SK500302013A3 - Pyrolysis process of the solid loose organic waste and the reactor for thermal decomposition - Google Patents

Abstract

Described is a reactor (1) for the pyrolysis of waste, in particular from sewage sludge and sludge from a biogas plant, in the interior of which a reaction space (320) is formed around which a heated hollow shell (32) is arranged which is connected to the inlet (30) a heat transfer medium to the reactor (1) and with its outlet (34), which is simultaneously separated from the interior of the reactor (1). Further described is a process for the pyrolysis of solid bulk waste which is fed into the reaction space (320). The movement of the subsequently fed waste in this reaction space is slowed down by the countercurrent of the steam-gas products generated by the pyrolysis, thereby achieving its high efficiency.

Description

Process for pyrolysis, thermal decomposition, solid bulk organic waste and a reactor for carrying it out

Technical field

The invention relates to a process for the pyrolysis of solid loose organic waste (POO), in particular sewage sludge and sludge from biogas stations, and the like.

The invention also relates to a reactor for carrying out the process.

BACKGROUND OF THE INVENTION

Sewage sludge is a product of technological processes of waste water treatment in municipal sewage plants. These are heterogeneous suspensions of organic and inorganic substances, which include, inter alia, a number of microorganisms (bacteria, fungi, molds, yeasts, etc.), some higher organisms (protozoa, gyroplanes, nematodes, etc.) as well as various trace elements, including residues of certain chemicals (drugs, hormones, pesticides, surfactants, etc.).

The sludges from biogas stations are then the product of controlled aerobic or anaerobic bacterial decomposition of organic waste and energy crops. It is a solid, predominantly organic material that has a higher pH (usually 7 to 8) and, in addition to residues of various chemicals, also contains relatively high amounts of nitrogen, phytopathogenic plant seeds, and some microorganisms such as e.g. potato cancer agent (Synchytrium endobioticium), etc.

Due to their composition, these materials represent hazardous organic waste, which is a serious risk not only to the environment but also to human and animal health. In the Czech Republic alone, more than 200,000 tons of sewage sludge are produced annually, and the costs of their storage and handling account for more than half of the total costs of waste water treatment. At present, however, there is no universal method for the efficient and at the same time ecological utilization or disposal of these materials - most of them are used as organic fertilizer in spite of the above, a smaller part is burned or gasified.

For the gasification of these materials as well as other types of biomass, the RU 2393200 proposed a pyrolysis reactor, which is based on the principle of countercurrent, and at > >

3 to which a stream of heat-carrying gaseous medium heated by the combustion of process fuel at the bottom of the reactor is supplied to the gasified material. The disadvantage of this solution is that due to the design of the reactor, the steam-gas pyrolysis products are mixed with the heat-transfer gas medium, so that the steam-gas pyrolysis products are diluted and contaminated, and consequently their energy properties and / or energy are reduced. possibilities of their further use (eg combustion).

It is therefore an object of the present invention to provide a process for the pyrolysis of solid particulate organic waste (POO), in particular sewage sludge from municipal sewage treatment plants and sludge from biogas stations and the like, and a reactor for carrying out this process. this or a similar purpose, while being economically advantageous and energy self-sufficient.

SUMMARY OF THE INVENTION

The object of the invention is achieved by a method of pyrolysis of solid loose organic waste, in particular treatment sludge and sludge from a biogas station in a reactor, in which solid loose organic waste is fed into the reaction space of the reactor around which a heated hollow jacket of the reaction space is formed. separated from the interior of the reactor. The passage of solid bulk organic waste is then pyrolyzed, and the movement of the subsequently introduced bulk organic waste is slowed in this reaction space by the countercurrent of steam-gas products formed by pyrolysis of the previous solid bulk organic waste. This achieves high pyrolysis efficiency without mixing or diluting the steam-gas pyrolysis products with the heat transfer medium, and these are thus suitable for further use without further technological steps.

Further, an increase in pyrolysis efficiency is achieved if solid particulate organic waste is fed to an inclined and / or rounded heating surface before being introduced into the reaction space on which it forms a moving layer and on which it is preheated and at the same time partially pyrolyzed.

Further efficiency gains are then achieved when solid particulate organic waste, after leaving the reaction space, is fed to an inclined and / or rounded heating surface on which it forms a moving layer and upon which its final pyrolysis occurs. It is advantageous here that the steam-gas products of this final pyrolysis enter

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into the reactor reaction space to further slow down the movement of solid bulk organic waste therein.

