EP1377649B1 - Installation and method for producing energy using pyrolysis - Google Patents

Abstract

The aim of the invention is to achieve a good energy balance, in particular in small energy-production installations, in which combustibles containing carbon are exploited by means of pyrolysis. To achieve this, the installation comprises: a) a reaction section provided with at least one pyrolysis zone for exploiting the combustible, b) at least one combustion device, used to burn the gas obtained by pyrolysis to form flue gas, c) supply means for supplying the gas from the pyrolysis zone to the combustion device, d) conduit means, in which the burning gas and the resulting flue gas can be conducted from the combustion device to a gas outlet point, e) a thermal utilisation device, which is used to convert at least one portion of the thermal energy that is released by the combustion process into a useful form of energy that can be output by the installation, using a heat exchanger, whereby f) the burning gas and/or the resulting flue gas is guided past the pyrolysis zone (8) and at the same time past at least one section of the heat exchanger (28a), in relation to the direction of flow, by means of one section of the conduit means (26), and whereby the heat exchanger (28a) absorbs the thermal energy of the gases in a first area (40) and in a second area (41) releases said energy into a medium of the thermal utilisation device.

Description

The invention relates to a plant and a method for energy production, as described in the preambles of claims 1 and 12.

It has long been known that pyrolytic processes can be used to energize waste or residual materials. As residues such as municipal and industrial waste, recycling sorting waste, waste and residual wood, sewage sludge, animal meal, etc. in question. In this case, the pyrolytic processes are based on degassing of the carbonaceous residues provided as fuels under high temperatures and essentially with the exclusion of oxygen. The energy contained in the resulting gases can be determined, for example, by combustion, i. Oxidation, which convert gases into thermal energy. Thermal energy is relatively easy to use, for example, to generate heat, cold or electricity.

Thus, various plant concepts have been proposed to win usable energy by means of a pyrolytic utilization of residues. One of the first concept plants became known under the name "Thermoselect". This envisages degassing the residues in a temperature range of 450 ° C to 550 ° C. The remaining wholly or partially charred residual from this process then pass into a carburetor part of the plant, in which they are gasified with supply of natural gas and oxygen at 1200 ° C to 2000 ° C. The resulting synthesis gases are then cooled in a wet process and used after various purification stages for energy and a partial flow for heating the pyrolysis zone. The disadvantage of the system is its high complexity. Especially because of Due to the high technical effort required for the process that can be carried out with this plant, only large plants with a volume of around 100,000 tonnes of residues per year seem to be profitable.

Another, under the name Carbo-V process, become known method provides to decompose mainly wood-containing residues in a first reactor by partial oxidation into their volatile and solid constituents. The solid constituents, predominantly carbonaceous coke, are ground. In a second stage, the resulting, very tar-containing gas is post-oxidized in the upper part of a combustion chamber, while in the lower part of the combustion chamber, the coke dust is converted into gasification gas. This gas is cooled and purified several times along with the first stage synthesis gas. The purified gas is then provided for generating useful energy. In this method, the complex wet cleaning can be seen as a disadvantage. The system required for this process must also be relatively large and complex for economical operation. Moreover, this process is essentially intended only for the energy recovery of wood.

Another concept is shown in EP 0 874 881 B1. Here only solid fuels should be used. The solid fuels are subjected to pyrolysis in a pyrolysis zone of the plant, with the supply of catalysing substances, a gasification. The gases obtained by both pyrolysis and gasification are then burned, with some of the energy recovered from the combustion being used first to heat the pyrolysis zone with radiant heat. The combustion gases are then passed into another part of the plant downstream of the pyrolysis zone in the flow direction of the gases in order to use the energy content remaining in the gases there.

At this plant can be considered disadvantageous that a great effort for the isolation of those parts of the system is required, in which the combustion gases are conducted at high temperatures. In addition, it has been shown that this system concept only leads to economic results if comparatively large systems are thus realized, for example of the order of magnitude of greater than 10 MW of thermal power.

In DE-A-2651302 a plant according to the preamble of claim 1 is disclosed, in which the gases are first fed to an outer surface of the pyrolysis tube in order then to pass via a conduit far from the pyrolysis tube to a heat exchanger. Only the heat exchanger performs a conversion into a useful energy form, namely water vapor.

WO-A-97/15641 also discloses a plant in which the hot combustion gases produced by degasification and pyrolysis can be used conventionally for steam generation.

