, the second reactor chamber following or downstream reactor space is formed for gasification of the pyrolysis with the process gas to form a product gas.

Structurally, the reactor spaces may be separate components or component groups or at least partially integral. It is crucial that the function of each reactor space is guaranteed, d. H. So z. B. the first reactor space is constructed so that in this pyrolysis of organic compounds containing materials, in particular with supply of at least one oxygen-containing gas and / or steam, is feasible, so that a tar compound containing pyrolysis gas and pyrolysis can be formed. This applies analogously to the second and third reactor space.

The three reactor chambers communicate with each other in such a way that a gas flow can be formed between them. In particular, it is thus ensured that the pyrolysis gas formed during operation of the reactor within the first reactor space can flow into the second reactor space and the process gas formed there into the third reactor space. In particular, a connection to the third reactor space can be provided between parts of the first and / or second reactor space via which, for example, organic substances or pyrolysis solids contained in the pyrolysis gas or the process gas are introduced into the third reactor space in the organic substances fed into the first reactor space can be.

In principle, all statements relating to the process according to the invention apply analogously to the reactor according to the invention, in particular with regard to the processes or process steps taking place therein.

Constructively, the reactor z. B. a cylindrical shape and is formed for example as a hollow cylinder. It is essential for the design of the reactor that this limits an interior space in which the three aforementioned, mutually communicating reactor spaces can be arranged or arranged.

Advantageously, the first reactor space has a tubular, elongated shape and passes through the reactor axially, ie, along or in the region of its longitudinal central axis. The tubular formation of the first reactor space in the sense of a so-called "riser" also allows variations of the geometric shape of the organic substances to be supplied in these, so that both particulate fuels (eg wood parts) or dust-like fuels (eg sawdust ) as well as liquid fuels (eg oils, sludges) can be supplied. The axial extent of the first reactor space advantageously extends to over half the height of the Reactor, so that the first reactor space advantageously extends to more than half in the reactor.

Constructively, the reactor may be designed such that the third reactor space extends between the first and the second reactor space, wherein the second reactor space extends at least partially along the lateral surface of the reactor. The advantage of this reactor design lies in the fact that the second reactor space is easily accessible due to the lateral arrangement in the region of the inner surface or side wall of the reactor, so that any necessary service or especially cleaning work, which due to z. B. adhering to the walls of the second reactor space, not decomposed tar compounds pollution may be required.

Alternatively, the reactor z. B. be designed such that the second reactor space extends between the first and the third reactor space, wherein the third reactor space extends at least partially along the lateral surface of the reactor. In this case, the second reactor space advantageously completely surrounds the tubular first reactor space and is thus arranged in particular likewise in or in the region of the longitudinal central axis of the reactor. In this way, a heat exchange between the second and the first reactor space is possible, so that the thermal energy produced as part of the thermal decomposition of the tar compounds during operation of the reactor in the second reactor space can be used in part to control the temperature of the first reactor space.

Preferably, the third reactor space is designed as a fluidized bed reactor. Fluidized bed reactors serve to receive a bed of, in particular particulate, solids, wherein the bed of solids an upward flow of a gas is performed. In the context of the method according to the invention, the bed formed essentially from the pyrolysis solids and a bed material is reacted or gasified with the process gas flowing through it to form the product gas, so that the formation of the third reactor space as a fluidized bed reactor is expedient.

The first reactor space is advantageously connectable or connectable to a supply device, wherein the substances containing organic compounds and / or an oxygen-containing gas and / or water vapor can be supplied via the supply device into the first reactor space. The supply device is present in particular as part of a so-called "riser", via which organic substances and optionally further substances, in particular pressurized, supplied into the first reactor space, d. H. especially blown, can be.

In order to enable a supply of oxygen-containing gases and / or water vapor which is expedient or necessary for the course of the process according to the invention, the reactor has at least one, in particular at least two, feed devices for the supply of oxygen-containing gases and / or water vapor. Corresponding supply means are provided in particular for the first and second reactor space, since in these take place those steps in the context of removing the tar compounds from the pyrolysis gas, which require the supply of oxygen-containing gases and / or water vapor.

In a further development of the invention, at least one, in particular electrostatic, separating device for separating solids contained in the process gas is arranged at least between the first and the second reactor space. For example, an electrostatic separation device connected to an electrical voltage source can be provided as a separation device, which allows an electrostatic separation of solids contained in the pyrolysis gas.

Finally, the reactor has at least one outlet communicating with the third reactor space for the product gas. The product gas led out of the reactor via the outlet can be used for various purposes, in particular in connection with the method according to the invention.