The object of the invention is also achieved by a reactor for the pyrolysis of solid loose organic waste, in particular sewage sludge and sludge from a biogas plant, in which an internal reaction space is formed, around which a heated hollow shell of the reaction space is arranged and connected to the inlet of the heat transfer medium into the reactor and with the exit of the heat transfer medium from the reactor and which is closed to the interior of the reactor so as not to mix the steam-gas pyrolysis products with the heat transfer medium.

In order to increase the efficiency of pyrolysis, a lower chamber is arranged downstream of the reaction space in the direction of movement of the solid bulk organic waste downstream of the reaction space and comprises at least one heated sloped and / or rounded surface facing at least partially the solid bulk organic waste outlet. directly connected to the inlet of the heat transfer medium to the reactor and to the outlet of the heat transfer medium from the reactor, or is connected to the inlet of the heat transfer medium to the reactor and / or the outlet of the heat transfer medium from the reactor via a hollow jacket of the reaction space. At the same time, this chamber is closed to the interior of the reactor to avoid mixing of the steam-gas pyrolysis products with the heat transfer medium.

The heated inclined and / or rounded surface of the lower chamber is preferably formed by a cone-shaped, truncated cone or truncated cone surface with an inclined upper base.

To further increase pyrolysis efficiency, an upstream chamber is provided upstream of the reaction space in the direction of solid particulate organic waste displacement in front of the reaction space, and includes at least one heated slanted and / or rounded surface facing at least partially to feed solid particulate organic waste into the reactor interior; which is directly connected to the exit of the heat transfer medium from the reactor and the inlet of the heat transfer medium to the reactor, or is connected to the inlet of the heat transfer medium to the reactor and / or to the exit of the heat transfer medium from the reactor. At the same time, this chamber is closed to the interior of the reactor to avoid mixing of the steam-gas pyrolysis products with the heat transfer medium.

The heated inclined and / or rounded surface of the upper chamber is preferably formed by a cone-shaped, truncated cone or truncated cone surface with an inclined upper base.

In another variant of the reactor according to the invention, the upper chamber, which comprises at least one heated inclined and / or rounded surface facing at least partially the solid particulate organic waste inlet into the reactor interior space, is located at least partially in the reactor reaction space. Its heated inclined and / or rounded surface preferably has the shape of a cone shell, truncated cone or truncated cone with an inclined upper base.

In this case, the upper chamber does not have to be connected to the inlet and thus also to the outlet of the heat transfer medium into the reactor, and is heated indirectly by transferring heat from the hollow jacket of the reaction space. However, to improve its heating efficiency, it may be connected to the heat transfer medium exit from the reactor and the heat transfer medium entry either directly or at least one of them via the hollow shell of the reaction space and / or the lower chamber. In such a case, it is necessary that the upper chamber is closed to the interior of the reactor in order to avoid mixing of the steam-gas pyrolysis products with the heat transfer medium.

In this arrangement, it is further preferred that at least a portion of the height of the upper chamber is provided a solid particulate organic waste rectifier, the outlet end of which houses a pyrolysis steam stream gas breaker that prevents pyrolysis steam gas products entering the solid particulate organic waste rectifier and retarding it. movement in it.

In the case where a space is created between the outer wall of the hollow jacket of the reaction space and the inner wall of the reactor jacket for design or technological reasons, it is preferable that this space is at least partially blinded and / or filled with a suitable heat insulating material.

BRIEF DESCRIPTION OF THE DRAWINGS

In the accompanying drawing, FIG. 1a shows a schematic cross-section through a first exemplary variant of a reactor for carrying out pyrolysis of solid bulk organic waste according to the invention, FIG. 1b to 1d show a cross-sectional view of individual elements housed in the interior of the reactor in the variant of FIG. 1a, FIG. 2a is a cross-sectional view of a second exemplary variant of a solid bulk pyrolysis reactor. i »·· S»> »i»> 'S 9 1 * J 9'>?

9 »? 9, the organic waste according to the invention, and in FIG. 2b to 2d show a cross-sectional view of the individual elements housed in the interior of the reactor in the variant of FIG. 2a.

DETAILED DESCRIPTION OF THE INVENTION

The process of pyrolysis of solid particulate organic waste (POO), in particular sewage sludge and biogas sludge, will be explained in two exemplary reactor variants for carrying out the process shown in FIG. 1a and 2a. Moreover, it can also be carried out in structurally different reactors, subject to certain conditions which will be described below.

