SK288535B6 - Method of pyrolysis (thermal decomposition) of solid bulk organic waste and reactor for performing the method - Google Patents

Abstract

The invention relates to a method of pyrolysis of solid bulk organic waste, especially sewage sludge and sludge from a biogas station, in which solid bulk organic waste is fed to the reaction space (320) of the reactor (1), around which a heated hollow casing (32) of the reaction space (320) is arranged, which forms a duct (3) of the heat transfer medium separated from the inner space of the reactor (1), and during the passage of the solid bulk organic waste through this reaction space (320) its pyrolysis takes place, whereby the movement of the subsequently delivered solid bulk organic waste in this reaction space (320) is decelerated by counter flow of steam and gas products formed by the pyrolysis of the preceding solid bulk organic waste. The invention also relates to a reactor (1) for pyrolysis of solid bulk organic waste, especially sewage sludge and sludge from a biogas station, in whose inner space a reaction space (320) is created, around which is arranged a heated hollow casing (32) of the reaction space (320), which is connected to the inlet (30) of the heat transfer medium to the reactor (1) and the outlet (34) of the heat transfer medium from the reactor (1), and which is separated from the inner space of the reactor (1).

Description

The invention relates to a process for the pyrolysis of solid particulate organic waste (POO), in particular sewage sludge, 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 contain, among other things, a number of microorganisms (bacteria, fungi, molds, yeasts, etc.), some higher organisms (protozoa, gyroplanes, nematodes, etc.) and also various trace elements, including chemical substances (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 efficient and at the same time ecological utilization or disposal of these materials - most of them are used as organic fertilizer, a smaller part is burned or gasified.

For the gasification of these materials as well as other types of biomass, a pyrolysis reactor based on the principle of countercurrent was proposed in patent RU 2393200, in which a stream of a heat transfer gas medium heated by combustion of process fuel at the bottom of the reactor is supplied. 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, sludge from biogas plants 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 when solid particulate organic waste is fed to an inclined and / or rounded heating surface before being fed into the reaction space, forming a moving layer and preheating it while partially pyrolizing it.

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 the reactor reaction space in order 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 against 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 loose organic waste in the reactor interior space, which comprises at least one heated slanted and / or rounded surface facing at least partially towards the solid loose organic waste outlet. it is 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 to the outlet of the heat transfer medium from the reactor. At the same time, this chamber is closed against 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 downstream of the reactor space in the downstream direction of the solid bulk organic waste, which comprises at least one heated slanted and / or rounded surface facing at least partially to supply solid bulk organic waste to the reactor interior; it is directly connected to the heat transfer medium outlet from the reactor and the heat transfer medium inlet to the reactor, or is connected to the heat transfer medium inlet and / or to the heat transfer medium outlet from the reactor via a hollow jacket of the reaction space and / or lower chamber. At the same time, this chamber is closed against 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.

The upper chamber thus disposed 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 heat transfer 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 this case, it is necessary that the upper chamber is closed against the interior of the reactor in order not to mix 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 with an outlet end disposed therein a pyrolysis steam stream gas breaker which prevents pyrolysis steam gas products entering the solid particulate organic waste rectifier and slowing its 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 preferred that this space is at least partially blinded and / or filled with suitable thermal insulation 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-1d show a cross-sectional view of the 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 the reactor for carrying out pyrolysis of solid bulk organic waste according to the invention, and 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. In addition, however, it can also be carried out in structurally different reactors, subject to certain conditions to be described.

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 the heat transfer medium line 3 is located, which is separated from the interior of the reactor 1. The casing 2 of the reactor 1 is chamfered in its lower part towards the outlet 4 of solid pyrolysis products. here the walls 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 housing 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 through the overflow 62. In both variants, the inlet 6 is led obliquely upwards at an angle of 45 [deg.] In the interior of the reactor 1. This prevents unwanted ingress of steam-gas pyrolysis products via this inlet 6 outside the reactor 1. In other embodiments not shown the guide angle 6 of the feed SPD 6 can be essentially any other, in particular a larger angle, the feed 6 can also be formed and / or terminated, respectively. opening in the interior of the reactor 1 in another known manner and / or elsewhere - for example, it can also pass through the rounded upper part of the reactor jacket 2. The inlet 6 of the bulk POO is equipped with a suitable conveyor (not shown), e.g. screw conveyor.