The invention is therefore an object of the invention to provide a generic system and a method that allow a good balance of energy even with small plant size.

This object is achieved in a system of the type mentioned in the present invention that the combusting gas and / or the resulting flue gas by means of a portion of the conduit means, and with respect to their flow direction, at the same time with the passage to the pyrolysis substantially also at least one Section of a heat exchanger are passed, wherein the heat exchanger receives in a first region thermal energy of the gases and emits them in a second area to a medium of the heat utilization device. The object is also achieved by a method as described in claim 12.

In systems according to the invention, it is thus provided that a portion of a stream of hot combustion or flue gases produced during combustion is not supplied, as in the prior art, exclusively to successive different recycling purposes, but preferably already during combustion and immediately thereafter substantially simultaneously is used both for heating the pyrolysis zone as well as for the release of thermal energy to a heat exchanger.

Essentially regardless of how this is realized constructively concrete, thereby at least a significant part of the previously required isolation can be omitted. On the contrary, according to the invention is just provided that in the section of the conduit means in which a heat transfer to the pyrolysis takes place, in addition, a further heat transfer to take place, namely a heat transfer at the heat exchanger. Unlike in the prior art, this part of the conduit should advantageously have a particularly good thermal conductivity.

It is hereby preferred that by a vote of the heat transfer at the heat exchanger on the heat transfer to the pyrolysis zone predefined physical conditions are created. This is intended to keep the temperature prevailing in the pyrolysis zone at a value which is favorable for the pyrolysis, within a certain temperature range. This temperature range may be, for example, from 850 ° C to 950 ° C. By knowing the temperatures of the flue gases or the combusting gases, their amount and the geometric design of the conduit, the pyrolysis zone and the heat exchanger, such conditions can be adjusted by a suitable choice of material. As a result, the amount of energy contained in the flue gases is available for the heat exchange process, which exceeds the amount of energy that is needed to heat the pyrolysis zone.

It has been found that the temperature of the combustion gases during combustion or immediately thereafter in a range of about 1000 ° C to 1200 ° C, preferably from 1050 ° C to 1150 ° C and more preferably about 1100 ° C, is located on the one hand to have good results in the pyrolysis process and on the other hand a sufficient amount of energy for the generation of useful energy available. This temperature range has also proved to be particularly advantageous because at On the one hand certainly no recombination of the combustion or flue gases to dioxins and furans takes place at these temperatures. On the other hand, the temperatures are high enough to lead the flue gases over a longer distance in the conduit means before they cool to temperatures at which such recombinations would be to be feared in significant quantities.

Due to the immediate use of the thermal energy released by the combustion, both for the pyrolysis and for the heating of a heat exchange medium of the heat utilization device, particularly low energy losses occur in systems according to the invention. This significantly increases the energy balance of such a system and also allows the operation of small systems in terms of size and the amount of energy gained. However, this advantage can also be used to generate a larger usable amount of energy with the same plant size as in a conventional system.

In order to heat both the pyrolysis zone and the heat exchanger simultaneously in a structurally simple and favorable manner with a section of a volume flow of flue gases, in a preferred embodiment a flow space for the second boundary surface opposite a first boundary surface and a second boundary surface opposite the first boundary surface Be formed gases. In this case, the pyrolysis zone should adjoin the first boundary surface and the second boundary surface should be part of the heat exchanger.

It has proved to be particularly favorable when the pyrolysis zone has at least one substantially elongated tube which is surrounded by an annular conduit means, the longitudinal extension of which can extend substantially parallel to the longitudinal extent of the pyrolysis tube. in this connection For example, an (outer) wall of the pyrolysis tube can also function as an inner wall of the conduit means, whereby a particularly good heat transfer into the pyrolysis zone is possible. An outer wall of the conduit means, however, may be formed as a heat exchanger, whereby also a particularly good heat transfer to the heat exchange medium with very low heat losses is possible. This also makes it possible to realize an inventive system with a particularly low design effort.

In a preferred embodiment, the pyrolysis tube and the conduit means are each circular in cross-section with the conduit means concentrically surrounding the pyrolysis tube. In other embodiments, a plurality of pyrolysis tubes can also be arranged in an annular cross-sectional conduit means, wherein the cross-sectional shapes of the conduit means and the pyrolysis tubes can be optimized with regard to good heat transfer. In principle, the cross-sectional shapes of the tubes can be chosen almost arbitrarily.