The reactor 1 for the pyrolysis of particulate POO, in particular the sewage sludge and biogas plant sludge according to the invention, shown in FIG. 1a and 2a comprises a cylindrical steel casing 2 in which a heat transfer medium line 3 is arranged, which is separated from the interior of the reactor 1. The casing 2 of the reactor 1 is bevelled in its lower part towards the outlet 4 of the solid pyrolysis products. its walls here form a conical hopper 40, and in its upper part it is rounded towards the outlet 5 of the steam-gas pyrolysis products, which is preferably located at its highest point. In the upper part of the reactor 1, an inlet 6 of loose POO is introduced into its interior through its jacket 2, which in the variants shown is formed by a feed line 60 terminated in the variant shown in FIG. 1a at the level of the longitudinal axis 20 of the reactor jacket 1 by the vertical section 61, and in the variant shown in FIG. 2a in the vicinity of this axis 20 via an overflow 62. In both variants, the inlet 6 in the interior of the reactor 1 is led obliquely upwards at an angle of 45 °, preventing unwanted penetration of steam-gas pyrolysis products through this inlet 6 outside the reactor LV of other variants not shown the guide angle 6 of the particulate POO inlet 6 is essentially any other, in particular a larger angle, which inlet 6 can also be formed and / or terminated, respectively. opening in the interior of the reactor in another known manner and / or elsewhere - for example, it can also pass through the rounded upper part of the reactor jacket 1. The feed line 6 is provided with a suitable conveyor (not shown), e.g. screw conveyor.

The line 3 of the heat transfer medium (gas, flue gas, etc.) separated from the interior of the reactor 1 comprises, in the variant of the reactor 1 shown in FIG. 1 and a lower chamber 31 (see FIG. 1b), which is connected to the inlet 30 of the heat transfer medium which is? ♦ 1:>

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9 in the lower part of the reactor i, the hollow shell 32 of the reaction space 320 (see FIG. 1c), which communicates with the lower chamber 31, and the upper chamber 33 (FIG. 1d), which is connected to the hollow shell 32 of the reaction space 320 and is connected to the heat transfer medium outlet 34, which is arranged in the upper part of the reactor 1. In the variant shown in FIG. 2a, then the heat transfer medium line 3 separated from the interior of the reactor comprises only a lower chamber 31 (see FIG. 2b) which adjoins the heat transfer medium inlet 30 and a hollow jacket 32 of the reaction space 320 (see FIG. 2c) which communicates with the lower chamber 31 and with a heat transfer medium outlet 34. The upper chamber 33 (see FIG. 2d) is at least partially embedded in the reaction space 320 without being connected to its hollow shell 32, so that it does not need to be separated from the interior of the reactor because the heat transfer medium is not introduced therein. However, in this embodiment (not shown), the upper chamber 33 can also be connected to the hollow shell 32 of the reaction space 320 and / or the lower chamber 31 and / or separately to the heat transfer medium source and thus form part or separate of the heat transfer medium 3.

The lower chamber 31 is in both variants of the embodiment formed by a hollow cylindrical chamber, which is arranged coaxially with its jacket 2 in the interior of the reactor 1, its upper part 310 is shaped upwards into a cone jacket 311 with a 90 ° apex angle however, variations not shown may have a different angle and / or the cone 311 may be formed without a peak, e.g. as trimmed or trimmed with an inclined upper base, and the like. In the interior of the lower chamber 31, a partition 312, which deflects the supplied heat transfer medium to its inclined surface - in the present embodiment into its conical part - is then preferably arranged opposite the outlet of the heat transfer medium inlet 30. The lower chamber 31 is connected by a conduit 3132 to the hollow jacket 32 of the reaction space 320 arranged above it, and this conduit 3132 may in particular extend from its conical part (the variant shown in Fig. 1a) or from its cylindrical part (the variant shown in Fig. 2a). ), or elsewhere.