The heat transfer medium line (gas, flue gas, etc.) separated from the interior of the reactor 1 comprises, in the variant of the reactor 1 shown in FIG. 1a, a lower chamber 31 (see FIG. 1b), which is connected to the inlet 30 of the heat transfer medium arranged at the bottom of the reactor 11, a hollow shell 32 of the reaction space 320 (see FIG. 1c) which communicates with the lower chamber 31 and a chamber 33 (FIG. 1d) which communicates with the hollow shell 32 of the reaction space 320 and is followed by a heat transfer medium outlet 34 arranged at the top of the reactor L 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 shell 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 accommodated in the reaction chamber 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 into it. However, in this embodiment (not shown), the upper chamber 33 can also be connected to the hollow shell 32 of the reaction chamber 320 and / or the lower chamber 31 and / or separately to the heat transfer medium source to form part or separate heat transfer medium conduit 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 cross-section 312 is then preferably arranged opposite the outlet of the inlet 30 of the heat transfer medium, which deflects the supplied heat transfer medium to its inclined surface - in the present embodiment into its conical portion. 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 interior of the hollow jacket 32 of the reaction space 320 is a system of crossbars 321 of suitable shape and size. 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 that provides the most perfect heat exchange between the heat transfer medium introduced into the interior space of the hollow jacket 32 of the reaction space 320 and the reaction space 320. The upper wall 322 of the hollow jacket 32 the variation shown in FIG. la, respectively. lc beveled towards its center, respectively. to the entrance to the reaction space 320 of the 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 jacket 32 of the reaction space 320 is then connected via a conduit 3233 to an upper chamber arranged above it.

33, whereby this conduit 3233 may extend, for example, from its upper tapered wall 322 (a variant shown in FIG. 1a), from its inner wall, or elsewhere.

In other variants 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) whose peripheral wall is heated by as much heat transfer medium as possible. 32nd

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 X (if provided for design or technological reasons) is preferably blinded at least on its underside, i. j. 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. 1a is formed by a hollow cylindrical chamber (see FIG. 1d), which is coaxial to the interior of reactor X with its jacket 2, its upper part 330 being shaped upwardly in the shape of a cone 331 with an apex angle of 60 ° and its lower part 332 shaped downwardly into a frustoconical shell 333 with the same apex angle. However, in other variations not shown, the apex angle and at least one portion thereof 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 interior 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 line 3334 to the heat transfer medium outlet 34 from the interior of the reactor. This conduit 3334 may in particular extend 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. Its apex angle is preferably the same as the cone apex angle 333 of the lower portion 332 of the upper chamber 33, but in other variations it may be substantially any other, especially larger, to ensure a smooth passage of the particulate POO. To the top of the lower portion 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 a 90 ° apex angle. 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 fully 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 of the reactor space X. In the variant not shown, the upper wall 322 of the hollow jacket 32 of the reaction space 320 can then be beveled and / or rounded towards the inlet. In another variation (not shown) of the reaction chamber 320, the inner wall of its hollow shell 32 may be tapered 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.

Accordingly, it will be apparent to those skilled in the art that the individual elements of the reactor X, 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, some of these elements may be located in the interior of reactor X non-aligned with its shell 2 and / or other elements of the heat transfer medium 3 separated from the interior of reactor X, 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. In addition, these inclined and / or rounded surfaces can be provided with suitable guide elements (not shown), e.g. grooves and / or guides, and / or other protrusions that regulate 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 rounding - in the case of when formed by a conical surface, any of them 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 X, 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 partition 312, 321, 334, spatially shaped partition, aperture, rib, blade (s) or other suitable means, provided with aperture (s) if necessary.

