Pyrolysis method and apparatus for producing pyrolysis gas and pyrolysis coke

Abstract

The present invention relates to a method and an apparatus for providing pyrolysis oil and pyrolysis gas.

Description

[Technical Field]

[0001] The present invention relates to a pyrolysis process and a pyrolysis apparatus. [Background technology]

[0002] A process for producing pyrolysis oil at process temperatures is known from DE 10 2015 108 552 A1. The process described comprises a pyrolysis step at 600-750 °C in the presence of a catalyst bed, in particular a catalyst bed consisting of newly formed pyrolysis solids, and a reforming step. In this process, the solids to be treated are introduced into the reactor tube from the top, the pyrolyzed solids are removed downwards from the reactor tube, and the pyrolysis gases are removed through the inner tube for further treatment.

[0003] DE 102014105340 A1 discloses a process for producing pyrolysis oil using a tubular reactor, the longitudinal axis of which is inclined at an angle of 45° or less to the horizontal, and the material to be pyrolyzed is conveyed through the reactor by a conveying screw.

[0004] German Patent Application No. 102016115700 also discloses a pyrolysis process with a reforming step at 600-750°C. An average particle size of the solid fossil fuel of 3-30 mm is stated to be particularly suitable. In German Patent Application No. 102016115700, the use of materials of biological origin is only envisaged in conjunction with fossil fuels. The transport of the material to be treated is achieved by means of conveyor belts or conveying screws, in particular single-screw extruders. [Prior art documents] [Patent documents]

[0005] [Patent Document 1] German Patent Application Publication No. 102015108552 [Patent Document 2] German Patent Application Publication No. 102014105340 [Patent Document 3] German Patent Application Publication No. 102016115700 Summary of the Invention [Problem to be solved by the invention]

[0006] Known processes result in relatively large, not very compact plants. The problem addressed was therefore to provide a process and plant that provides pyrolysis oil but with a very compact configuration and that avoids further drawbacks mentioned in the prior art, such as deposits and blockages, especially when filters are used to clean the pyrolysis gases. Another problem addressed was to provide a process that can withstand a relatively high proportion of fines (based on the feedstock). [Means for solving the problem]

[0007] The present invention provides a biomass in the form of small particles having a moisture content of less than 30% by weight, wherein the biomass in the form of small particles has a median particle size D 50 The present invention is based on the finding that providing biomass having a particle size of 2.0 mm to 60 mm (determined in accordance with ASTM E112) can be avoided by combining a pyrolysis device with a reactor space having a substantially vertical arrangement, which reactor space is substantially cylindrical or substantially conical and has a conveying device for transporting biomass in particle form from the bottom upward through said reactor space and for feeding biomass in particle form from the bottom upward through the reactor space so that a bed is present in the reactor space.

[0008] In this regard, the present invention provides A pyrolysis process for producing pyrolysis gas and pyrolysis coke (pyrolysis coal), comprising: a) providing biomass in the form of small particles having a moisture content of less than 30% by weight, wherein the biomass in the form of small particles has a median particle size D 50is preferably determined according to ASTM E112 and is between 2.0 mm and 60 mm; b) i) a reactor space of substantially vertical orientation, said reactor space being substantially cylindrical or substantially conical; ii) a conveying unit for transporting the biomass in particle form from the bottom upward through the reactor space; iii) a heating unit for said reactor space; iv) a supply of heating medium from above to the heating unit and a discharge for the heating medium so that the heating medium is conducted in countercurrent to the biomass; v) an outlet for the pyrolysis gases in the upper region of the reactor space; vi) optionally a dedusting unit for said pyrolysis gases; vii) a discharge unit for pyrolysis coke; viii) Optionally, a removal unit for separated dust particles. providing a pyrolysis apparatus comprising: c) feeding the biomass in the form of small particles from the bottom upward through the reactor space so that a bed is present in the reactor space; d) heating the biomass in the form of small pieces at a heating rate of 0.3 to 5 K / s; e) pyrolyzing the biomass in the form of small pieces at a temperature of 400 to 750°C, preferably 450 to 650°C, for 5 to 60 minutes in the substantial absence of oxygen; f) removing the pyrolysis gas from the reactor and optionally feeding the pyrolysis gas to the dedusting unit; g) optionally separating and removing dust particles; h) removing the resulting pyrolysis coke; i) extracting the pyrolysis gas; j) optionally providing pyrolysis oil by partial condensation of the withdrawn pyrolysis gas; The present invention provides a process (method) comprising:

[0009] The present invention further provides a pyrolysis apparatus comprising: i) a reactor space of substantially vertical orientation, the reactor space being substantially cylindrical and / or substantially conical; ii) a conveying unit suitable for transporting biomass in particle form from the bottom upwards through said reactor space to provide a bed of biomass; iii) a heating unit for the reactor space; iv) a supply and discharge of a heating medium from above into the heating unit, so that the heating medium is conducted in countercurrent to the biomass, as well as an outlet for the pyrolysis gases in the upper region of the reactor space; v) optionally a dedusting unit for the pyrolysis gases; vi) a discharge unit for pyrolysis coke; vii) optionally a removal unit for separated dust particles; A pyrolysis apparatus is provided, comprising:

[0010] Biomass with a moisture content of less than 30% by weight is known and is not limited to this. All types of biogenic waste are possible options. Drying is optional. Therefore, it is also possible to use biogenic waste such as sewage sludge.

[0011] The median particle size D of biomass in the form of small particles of 2.0 mm to 60 mm, preferably determined according to ASTM E112 50 can be ensured by known pre-treatment steps. 10 It is particularly preferred that the fraction is present in an amount of less than 30 weight percent (based on the total particles). In some circumstances, it may be necessary to adjust the average size and amount of the fine fraction, for example, by sieving. 10 The fraction is preferably 10 to 30% by weight.

[0012] A major advantage of the process is that it produces a relatively large amount of fines, e.g., 10% to 25% by weight of D based on the total particles. 10 It is also possible to use

[0013] The reactor space (1) is substantially vertically oriented. This means that it can deviate from exactly vertical (up-down) alignment by up to 40°. Preferably, the deviation from exactly vertical alignment is less than 20°. Furthermore, the reactor space is substantially cylindrical and / or substantially conical. By substantially cylindrical, it is meant that it can deviate from a circular cross-sectional area. In a substantially conical embodiment, the cross-sectional area of ​​the reactor space increases from the bottom upward. It is also possible, and preferred, for the reactor space to be substantially cylindrical in the middle and lower parts and substantially conical in the upper part. More preferably, in an embodiment having a "cylindrical middle and lower parts and a conical upper part," the middle and lower parts occupy 60% to 85% of the total height of the reactor space.

[0014] A further variable for affecting residence time is the speed of the transport unit. A conveying unit is used to transport the biomass in particle form from the bottom upward through the reactor space. This is usually a conveying screw. The conveying screw preferably occupies 80% to 95% of the cross-sectional area of ​​the reactor space (based on the internal dimensions). This ensures that a portion of the biomass in particle form can slide under gravity on the inner surface of the reactor shell. This ensures good mixing. The area occupied by the conveying screw is considered to be the total area of ​​the conveying screw, including the core and any additional units. The remaining ring space is therefore 5% to 20% of the cross-sectional area of ​​the reactor interior. In the case of a conical reactor geometry, the average cross-sectional area (arithmetic mean) is taken into account accordingly, i.e., the area considered is the cross-sectional area of ​​the reactor in the region of the conveying screw.

[0015] Typically, the conveying screw does not fill the reactor space vertically, but only to the extent of about 60% to 85% of the total internal height of the reactor space. However, embodiments are also possible in which the conveying screw protrudes through the entire reactor space. Typically, the height of the conveying unit is selected so that a bed of biomass in the form of particles forms above it. In other words, above the conveying screw, an accumulation in the form of a bed forms. It will be clear that the bed fills the entire remaining reactor space below, in particular the ring space discussed above.

[0016] To ensure a suitable temperature for pyrolysis and to provide an appropriate amount of heat, a heating unit is provided for the reactor space. It will be clear that the heating is carried out indirectly. Usually, the reactor walls are at least partially heated. The biomass in particle form is therefore heated by the introduction of heat from outside. There is therefore no direct contact between the biomass in particle form and the heating medium. Additionally and preferably, there may be a heating unit within the transport unit, which means that the transport unit may optionally be heated.

[0017] The heating medium is fed into the heating unit from the top via the feed (5) and is removed from the heating unit via the discharge (6), which means that the heating medium is conducted in countercurrent to the biomass. The heating medium may be gaseous. Alternatively, the heating medium may be a liquid metal or liquid metal alloy. In a preferred embodiment, the heating medium is a liquid salt melt.