In other embodiments not shown, the lower chamber 31 may be formed in any arbitrary manner, the only requirement being that it comprises at least one heated oblique and / or rounded surface facing at least partially the exit of the bulk POO from the reaction space 320. The hollow shell 32 of the reaction space 320 it is formed by a hollow cylindrical body arranged coaxially with its jacket 2 in the interior of the reactor 1, around the cylindrical reaction space 320. In the inner space of the hollow jacket 32 of the reaction space 320, a conduit 321 of suitable shape and size is provided. in the preferred embodiment shown in FIG. 1c and 2c e.g. the shape of an ascending helix, but in other variations not shown, may have any other shape which provides for the best possible heat exchange between the heat transfer medium introduced into the interior space of the hollow shell 32 of the reaction space 320 and the reaction space 320. the variation shown in FIG. 1a, respectively. 1c beveled towards its center, respectively. to the inlet of reaction space 320 of reactor 1 with a top angle of 105 °. However, in other variations (not shown), the apex angle may be of any other suitable size that provides for the displacement of the particulate POO falling on the wall 322 into the reaction space 320, or may be at least partially rounded. The hollow casing 32 of the reaction space 320 is then connected via a conduit 3233 to an upper chamber 33 above it, and this conduit 3233 may extend, for example, from its upper tapered wall 322 (a variant shown in FIG. 1a), its inner wall or elsewhere. .

In further variations of the embodiment (not shown), the hollow shell 32 of the reaction space 320 can be shaped in any other way, the only requirement being that it comprises a cavity (reaction space 320). wherein the peripheral wall is heated by a heat transfer medium guided in the hollow shell 32 over as much of its surface as possible.

The space 3220 between the outer wall of the hollow casing 32 of the reaction space 320 and the inner wall of the casing 2 of the reactor 1 (if provided for design or technological reasons) is preferably blinded at least on its underside, i. filled, closed and / or at least partially filled with suitable material so that all steam-gas pyrolysis products formed in the space below it are directed only or preferably to the reaction space 320. In particular, a suitable filler is a material with good insulating properties and at the same time refractory, e.g. ceramic wadding.

The upper chamber 33 is in the variant shown in FIG. 1 and is formed by a hollow cylindrical chamber (see FIG. 1d), which is coaxial to the interior of the reactor 1 with its jacket 2, its upper part 330 being shaped upwardly into a cone jacket 331 with an apex angle of 60 °, and its lower part 332 is formed downwardly in the shape of a truncated cone shell 333 with the same apex angle. In the next »and t ·, ->

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However, with 3 variations not shown, the apex angle of at least one of their portions may be of a different size and / or the upper cone 331 may be formed without a apex, e.g. Alternatively, the lower cone 333 may be formed with a vertex, a truncated cone with an inclined base, and so on. In the inner space of the upper chamber 33, a cross-member 334 is preferably arranged opposite to the outlet of the conduit 3233, which deflects the supplied heat transfer medium to its inclined surface and / or rounded surface facing the inlet 6 of the bulk particulate POO. The upper chamber 33 is connected via a conduit 3334 to a heat transfer medium outlet 34 from the interior of the reactor 1. This conduit 3334 may extend, in particular, from its lower conical portion (the variant shown in FIG. 1a), the upper conical portion, or elsewhere.

In the variation shown in FIG. 2a, a free flow cone rectifier 35 is provided around the lower portion 332 of the upper chamber 33, which is shaped like a cone shell 333, over its entire height or at least a portion thereof, formed by a frusto-conical casing guide. Preferably, its apex angle is the same as the cone apex angle 333 of the lower portion 332 of the upper chamber 33, but in other variations there may be substantially any other, particularly larger, to ensure a smooth passage of the particulate POO. To the top of the lower part 332 of the upper chamber 33 is then connected a steam breaker 36 of the steam-gas pyrolysis products, which in the embodiment shown is a solid disk-shaped body whose upper wall 360 is shaped upwards into a cone 3601 with an apex angle of 90 °. substantially any other, and whose bottom wall 361 is rounded downwardly. However, in other embodiments not shown, the steam gasifier pyrolysis stream 36 may be formed by at least one otherwise shaped and / or else near the outlet end of the baffle 35 supported by a fixed or movable body. In a variant of the embodiment (not shown), the striker 36 may be formed by vanes mounted on the surface of the upper chamber 33 and / or the hollow shell 32 of the reaction space 320 and / or in the space therebetween. Another difference from the variant shown in FIG. 1a, the shape of the upper wall 322 of the hollow casing 32 of the reaction space 320, which in this variant is straight, and the location of the upper chamber 33, which is at least partially or completely arranged in the upper part of the hollow casing 32 of the reaction space 320 the purpose and also that the hollow jacket 32 of the reaction space 320 is connected to the heat transfer medium exit 34 from the reactor 1. In the variant not shown, the upper wall 322 of the hollow jacket may then be " y "

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9 of the reaction space 320 formed as tapered and / or rounded toward the entrance to the reaction space 320. In another variant (not shown), the inner wall of its hollow skirt 32 may be tapered at the top of the reaction space 320 and / or rounded towards its center and better, respectively. thus more closely follow the shape of the upper chamber 33.