Further advantages, features and details of the invention will become apparent from the embodiment described below and from the drawing. Showing:

1 a block diagram illustrating the method according to the invention;

2 a schematic representation of a reactor according to a first exemplary embodiment of the invention; and

3 a schematic representation of a reactor according to a second exemplary embodiment of the invention.

1 shows a block diagram illustrating the method according to the invention. The method according to the invention describes a three-stage process. In a first, in box a) step shown organic compounds containing substances, organic substances or biomass, at temperatures in the range of 500-900 ° C pyrolyzed, wherein a tar compounds containing pyrolysis gas and pyrolysis, such as coke, are formed.

It is by the arrow 1 indicated that the pyrolysis under supply of pure oxygen, which over conventional methods for oxygen generation, such. B. pressure swing adsorption, membrane process or cryogenic air separation, is provided, or oxygen-containing gases, such as. B. oxygen-enriched air, can be performed.

Similarly, the pyrolysis can be done under, optionally additional, supply of water vapor.

The resulting by the pyrolysis of the organic substances pyrolysis, which are present substantially as coke are separated, the tar compounds contained in the pyrolysis gas are thermally decomposed in a second step, shown in box b), d. H. the essentially high molecular weight tar compounds are decomposed or split under the influence of temperature into low molecular weight decomposition products. The temperatures required for carrying out the second step are in the range of 900-1300 ° C, especially 950-1200 ° C.

By the arrow 2 is shown that also in the context of the thermal decomposition of the tarry compounds contained in the pyrolysis gas, a supply of pure oxygen or oxygen-containing gases, such as. B. oxygen-enriched air, and / or steam can be done. This is particularly useful to achieve or adjust the necessary for the thermal decomposition of the tar compounds high temperatures.

The process gas produced in the second step (cf box b)), resulting from the thermal decomposition of the tar compounds, in particular low molecular weight organic, decomposition products containing high thermal energy due to the high temperatures required for the thermal decomposition of the tar compounds and is in the third gasification step represented by box c), d. H. in particular steam gasification, the previously separated pyrolysis used. Here, a product gas which is wholly or at least substantially free of tar compounds is generated. The product gas is high-energy or high-caloric and can be used, for example, for energy production, for example in a gas turbine or a gas engine, or for chemical synthesis.

A typical product gas contains z. 25-50% hydrogen, 10-40% carbon monoxide, 10-35% carbon dioxide, the composition being such that the total content of the compounds does not exceed 100%.

2 shows a schematic diagram of a reactor 3 according to a first exemplary embodiment of the invention. The reactor 3 is related to the implementation of 1 formed method described.

The reactor 3 has a cylindrical body 4 in which three communicating reactor rooms 5 . 6 . 7 are provided. The first, in particular tubular or designed as a so-called "riser", reactor space 5 can via a feeder 8th with the organic substances to be pyrolyzed, which may be, for example, comminuted wood parts ("wood chips"), wood dusts, etc., and optionally other materials, such as sands or sludges, are charged. The substances to be pyrolyzed are pressurized at a certain flow rate into the first reactor space 5 guided. In addition, via the supply device 8th Oxygen, oxygen-enriched air and water vapor in the first reactor space 5 be supplied. In addition, from the third reaction space 7 Parts of the bed material of the fluidized bed be entrained.

In the first reactor room 5 The organic substances are pyrolyzed, ie converted into a pyrolysis gas under the influence of thermal energy supplied via suitable heating devices or through the bed material of the fluidized bed. As part of the pyrolysis of organic substances also arise tar compounds, which are contained in the pyrolysis gas substantially, as well as pyrolysis.

Obviously, the construction of the reactor 3 after exiting the first reactor space 5 an expansion of the reactor space, which leads to the fact that the flow velocity of the pyrolysis gas is reduced, resulting in a separation of optionally contained in the pyrolysis pyrolysis, such as coke, which due to gravity in a funnel-shaped or hollow cylindrical siphon 9 fall and from there into the third reactor room 7 reach.

The third reactor room 7 is formed as a fluidized bed reactor, so that, as described above, separated from the pyrolysis pyrolysis in the third reactor space 7 present in a fluidized bed. In this case, it is possible to at least partially remove the pyrolysis residues, ie in the region of the lower, the third reactor space 7 facing the end of the siphon 9 to flow through with a fluid. Not shown, but where appropriate, it may be a separate Feeding device for the supply of coke or similar, the pyrolysis substances corresponding substances in the third reactor space 7 provided.

That from the first reactor room 5 exiting pyrolysis gas can after passing through an electrostatic connected to an external power source separation device 10 , via which any pyrolysis residues still present in the pyrolysis gas are separated, laterally into the second reactor space 6 enter (see arrow 11 ).