[0018] The biomass in the form of small particles is heated at a heating rate of 0.3-5 K / s, i.e., relatively quickly. Pyrolysis is then carried out in the substantial absence of oxygen at temperatures of 400-750°C, preferably 450-650°C, for 5-60 minutes. The temperature range of 400-750°C means that the pyrolysis temperature is within this range. The bed will therefore have a temperature from this range in the upper region, preferably in the accumulation section above the conveying screw, in particular. Temperatures above 750°C should be avoided at all costs, otherwise the coking problem cannot be eliminated.

[0019] Optionally, and preferably, there is a dedusting unit (8) for the pyrolysis gases. It is preferable to use a cyclone. Additionally or alternatively, it is possible to use a hot gas filter.

[0020] It is particularly preferred that the dust removal unit (8) is located within the reactor space (1), most preferably at the top of the reactor space. This has the great advantage that the dust removal unit is heated together with the reactor space, which means that this integrated solution leads to simplification and greater compactness. A further advantage results from the fact that the separated dust can be removed directly together with the pyrolysis coke, which means that there is also no need for a separate removal in this respect, i.e., compactness is maximized. Alternatively, in another embodiment, the dedusting unit may be located outside the reactor space.

[0021] The pyrolysis coke obtained is advantageously removed by gravity. It is particularly preferred to combine the pyrolysis coke obtained with the separated dust particles. As explained above, this is possible in a particularly simple manner if the dust removal unit is arranged at the top of the reactor space.

[0022] Pyrolysis oil is obtained from the pyrolysis gases by optional partial condensation. The pyrolysis oil is preferably obtained as a two-phase mixture of pyrolysis oil and water by partial condensation of the extracted pyrolysis gases. This two-phase mixture can be separated, for example, by removing the phases by suction. The phase boundary can be determined by conventional measurement parameters such as electrical conductivity, refractive index, etc.

[0023] Advantageously, the pyrolysis coke is discharged under gravity, which allows for a particularly compact design since there is no need for additional conveying elements. Compactness is further assisted when separated dust particles are combined with the pyrolysis coke, which is preferred. If the dust removal unit is provided outside the reactor space, the discharge conduit for the dust may also be combined with the discharge conduit for the pyrolysis coke.

[0024] In the process according to the invention, feeding the biomass in small particle form from the bottom upwards through the reactor space is preferably carried out by means of a conveying screw, more preferably at 0.5 to 20 revolutions per minute.

[0025] In the process of the present invention, the pyrolysis gas is preferably pre-purified by a bed of biomass in particle form.

[0026] In the process according to the present invention, the screw pitch of the conveying screw preferably decreases from top to bottom. This means that the distance between the screw flights decreases in that direction. This creates a gradient based on the bed packing density. In the upper region, the bed density is lower than in the lower region. In this way, a pressure increase in the reaction zone is avoided.

[0027] The bed height within the reactor space is selected to achieve a residence time of the biomass within the reactor space of 5 to 60 minutes at a temperature of 400 to 750°C, preferably 450 to 650°C.

[0028] Preferably, continuous mixing of the biomass, especially its bed, within the reactor space should be ensured. More preferably, continuous mixing of the biomass in particle form is provided by a conveying unit, which means that the conveying unit functions simultaneously for conveying and mixing.

[0029] The conveying unit is preferably configured so that the bed of biomass is partially mixed from above downwards, more preferably so that the bed of biomass can partially move vertically downwards under gravity near the shell surface, in particular near the shell surface.

[0030] The process according to the invention is also suitable for the production of hydrogen from pyrolysis gases, the amount of which can be maximized by additionally introducing water.

[0031] In the pyrolysis units described herein, external heating is preferably provided by heating the outer concluding face of the reactor or even by heating the conveying unit. By external heating, it is meant that heat is fed in from other units and processes. Typically, waste heat from synthesis gas or other high-temperature processes is used. It is possible, and preferred, to recover heat from the heat flow remaining after heating the reactor and / or the conveying unit. The heat still present may be advantageously used to preheat the air in the combined process. The heat transfer for heating the reactor and / or the conveying unit may either be direct or an additional heat transfer medium such as a liquid salt melt or a liquid metal or liquid metal alloy may be used. The same applies to the recovery of heat. For reactor heating, the heating medium is preferably fed from the top to ensure counter-current conditions (heating medium to biomass).