In a further preferred embodiment, the heat exchanger discharges the energy to a boiler in which water vapor is generated, which in turn can be used to produce a usable form of energy, such as heat, cold or electricity. In terms of good heat transfer and to avoid insulation material for the conduit means, it may be advantageous if the conduit means and thus also the heat exchanger are arranged over at least a portion of the conduit means completely within the kettle. This may have the consequence that the pyrolysis zone, at least over a section along a conveying path of the fuel through the pyrolysis zone, is also located completely within the heat exchanger and thus also the heat exchange medium.

In a further preferred embodiment, the system according to the invention can be provided with a control circuit in which one or more parameters of the water vapor emerging from the boiler are measured. These measurement results can be used to control the feed rate of fuel into the pyrolysis tube so that the values of the vapor parameters are set to be substantially constant.

In order to be able to produce different systems according to the inventive principle, for example with regard to the size of the systems, with a particularly low constructional and production engineering effort, these systems should have a modular construction. This means that the systems can be provided with predefined interfaces to which system components can be interconnected by preferably detachable connections. This also makes it possible to adapt existing systems quickly and with little effort to changing conditions.

Further preferred embodiments of the invention will become apparent from the dependent claims, the description of the figures and the figures.

Fig. 1

ein grundsätzlicher Aufbau einer möglichen erfindungsgemässen Anlage;

Fig. 2

eine Querschnitts-Darstellung eines Ringbrenners der erfindungsgemässen Anlage;

Fig. 3

eine Längsschnitt-Darstellung einer weiteren möglichen Ausführungsform eines Ringbrenners.

Fig. 4

einen Querschnitt entlang der Linie X von Fig. 1 durch ein Pyrolyserohr und einen Teil eines Wärmetauschers.

The invention will be explained in more detail with reference to an embodiment schematically illustrated in the figures; show it:

Fig. 1

a basic structure of a possible inventive system;

Fig. 2

a cross-sectional view of a ring burner of the inventive system;

Fig. 3

a longitudinal sectional view of another possible embodiment of a ring burner.

Fig. 4

a cross-section along the line X of Fig. 1 by a pyrolysis tube and a part of a heat exchanger.

In Fig. 1, an inventive plant for the conversion of residues is shown in energy. The plant has an input point 1, can be given in the residual material 2 in an intermediate silo 3 of the plant. The intermediate silo 3 is used for intermediate storage of residues 2 before they are fed to the recovery described in more detail below.

At a lower funnel-shaped end of the intermediate silo, a arranged in a downpipe conveyor 4 follows. The feed wheel 4 and / or stored in the silo 3 residues 2 conclude on this side of the plant the latter substantially airtight. The downcomer opens in the region of one end of a horizontally oriented tube 5 in the latter. In the tube 5 a rotatably driven screw conveyor 6 is arranged, which promotes the residues 2 in the region of the other end of the tube 5. Here, an opening is present in the tube 5, through which the residues pass through a further downpipe 7 into a region of a front end of a pyrolysis zone designed as a pyrolysis tube 8. Also in the pyrolysis tube 8 a rotatably drivable screw conveyor 9 is arranged, with which the residues 2 are conveyed from an inlet opening 8a to a provided at the other end of the pyrolysis tube lower outlet opening 8b. The pyrolysis tube 8 is sealed against an air inlet. By the preferably substantially anaerobic pyrolysis occur in the interior of the pyrolysis tube temperatures of about 850 ° to about 950 ° C, preferably about 900 ° C.

The latter end of the pyrolysis tube opens into a silo-like container 10, in which below the pyrolysis tube 8 a gasification chamber 11 and above a gas mixing chamber 12 is formed. Like the pyrolysis tube 8, the gasification chamber 11 also belongs to a reaction part of the plant. The residual substances 2, which have passed through the pyrolysis tube 8 and an essentially anaerobic pyrolysis, thus fall downwards into the gasification chamber 11 provided with a lower funnel-shaped end due to gravity through the outlet opening 8b of the pyrolysis tube 8. The funnel-shaped end finally ends in another Pipe 14 with screw conveyor 15 through which the end products of the gasification process, essentially ash or slag, in a predetermined amount and time can be removed from the plant. By one arrow 16, 17, 18, three possible discharges are indicated with which alternatively or cumulatively water vapor (with a temperature of about 300 ° C), recited exhaust gas (with a temperature of about 200 ° C) and / or a heated to about 200 ° C preheated oxygen / nitrogen mixture can be introduced into the gasification chamber. As a result, a gasification of the already pyrolyzed residual or fuels at temperatures of about 750 ° C to 850 ° C is possible, whereby, for example, the gases hydrogen (H ₂ ) and carbon monoxide (CO) can be released.