About another feeder 12 , which is formed from or may comprise porous, ceramic material, additional pure oxygen, oxygen-containing gases or steam can be supplied if necessary. The addition of pure oxygen, oxygen-containing gases and water vapor leads to a temperature increase in the second reactor space 6 , The temperatures prevailing in the second reactor space are in the range of 950-1100 ° C., in particular around 1000 ° C., and cause thermal decomposition of the tar compounds contained in the pyrolysis gas, which decompose or decompose into decomposition products, in particular in the form of low molecular weight hydrocarbon compounds become.

In the second reactor space, a process gas which contains the decomposition products resulting from the decomposition of the tar compounds is formed by thermal decomposition of the tar compounds contained in the pyrolysis gas. The in the second reactor space 6 formed process gas is therefore free or at least largely free of tar compounds.

In the lower part of the second reactor space 6 is another feeder 13 provided over which the process gas, if necessary, water vapor can be added in order to achieve an optionally required adjustment of the temperature of the process gas, ie, in particular cooling of the process gas to a desired temperature.

That from the second reactor room 6 escaping hot process gas enters the third reactor space 7 in which it is gasified with the present in a fluidized bed pyrolysis, ie converted to a product gas. The thermal energy of the second reactor space 6 exiting process gas is thus used to gasify the pyrolysis. The gasification of the pyrolysis is an endothermic process, so that finally from the third reactor space 7 via an outlet 14 emerging product gas has a comparatively low temperature.

The outlet 14 may be provided with a control valve (not shown) via which certain pressure conditions within the third reactor space 7 and therefore within the reactor 3 can be ensured.

Basically, a backflow of process gases from about the third reactor space 7 in the second reactor room 6 and further into the first reactor room 5 thereby avoiding that the organic substances to be pyrolyzed via the supply device 8th under high pressure in the first reactor space 5 be supplied. Overall, the reactor offers 3 the possibility of a simple and safe pressure control, even in the range of high pressures, ie in particular pressures above 30 bar.

By not shown here additional feeder. via which a supply of pure oxygen, oxygen-containing gases and / or water vapor in the third reactor space 7 is possible, the thermodynamics of the gasification of the pyrolysis and thus the energy balance of the method according to the invention can be influenced.

It is possible that by compared to one in the third reactor space 7 bedding material of the fluidized bed lower density of the pyrolysis, which, as mentioned, are substantially present as coke, the pyrolysis can act as a barrier for tar compounds, ie the release of optionally in the third reactor space 7 arrived tar compounds, which z. B. in the second reactor space 6 not or not completely decomposed. The pyrolysis residues in the third reactor space 7 can thus act as a kind of filter for tar compounds and, if appropriate, contribute catalytically to the reaction of tar compounds still present. By a sufficiently long residence time of the tar compounds in the third reactor space 7 In addition, there is the possibility of this possibly in the third reactor space 7 thermally decompose into corresponding decomposition products.

It is expedient that in the third reactor space 7 existing fluidized bed another separator (not shown), in particular in the form of a cyclone downstream, to separate any solids emerging from the fluidized bed. The separated solids can g in the feeder 8th (Back) are guided so that a loss of bedding material and pyrolysis residues can be avoided.

The construction of the in 2 shown reactor 3 is seen such that the tubular first reactor space 5 the reactor 3 partially penetrated axially in the region of its longitudinal central axis. The second reactor room 6 is in the area of the side wall of the reactor 3 or of the basic body 4 arranged, ie the second reactor space 6 extends along the lateral surface of the reactor 3 or of the basic body 4 , The third reactor room 7 extends between the first reactor space 5 and the second reactor space 6 ,

By the in 2 construction shown is the second reactor space 6 easily accessible, so that any necessary service or cleaning work, which due to on the walls of the second reactor space 6 adherent, non-degraded tar compounds formed pollutants may be required, are easy to carry out.

3 shows a schematic diagram of a reactor 3 according to a second exemplary embodiment of the invention. The main difference to the in 2 shown exemplary embodiment of a reactor 3 consists in the arrangement of the second reactor space 6 , which is not here along the lateral surface or side wall of the reactor 3 or of the basic body 4 but the first reactor space 5 is arranged immediately surrounding.

Thus, the second reactor space extends 6 also centrally within, ie in the region of the longitudinal central axis of the reactor 3 or of the basic body 4 , Compared to the in 2 In the embodiment shown, the second reactor space extends 6 here between the third reactor room 7 and the first reactor space 5 , which may be advantageous insofar as such in the second reactor space 6 during the thermal decomposition of the tar compounds prevailing high temperatures of the body 4 of the reactor 3 can be kept away. The main body 4 can be designed for operation at high pressures, the temperature being well below the maximum process temperature in the second reactor space 6 is.