[0032] Also disclosed herein is the use of the process and / or apparatus for the production of bio-coke, activated carbon and / or barbecue charcoal. [Brief explanation of the drawings]

[0033] [Figure 1] 1 shows a cross section of a pyrolysis device according to the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0034] A preferred embodiment will now be described with reference to FIG. FIG. 1 shows a cross section of a pyrolysis apparatus according to the present invention.

[0035] In the illustrated embodiment, the reactor space (1) is conical. It has an internal conveying screw (2), by means of which the biomass is transported from the bottom upwards and simultaneously mixed and loosened. The biomass is in the form of a loose bed (3). The reactor space (1) is heated by a heating unit (4), which may be designed as a simple jacket structure or in the form of piping on or optionally within the reactor wall. A heating medium, e.g., a gas, is fed in from above via a feed (5). The heating medium leaves the reactor wall again in the lower region of the reactor. The biomass is conveyed from the bottom upwards and the heating medium is conveyed from the top downwards, i.e., heating takes place in countercurrent.

[0036] The conveying screw (2) does not completely fill the reactor space, but only to the extent of 80% to 95% of its cross-sectional area. The biomass in particle form is in the form of a bed (3), which is constantly mixed. The feeding of the biomass in particle form is carried out via a unit (10). In addition, the bed (3) serves as a preliminary filter for the pyrolysis gases. The upper part of the reactor space is provided with a dust removal unit (8), to which the pyrolysis gases are fed and cleaned. The dust removal unit is preferably designed as a cyclone. The separated dust falls to the bed under gravity and can be removed together with the resulting pyrolysis coke. For this purpose, a discharge unit (9) for the pyrolysis coke is provided. This is preferably designed so that the pyrolysis coke is removed under gravity. It is particularly advantageous that the separated dust particles can also be removed via this discharge unit.

[0037] Experimental section A pilot plant was projected and tested and it was found that no blocking problems occurred and that excellent compactness was achieved.

[0038] Embodiment 1. A pyrolysis process for producing pyrolysis gas and pyrolysis coke, comprising: a) providing biomass in the form of small particles having a moisture content of less than 30% by weight, wherein the biomass in the form of small particles has a median particle size D 50 is preferably determined according to ASTM E112 and is between 2.0 mm and 60 mm; b) i) a reactor space (1) of substantially vertical orientation, which is substantially cylindrical and / or substantially conical; ii) a conveying unit (2) for transporting the biomass in particle form from the bottom upwards through the reactor space; iii) a heating unit (4) for said reactor space; iv) a supply (5) of a heating medium to the heating unit from above and a discharge (6) for the heating medium, so that the heating medium is conducted in countercurrent to the biomass; v) an outlet (7) for the pyrolysis gases in the upper region of the reactor space; vi) optionally a dedusting unit (8) for said pyrolysis gases; vii) A discharge unit (9) for pyrolysis coke or for pyrolysis coke and separated dust particles (9). providing a pyrolysis apparatus comprising: c) feeding the biomass in particle form from the bottom upwards through the reactor space (1) so that a bed (3) is present in the reactor space; d) heating the biomass in the form of small pieces at a heating rate of 0.3 to 5 K / s; e) pyrolyzing the biomass in the form of small pieces at a temperature of 400 to 750°C, preferably 450 to 650°C, for 5 to 60 minutes in the substantial absence of oxygen; f) removing the pyrolysis gas from the reactor and optionally feeding the pyrolysis gas to the dedusting unit; g) optionally separating and removing dust particles; h) removing the pyrolysis coke obtained, optionally together with the separated dust particles; i) extracting the pyrolysis gas; h) optionally providing pyrolysis oil by partial condensation of the withdrawn pyrolysis gas; The process includes:

[0039] 2. The process of embodiment 1, wherein pyrolysis oil is obtained as a two-phase mixture of pyrolysis oil and water by partial condensation of the withdrawn pyrolysis gas, and the two-phase mixture is separated.

[0040] 3. The process of claim 1 or claim 2, wherein the dust particles are separated by a cyclone and / or an HG filter.

[0041] 4. The process of any one of claims 1 to 3, wherein the pyrolysis coke is discharged under gravity.

[0042] 5. The process of any one of claims 1 to 4, wherein the separated dust particles are removed together with the pyrolysis coke.

[0043] 6. The process of any one of the preceding claims, wherein feeding the biomass in particle form from the bottom upward through the reactor space is carried out using a conveying screw, preferably at 0.5 to 20 revolutions per minute.

[0044] 7. The process of embodiment 6, wherein the screw pitch of the conveying screw decreases from top to bottom.