In further variants of the embodiment (not shown), the individual parts of the heat transfer line 3 are connected outside the reactor X, or each or any combination of at least two of them is connected to the heat transfer medium source separately so that it forms a separate heat transfer line 3 separated from the interior. reactor χ.

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

In operation of reactor X according to the invention, respectively. In carrying out pyrolysis of the bulk POO according to the invention, a heat transfer medium (gas, flue gas, etc.) is fed to the heat transfer medium line 3 separated from the interior of the reactor X, which heats the walls of the lower chamber 31 of the hollow shell 32 of the reaction space 320 and the upper chamber 33 ( in the case of the variant in Fig. 2a indirectly). At the same time, the feed 6 of the bulk POO is supplied to the interior of the reactor X with the POO, especially 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 by gravity onto the inclined surface of the upper chamber 33 - in the embodiment shown, to the top and / or near the upper cone 331 and moves downwardly on this surface, forming into a relatively thin layer, the thickness of which it gradually decreases by further displacement and increasing the size of the inclined surface. As a result, heat is transferred efficiently from the heating medium through the upper wall 33 of the upper chamber to the particulate POO and is well overheated throughout the volume, while exceeding the thermal stability limit of the organic compounds contained therein to cleave these compounds into a stable low molecular steam gas product. solid residue - t. j. to pyrolysis. Upon dropping of the particulate POO over the edge of the inclined surface of the upper chamber 33, the POO impinges on the upper wall 322 of the hollow shell 32 of the reaction space 320 and is directed into the reaction space 320 by design and / or relative positioning of the upper chamber 33 and the hollow shell 32 of 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 free-flowing POO then falls through the reaction space 320 onto the inclined surface of the lower chamber 31 - in the embodiment shown, to or near the top cone 311. After this surface, due to its inclination, it again moves downwards, forming a relatively thin layer. the 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 X towards the outlet 5 of the steam-gas pyrolysis products and in the reaction space 320 of the reactor X come into contact with falling particulate POO particles. increase the efficiency of their pyrolysis.

In the operation of reactor X 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 χ.

Upon exiting the reactor X, 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 X, or to generate the electricity required to operate reactor X and its operating elements. As a result, the operation of the reactor X according to the invention is energetically self-sufficient.

Solid pyrolysis products consisting predominantly of ash, slag or non-combustible POO, such as sand, stones, etc. they then fall into the bottom of reactor X and, due to its shaping, are directed to the outlet 4 of the 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 without further action. Another significant advantage is that any pyrolysis 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 using the reactor 1 according to the invention, pyrolysis takes place at a temperature in the range of about 450 to 650 ° C, but the design of the reactor 1 does not prevent it from being carried out at a higher temperature, if 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 comprising a heat transfer medium line 3 separated from the interior of the reactor 1 formed by a at least heated hollow shell 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.

PATENT CLAIMS

Claims (14)

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 to the reactor (1) and the outlet (34) of the heat transfer medium from the reactor (1) and which is separated from the interior of the reactor (1). 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 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 simultaneously separated from the interior of the 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 in the direction of movement of the solid bulk organic waste in the interior of the reactor (1), an upper chamber (33) is arranged upstream of the reaction space (32). at least one heated inclined and / or rounded surface facing at least partially 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) of the heat transfer medium to the reactor (1) and / or connected to the heat transfer medium inlet (30) to the reactor (1) 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 (D 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 inclined and / or rounded surface. directed at least partially to a solid bulk organic waste feed (6) to 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 surface (331), truncated cone or truncated cone with an inclined upper base. Reactor (1) according to claims 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 heat transfer medium inlet (30) to the reactor (1), and / or with the heat transfer medium outlet (34) from the reactor (1) via a hollow shell (32) of the reaction space (320) and / or a lower chamber ( 31), and at the same time 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 thermal insulation material. 4 drawings