By the in 3 shown construction of the reactor 3 is a heat exchange between the second reactor space 6 and the first reactor space 5 possible for those in the first reactor room 5 performed pyrolysis required thermal energy in the sense of a jacket heating at least partially over the second reactor space 6 can be provided.

Both in the in 2 as well as in the 3 shown embodiment of the reactor 3 it is conceivable the outer walls of the main body 4 of the reactor 3 thermally isolate, in particular the temperature-related or dependent on this process conditions within the reactor 3 to control and prevent heat loss.

Although the invention has been further illustrated and described in detail by the preferred embodiment, the invention is not limited by the disclosed examples, and other variations can be derived therefrom by those skilled in the art without departing from the scope of the invention.

Claims (15)

 Process for the removal of tar compounds formed from pyrolysis gas in the course of the pyrolysis of organic compounds, characterized by the steps: a) pyrolysis of substances containing organic compounds, wherein the pyrolysis gas containing tar compounds and pyrolysis solids are formed, b) thermal decomposition of the tar compounds contained in the pyrolysis gas, whereby a process gas containing decomposition products formed from the thermal decomposition of the tar compounds is produced, c) gasification of the pyrolysis with the process gas to form a product gas. A method according to claim 1, characterized in that in step a) and / or b) at least one oxygen-containing gas is supplied and in step a) and / or b) steam is supplied. A method according to claim 2, characterized in that as oxygen-containing gas pure oxygen or an oxygen-enriched gas, in particular oxygen-enriched air, is used. Method according to one of the preceding claims, characterized in that the pyrolysis gas at least one, in particular electrostatic, separation device ( 10 ) flows through. Method according to one of the preceding claims, characterized in that in step a) carried out pyrolysis of organic compounds containing substances in a temperature range of 500-950 ° C, in particular 600-900 ° C, is performed. Method according to one of the preceding claims, characterized in that in step b) performed thermal decomposition of the tarry compounds contained in the pyrolysis gas in a temperature range of 900-1300 ° C, in particular 950-1200 ° C, is performed. Reactor ( 3 ) for the removal of pyrolysis of organic compounds Tar compounds formed from a pyrolysis gas, in particular according to the method according to one of claims 1 to 6, characterized in that it communicates with each other three reactor chambers ( 5 . 6 . 7 ), wherein - a first reactor space ( 5 ) for the pyrolysis of substances containing organic compounds, wherein the pyrolysis gas containing pyrolysis gas and pyrolysis residues are formed is formed, - a second, the first reactor space ( 5 ) following reactor space ( 6 ) for the thermal decomposition of the tar compounds contained in the pyrolysis gas, wherein a process gas containing decomposition products formed from the thermal decomposition of the tar compounds is produced, and - a third, the second reactor space ( 6 ) following reactor space ( 7 ) is formed for the gasification of the pyrolysis with the process gas to form a product gas. Reactor according to claim 7, characterized in that it has a cylindrical shape, wherein the first reactor space ( 5 ) is tubular and the reactor ( 3 ) at least partially penetrated axially. Reactor according to claim 8, characterized in that the third reactor space ( 7 ) between the first reactor space ( 5 ) and the second reactor space ( 6 ), wherein the second reactor space ( 6 ) at least partially along the lateral surface of the reactor ( 3 ). Reactor according to claim 8, characterized in that the second reactor space ( 6 ) between the first reactor space ( 5 ) and the third reactor space ( 7 ), wherein the third reactor space ( 7 ) at least partially along the lateral surface of the reactor ( 3 ). Reactor according to one of claims 7 to 10, characterized in that the third reactor space ( 7 ) is formed as a fluidized bed reactor. Reactor according to one of claims 7 to 11, characterized in that the first reactor space ( 5 ) with a supply device ( 8th ) is connectable or connected, wherein the organic compounds containing substances and / or an oxygen-containing gas and / or water vapor via the supply device ( 8th ) in the first reactor space ( 5 ) can be supplied. Reactor according to one of claims 7 to 12, characterized in that it comprises at least one feed device ( 8th . 12 . 13 ) for supplying oxygen-containing gas and / or water vapor. Reactor according to one of claims 7 to 13, characterized in that between the first reactor space ( 5 ) and the second reactor space ( 6 ) at least one, in particular electrostatic, separation device ( 10 ) is arranged for separating solids contained in the process gas. Reactor according to one of claims 7 to 14, characterized in that it has at least one with the third reactor space ( 7 ) communicating outlet ( 14 ) for the product gas.

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