[0045] 8. The process of any one of the preceding embodiments, wherein the pyrolysis gas is pre-purified by a bed of the biomass in particle form.

[0046] 9. The process of any one of the preceding claims, wherein the bed of biomass in an upper region of the reactor volume has a bulk density lower than the bulk density in a lower region of the reactor volume.

[0047] 10. The process of any one of the preceding embodiments, wherein a bed height within the reactor volume is selected to achieve a residence time of the biomass within the reactor volume of 5 to 60 minutes at a temperature of 400 to 750°C, preferably 450 to 650°C.

[0048] 11. The process of any one of the preceding claims, wherein continuous mixing of the biomass in particle form is performed by the conveying unit for transporting the biomass in particle form from the bottom upward through the reactor space.

[0049] 12. The process of embodiment 11, wherein the conveying unit is configured to partially mix the bed of biomass from above downwards, preferably configured to allow the bed of biomass to move vertically downwards under gravity near the shell surface, most preferably near the shell surface.

[0050] 13. The process of any one of embodiments 1 to 12, wherein hydrogen is obtained from the pyrolysis gas.

[0051] 14. The process of embodiment 13, wherein water is additionally introduced.

[0052] 15. A pyrolysis apparatus comprising: i) a reactor space (1) of substantially vertical orientation, which is substantially cylindrical and / or substantially conical; ii) a conveying unit (2) suitable for transporting biomass in particle form from the bottom upwards through said reactor space to provide a bed (3); iii) a heating unit (4) for said reactor space; iv) a supply (5) of a heating medium to the heating unit from above and a discharge (6) for the heating medium so that the heating medium is conducted in countercurrent to the biomass; v) an outlet (7) for pyrolysis gases in the upper region of the reactor space; vi) optionally a dedusting unit (8) for the pyrolysis gases; vii) a discharge unit (9) for pyrolysis coke or, optionally, for pyrolysis coke and separated dust particles (9); A pyrolysis device comprising:

[0053] 16. The pyrolysis apparatus of embodiment 15, which is accompanied by external heating, preferably heating the outer closed surface of the reactor, or the outer closed surface of the reactor and the conveying unit.

[0054] 17. The pyrolysis apparatus of embodiment 15 or embodiment 16, wherein the heating medium is fed from the top.

[0055] 18. The pyrolysis apparatus of embodiment 15, embodiment 16, or embodiment 17, wherein the heating medium is gaseous, or the heating medium is a liquid metal or liquid metal alloy, or the heating medium is a liquid salt melt.

[0056] 19. Use of the process according to any one of embodiments 1 to 14 and / or the device according to any one of embodiments 15 to 18 for the production of biocoke, activated carbon and / or barbecue charcoal. [Explanation of symbols]

[0057] 1. Vertically arranged reactor space (cylindrical and / or conical) 2. A conveying unit (conveying screw) for transporting the biomass in the form of small pieces from the bottom upwards through the reactor space. 3. Biomass floor 4 Heating Unit 5 Heating medium supply section from the top to the heating unit 6. Discharge for heating medium 7 Outlet for pyrolysis gas 8. Dust removal unit for pyrolysis gases 9. Discharge unit for pyrolysis coke (and separated dust particles) 10 Introduction to Biomass 11 Recuperator (for preheating air from waste air)

Claims

1. 1. A pyrolysis process for producing pyrolysis gas and pyrolysis coke, comprising: a) providing biomass in particle form having a moisture content of less than 30% by weight, wherein the median particle size D of said biomass in particle form is ５０ is determined in accordance with ASTM E112 and is between 2.0 mm and 60 mm; b) i) a reactor space (1) of substantially vertical orientation, which reactor space is substantially cylindrical and / or substantially conical; ii) a conveying unit (2) for transporting the biomass in particle form from the bottom upwards through the reactor space; iii) a heating unit (4) for the reactor space; iv) a supply (5) of a heating medium to the heating unit from above and a discharge (6) for the heating medium, so that the heating medium is conducted in countercurrent to the biomass; v) an outlet (7) for pyrolysis gases in the upper region of the reactor space; vi) a discharge unit (9) for the pyrolysis coke or for the pyrolysis coke and separated dust particles; providing a pyrolysis apparatus comprising: c) feeding the biomass in particle form from the bottom upwards through the reactor space (1) so that a bed (3) is present in the reactor space; d) heating the biomass in particle form at a heating rate of 0.3 to 5 K / s; e) pyrolyzing the biomass in the form of small particles at a temperature of 400 to 750°C for 5 to 60 minutes in the substantial absence of oxygen; f) removing the pyrolysis gas from the reactor; h) removing the resulting pyrolysis coke; i) extracting the pyrolysis gas; A method comprising:

2. The pyrolysis device includes: vii) A dedusting unit for said pyrolysis gases (8). The method of claim 1 further comprising:

3. 3. The method of claim 1 or claim 2, wherein step h) of the method further comprises feeding the pyrolysis gas to a dust removal unit.