The gasification chamber 11 is connected to the outlet opening 8b of the pyrolysis tube 8 and bypass channels arranged on both sides thereof around the pyrolysis tube with the gas mixing chamber 12. The resulting in the pyrolysis tube gases, such as methane and carbon monoxide, thus can escape through the outlet opening 8b upwards also in the gas mixing chamber 12.

About a connected to the gas mixing chamber 12 supply line 20, the gas mixing chamber is connected to a burner having a ring burner 21. The combustion device 21 is in this case arranged over the full circumference of the pyrolysis tube 8 around the latter. The in Fig. 2 in a first embodiment in a cross-sectional view shown in more detail laterally arranged next to the gas mixing chamber annular burner uniformly distributed on the circumference of the conduit means a plurality of burners 22, for example, eight burners - but at least one burner on. In a manner not shown each of the burner 22 is connected to the gas supply to the supply line 20. The burners 22 may in this case be oriented such that the gas flowing out of them and initially burning in a flame 24 has a predetermined flow direction component 25 or a flame direction which runs tangentially to the pyrolysis tube 8, so that the pyrolysis tube is heated as evenly as possible. In Fig. 2 it is shown that thereby an alignment of the flame 24 of each burner 22 is made possible on the flame 24 of the circumferentially subsequent burner 22. This can be achieved safely and in a structurally simple way that the individual burners 22 of the annular burner ignite each other.

The stream of still combusting gases produced by the burners 22 and flue gases already formed by combustion may preferably also have a flow direction component which runs parallel to the longitudinal extent 8c of the pyrolysis tube 8 and opposite to the passage direction of the fuels 2 in the pyrolysis tube. In the longitudinal sectional illustration of FIG. 3, such an embodiment of a firing device 21 is shown in which the flame direction 25 of the individual burners 22 are inclined and directed onto the longitudinal axis 8c of the pyrolysis tube. As can be seen in particular in this illustration, a conduit means 26 described in more detail below is closed at its end 26a in the region of the firing device 21.

FIGS. 2 and 3 show extreme positions of the individual burners 22. Thus, the burners 22 in FIG. 2 are aligned completely tangentially to the pyrolysis tube 8, the orientation of the flames 24 having no component parallel to the longitudinal axis 8c of the pyrolysis tube. In Fig. 3, however, the direction of the flames 24 has no tangential component. As a result, the flame direction 25 lies in each case in a sectional plane through the longitudinal axis 8c of the pyrolysis tube. In other, not shown embodiments, the individual burners of the burner can also occupy any position between the extreme positions shown in the two figures, which can be achieved for example by pivoting the burner shown in Fig. 2 by an angle less than 90 °.

As can be seen in Fig. 1, a start / support burner 27 is provided in the peripheral region of the annular burner, with which the annular burner can be ignited on the one hand. For this purpose, the flame (not shown) generated by the start / support burner 27 may be directed to at least one of the burners 22 of the annular burner. On the other hand, the start / support burner 27 can also be used if too small amounts of energy are supplied by the ring burner. The start / support burner 27 may be powered by an external fuel supply.

In the embodiment of FIGS. 1 and 2, the annular burner 26 may be integrated at one end of the conduit means 26 in this. The conduit means 26 may initially be formed as a cross-sectionally annular, substantially rectilinear pipe 28. The annular tube 28 is in this case arranged concentrically around the pyrolysis tube 8. As a result, the concentric tube 28 surrounds the pyrolysis tube 8 over its entire length, the longitudinal axes of the two tubes being identical. In order to allow a good heat transfer from the annular tube to the pyrolysis tube, they have a common tube wall 29 made of a material with good thermal conductivity on. For this purpose, especially metallic materials, such as alloyed steel and cast steel, in question.