Generally, the upper chamber 33 can be shaped in any other way, the only requirement being that it comprises at least one heated inclined and / or rounded surface facing at least partially to the inlet 6 of the particulate POO.

On the basis of the foregoing, it will be apparent to the person skilled in the art that the individual elements of the reactor 1, in particular the heating medium ducts 3 or part thereof, can be formed and arranged in any other way in a substantially arbitrary manner. For example, one of these elements may be located in the interior of the reactor 1 non-aligned with its jacket 2 and / or other elements of the heat transfer medium 3 separated from the interior of the reactor 1, or may have any cross-section other than circular - e.g. triangular, quadrilateral or polygonal (regular or irregular). In any other embodiment, however, the upper chamber 33 and the lower chamber 31 must have at least one heated oblique and / or rounded surface facing the inlet 6 of the bulk POO so that the bulk POO can move by gravity thereon while forming into a thin layer. These inclined and / or rounded surfaces can additionally be provided with suitable guide elements (not shown), such as e.g. grooves and / or guide rails and / or other protrusions that govern the movement of the particulate POO layer and / or may be formed with at least two different oblique and / or rounded surfaces of different length and / or oblique and / or curvature - when are formed by a conical surface, any of which may comprise at least two sections with different apex angles, including zero angle, and the like. In addition, the inclined surface may be formed by two inclined walls which form a cutting edge between them, or between which a planar or arbitrary spatial surface is arranged. At least one means for deflecting the supplied heat transfer medium can be provided in each part of the heat transfer medium line 3 separated from the interior of the reactor 1, e.g. to one of its walls, in particular to a wall with an inclined and / or rounded surface. Such a means may be e.g. planar baffle 312, 321. 334. a spatially shaped baffle, screen, rib, blade (s) or other suitable means, provided with aperture (s) if necessary.

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In other variants of the embodiment (not shown), the individual parts of the heat transfer line 3 are connected outside the reactor 1, or each of them, or any combination of at least two of them, is connected to the heat transfer medium source separately so that they form a separate heat transfer line 3 separated from the interior. Reactor L

The heat transfer medium conduit 3 or at least a part thereof is preferably formed of a material with a high heat transfer coefficient, such as e.g. cast iron, stainless steel, etc.

In the operation of the reactor 1 according to the invention, resp. In carrying out pyrolysis of the bulk POO according to the invention, a heat transfer medium (gas, flue gas, etc.) is supplied to the heat transfer medium line 3 separated from the interior of the reactor 1, which heats the walls of the lower chamber 31, the hollow shell 32 of the reaction space 320 and the upper chamber. 33 (indirectly in the case of the variant in FIG. 2a). At the same time, the feed 6 of the bulk POO is supplied to the interior of the reactor 1 by the POO, in particular sewage sludge and / or sludge from a biogas plant, and the like. transformed during previous drying and crushing / grinding into bulk material. This loose POO then falls on the inclined surface of the upper chamber 33 - in the embodiment shown, to the top and / or near the upper cone 331 by gravity, and moves downwards along this surface, forming into a relatively thin layer, the thickness of which gradually decreases as the slope increases in size. As a result, the heat transfer from the heating medium through the upper wall 33 of the upper chamber to the loose SPC is efficiently transferred and is well overheated throughout the volume, which exceeds the thermal stability limit of the organic compounds contained therein. solid residue - ie to pyrolysis. Upon dropping of the particulate POO over the edge of the inclined surface of the upper chamber 33, the POO impinges upon the upper wall 322 of the hollow shell 32 of the reaction space 320 and is directed into the reaction space 320 , or falls directly into the reaction space 320. Due to the construction of the hollow sheath 32, it is subjected to the greatest heating and thus its most intense pyrolysis takes place. The remaining bulk POO then falls through the reaction space 320 onto the inclined surface of the lower chamber 31 - in the embodiment shown, to the top or near the top cone 311. On this surface, due to its skewness, it again moves downwards, forming itself into a relatively thin layer, whereby it is formed into a relatively thin layer, whose thickness gradually decreases with further displacement and increasing size of the inclined surface. This results in its final pyrolysis and the release of organic compounds whose pyrolysis has not yet been completed or has not been completely completed. The steam-gas pyrolysis products pass through the whole jacket 2 of the reactor 1 towards the steam-gas pyrolysis product outlet 5 and in the reaction space 320 of the reactor 1 come into contact with falling particulate POO particles which slow down their fall and thereby prolong their presence in the reaction space 320. increase the efficiency of their pyrolysis.