4. The method comprises: g) Separating and removing dust particles and step h) further comprises removing the resulting pyrolysis coke together with the separated dust particles.

5. The method comprises: j) providing pyrolysis oil by partial condensation of the withdrawn pyrolysis gas. The method of claim 1 or claim 2, further comprising:

6. 3. The method of claim 1 or claim 2, wherein step e) comprises pyrolyzing the biomass in particle form in the substantial absence of oxygen at a temperature of 450-650°C for 5-60 minutes.

7. 3. The method according to claim 1 or claim 2, wherein pyrolysis oil is obtained as a two-phase mixture of pyrolysis oil and water by partial condensation of the withdrawn pyrolysis gas, and the two-phase mixture is separated.

8. 3. The method according to claim 1 or claim 2, wherein the dust particles are separated by a cyclone and / or a hot gas filter.

9. 3. The method of claim 1 or claim 2, wherein the pyrolysis coke is discharged under gravity.

10. 3. The method according to claim 1 or claim 2, wherein the separated dust particles are removed together with the pyrolysis coke.

11. 3. The method according to claim 1 or claim 2, wherein feeding the biomass in particle form from the bottom upward through the reactor space is carried out using a conveying screw.

12. The method according to claim 11, wherein the screw pitch of the conveying screw decreases from top to bottom.

13. 3. The method according to claim 1 or claim 2, wherein the pyrolysis gas is pre-purified by a bed of the biomass in particle form.

14. 3. The method of claim 1 or claim 2, wherein the bed of biomass in an upper region of the reactor volume has a bulk density that is lower than the bulk density in a lower region of the reactor volume.

15. 3. The method of claim 1 or claim 2, wherein the bed height within the reactor space is selected to achieve a residence time of the biomass within the reactor space of 5 to 60 minutes at a temperature of 400 to 750°C.

16. 3. The method according to claim 1 or claim 2, wherein continuous mixing of the biomass in particle form is performed by the conveying unit for transporting the biomass in particle form from the bottom upward through the reactor space.

17. 17. The method of claim 16, wherein the conveying unit is configured to partially mix the bed of biomass from the top down.

18. 3. The method of claim 1 or claim 2, wherein hydrogen is obtained from the pyrolysis gas.

19. 20. The method of claim 18, wherein water is additionally introduced.

20. A pyrolysis apparatus comprising: i) a reactor space (1) of substantially vertical orientation, which is substantially cylindrical and / or substantially conical; ii) a conveying unit (2) suitable for transporting biomass in particle form from the bottom upwards through said reactor space to provide a bed (3); iii) a heating unit (4) for said reactor space; iv) a supply (5) of a heating medium from above to the heating unit and a discharge (6) for the heating medium so that the heating medium is conducted in countercurrent to the biomass; v) an outlet (7) for pyrolysis gases in the upper region of the reactor space; vi) a discharge unit (9) for pyrolysis coke; wherein the conveying unit (2) is a conveying screw that occupies 80% to 95% of the cross-sectional area of ​​the reactor space based on its internal dimensions.

21. The pyrolysis device includes: vii) A dedusting unit for said pyrolysis gases (8).

21. The pyrolysis apparatus of claim 20, further comprising:

22. 22. The pyrolysis apparatus of claim 20 or claim 21 with external heating.

23. 22. The pyrolysis apparatus according to claim 20 or 21, wherein the heating medium is fed from above.

24. 22. Pyrolysis apparatus according to claim 20 or claim 21, wherein the heating medium is gaseous, or the heating medium is a liquid metal or liquid metal alloy, or the heating medium is a liquid salt melt.

25. 3. Use of the method according to claim 1 or claim 2 for the production of biocoke, activated carbon and / or barbecue charcoal.

26. 22. Use of the device according to claim 20 or claim 21 for the production of biocoke, activated carbon and / or barbecue charcoal.

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