In the operation of the reactor 1 in the variant shown in FIG. 2a, the bulk POO after being overflowed from the upper wall 330 of the upper chamber 33 is directed to the reaction space 320 via a bulk particulate POO line 35. Its solid residues then fall from the reaction chamber 320 to the upper wall 310 of the lower chamber 31. The steam generator gas pyrolysis stream 36 prevents the steam gas pyrolysis products from penetrating into the bulk feed gas line 35, since they would slow it down, thereby bypassing the upper chamber 33. through a widened portion of the reaction space 320 and directed to the outlet 5 of the steam-gas pyrolysis products through which they are discharged from the reactor 1.

Upon exiting the reactor 1, these steam-gas pyrolysis products are fed to a cooling system (not shown) where they are condensed, respectively. to separate their constituents, which are liquid and gaseous under the set conditions. Both types of these components are flammable due to their composition, so that they can be used as fuel, e.g. for the production of electrical and / or thermal energy. Some of them and / or their residual heat can also be used to preheat and / or pre-dry the bulk SPC before it enters and / or after reactor 1, or to generate the electricity required to operate reactor 1 and its operating elements. As a result, the operation of the reactor 1 according to the invention is energetically self-sufficient.

Solid pyrolysis products consisting predominantly of ash, slag, or non-flammable impurities in POO, such as sand, stones, etc. then they fall into the lower part of the reactor 7 and, due to its shaping, are directed to the outlet 4 of solid particles. From there they are continuously or continuously exported to landfill or for further processing or use.

An advantage of the bulk pyrolysis reactor 1 according to the invention is that the steam-gas pyrolysis products do not come into contact with the heat transfer medium, so that they do not mix or dilute, so that they can be burned immediately. Another significant advantage is that pyrolysis is completely free of pyrolysis.

The microorganisms or higher organisms contained in the POO, such as e.g. in sewage sludge, biogas sludge or other similar materials, so that the solid pyrolysis residue does not pose any environmental risk in this respect.

When the reactor 1 according to the invention is used, the pyrolysis is carried out at a temperature in the range of about 450 to 650 ° C, but the construction of the reactor 1 does not prevent it from running at a higher temperature if this is necessary for some reason.

A reactor design other than the variants shown in FIG. 1a and 2a, wherein the required minimum is a reactor 1 which comprises a heat transfer medium line 3 separated from the interior of the reactor 1, formed by at least a heated hollow jacket 32 of the reaction space 320. However, it is preferred they decompose into a thin layer on a heated inclined surface, since the steam-gas pyrolysis products released from this layer form a countercurrent in the reaction space 320 and slow down the movement of the bulk POO thereby contributing to its more efficient pyrolysis. However, according to the experiments carried out, the arrangement with the upper chamber 33 upstream of the reaction space 320 in the reactor 1 upstream of the reaction space 320 seems to be the most effective arrangement. space is then faster and more thorough.

Claims (14)

PATENT CLAIMS Method for pyrolysis, thermal decomposition, solid bulk organic waste, in particular sewage sludge and biogas sludge in a reactor (1), characterized in that solid bulk organic waste is fed into the reaction space (320) of the reactor (1), around having a heated hollow jacket (32) of the reaction space (320), which forms the heat transfer medium (3) separated from the interior of the reactor (1), and pyrolysis of the solid bulk organic waste passes through the reaction space (320), wherein the movement of the subsequently introduced solid particulate organic waste in this reaction space (320) is slowed by the countercurrent of the steam-gas products formed by pyrolysis of the previous solid particulate organic waste. Pyrolysis method according to claim 1, characterized in that the solid bulk organic waste is fed to the inclined and / or rounded heated surface of the upper chamber (33) or the hollow jacket (32) before being introduced into the reaction space (320) of the reactor (1). a reaction space (320) on which it forms a moving layer and preheats and partially pyrolyses it. Pyrolysis method according to claim 1 or 2, characterized in that the solid bulk organic waste, after leaving the reaction space (320), is fed to the inclined and / or rounded heated surface of the lower chamber (31) on which it forms a moving layer. and in which its final pyrolysis takes place. The pyrolysis process according to claim 3, characterized in that the steam-gas products of the final pyrolysis of solid bulk organic waste enter the reaction space (320) of the reactor (1). Reactor (1) for pyrolysis of solid bulk organic waste, in particular sewage sludge and sludge from a biogas plant, characterized in that a reaction chamber (320) is formed in its interior space around which a heated hollow jacket (32) of the reaction reactor is arranged. a space (320) communicating with the inlet (30) of the heat transfer medium into the reactor (1) and with the outlet (34) of the heat transfer medium from the reactor (1) and which is separated from the interior of the reactor (1). 5 β> · a => v *> δ> S ·> »1 9>> 5> Λ S S 'i t * ♦) ϊ - ». · · 7 Λ Reactor (1) according to claim 5, characterized in that a downstream chamber (31) is arranged downstream of the reaction chamber (31) in the direction of movement of the solid bulk organic waste in the interior of the reactor (1) and comprises at least one heated oblique and / or a rounded surface facing at least partially the solid particulate organic waste outlet from the reaction space (320) and communicating with the heat transfer medium inlet (30) to the reactor (1) and the heat transfer medium outlet (34) from the reactor (1) and / or is connected to the inlet (30) of the heat transfer medium to the reactor (1) and / or to the outlet (34) of the heat transfer medium from the reactor (1) via a hollow jacket (32) of the reaction space (320). Reactor (1). Reactor (1) according to claim 6, characterized in that the heated inclined and / or rounded surface of the lower chamber (31) is formed by a cone-shaped, cone-shaped or cone-shaped surface with an inclined upper base. Reactor (1) according to any one of claims 5 to 7, characterized in that an upstream chamber (33) is arranged upstream of the reaction chamber (33) in the direction of movement of the solid bulk organic waste in the interior of the reactor (1). one heated inclined and / or rounded surface facing at least partially to the solid particulate organic waste inlet (6) to the interior of the reactor (1) and communicating with the heat transfer medium outlet (34) of the reactor (1) and inlet (30) the heat transfer medium to the reactor (1) and / or is connected to the heat transfer medium inlet (30) and / or the heat transfer medium outlet (34) from the reactor (1) via a hollow jacket (32) of the reaction space (320) ) and / or a lower chamber (31), which is simultaneously separated from the interior of the reactor (1). Reactor (1) according to claim 8, characterized in that the heated inclined and / or rounded surface of the upper chamber (33) is formed by a cone-shaped, cone-shaped or cone-shaped surface with an inclined upper base. Reactor (1) according to any one of claims 5 to 7, characterized in that the reaction chamber (320) of the reactor (1) houses at least partially an upper chamber (33) comprising at least one heated oblique and / or rounded i. * »F •) •» i »Ί · ϊ S S »» an area facing at least partially the inlet (6) of solid bulk organic waste into the interior of the reactor (1). Reactor (1) according to claim 10, characterized in that the heated inclined and / or rounded surface of the upper chamber (33) is formed by a cone-shaped, cone-shaped or cone-shaped surface with an inclined upper base. Reactor (1) according to claim 10 or 11, characterized in that the upper chamber (33) is connected to the heat transfer medium outlet (34) from the reactor (1) and to the heat transfer medium inlet (30) to the reactor (1), and / or communicating with the inlet (30) of the heat transfer medium into the reactor (1) and / or with the outlet (34) of the heat transfer medium from the reactor (1) through the hollow jacket (32) of the reaction space (320) and / or the lower chamber (31). ), and at the same time it is separated from the interior of the reactor (1). Reactor (1) according to any one of claims 10 to 12, characterized in that at least a part of the height of the upper chamber (33) is arranged a solids organic waste rectifier (35), the outlet end of which houses a current breaker (36). steam-gas pyrolysis products, which prevent the steam-gas pyrolysis products from entering the solids organic waste rectifier (35). Reactor (1) according to any one of the preceding claims, characterized in that the space (3220) between the outer wall of the hollow jacket (32) of the reaction space (320) and the inner wall of the jacket (2) of the reactor (1) is at least partially closed; or filled with heat insulating material.