The annular tube 28 merges at an end opposite the firing device 21 into a first curved region 30 with a deflection angle of 180 °. In the curvature region 30, the one volume of the conduit means fanned into a plurality of individual tubes in a straight line and parallel to each other and to the annular tube 28. For reasons of simplification, this plurality of tubes is shown in FIG. 1 as only a single tube 31. By fanning the total area can be increased at which a heat transfer can take place. A second curvature region 32 is located at an end of the tubes 31 opposite the first curvature region 30. Here, too, the conduit means is deflected by 180 ° and divided into a further enlarged number of individual tubes 33 (also shown as a single tube) running parallel to one another. A third curvature region 34 then adjoins in the direction of flow, in turn increasing the number of individual tubes. From the third curvature region 34, the conduit means extends to a so-called quenching means 36, which is provided for the shock cooling of the flue gases.

As is apparent from Fig. 1, the previously described meandering portion (reference numerals 28 to 34) of the conduit means 26 is located approximately from the combustor 21 to the third curvature region 34 in a water-filled closed vessel 37. This section of the conduit means and Boiler 37 thus form a so-called three-pass boiler, which serves for heat recovery. At an upper end of the boiler 37, a steam line 38 is connected to these. Through this, the resulting due to the heating of the water vapor becomes a Device 39 out, in which the energy content of the water vapor for the production of useful energy, such as electricity, heat or cold, is used. Said section (28 to 34) of the conduit means 26, in particular the (outer) jacket of the annular tube 28 shown in more detail in FIG. 4, thus serves as a heat exchanger 28 a, with which a part of the energy content of the burned gases guided in the tube 28 to the Water of the three-pass boiler is discharged. In this case, the heat exchanger 28a absorbs thermal energy from the hot gases on an inner surface 40 of the tube 28 and discharges it to the water on an outer surface 41 of the tube 28. The respective same section of the volumetric flow of the gases simultaneously emits another part of its thermal energy to the pyrolysis tube 8 on an outer surface 42 of the tube wall 29. This part of the thermal energy can be used via an inner surface 43 of the tube wall 29 by radiant heat or by heat transfer to heat the contents of the pyrolysis tube.

With the designated in Fig. 1 with 36 quenching means the flue gas within a very short time, for example within 0.2 sec. From about 450 ° C to about 200 ° C, cooled. For this purpose, for example, water can be injected into a chamber through which the flue gases are carried out. The quenching process avoids recombinations of the flue gases to dioxins or furans or, at the most, allows them to be harmless enough. In a further section 44 of the conduit means 26, the thus cooled flue gases reach a known flue gas cleaning device 45. This has filters with which particles are removed from the flue gas stream. The filtrate, essentially filter dust, is collected in a container 46 for subsequent removal.

The thus cleaned flue gas now leaves the flue gas cleaning device 45 and passes over another section 48 of the conduit means to a trained as a suction fan 49 vacuum means. The induced draft fan 49 promotes, on the one hand, the flow of purified flue gas to a chimney 50 provided Rauchgasauslassstelle. The induced draft fan 49, on the other hand, generates at its installation location in the conduit means 26 a negative pressure which can act with respect to a direction opposite to the direction of flow up to the intermediate silo 3. The negative pressure causes a substantially constant volumetric flow of the flue gases through the line 26 closed against the entry of air. It may also be provided that the oxygen required for the combustion in the region of the combustor 21 alone due to the negative pressure acting in the combustion device or at least with its support is sucked. Likewise, the negative pressure for conveying the gas from the gas mixing chamber 12 to the combustor 21 can be used.

The system may also be provided with a control device, not shown in the drawing, with the parameters of the emerging from the boiler 37 water vapor can be set as substantially constant. For this purpose, parameters of the steam, such as pressure, quantity and temperature, can be measured in the region of the steam outlet, for which reason temperature, quantity and pressure sensors can be present at one or more locations in the steam line.

Based on the measured values, it is then possible to influence the amount of the substances introduced into the pyrolysis tube 8. Thus, for example, in the case of falling or already too low values of the steam parameters, the entry of residues can be increased in a predetermined manner. It can also be provided that in addition the start / support burner is turned on.

As a result of this regulation, depending on the concretely existing conditions in a system according to the invention, for example the heat transfer and the amounts of material to be pyrolyzed, it can be achieved that the combustion temperature of the gases is approximately from 1050.degree. C. to 1150.degree. Preferably, the temperature is kept as constant as possible within this range, for example at about 1100 ° C. This makes it possible to provide in the pyrolysis tube in a range of 850 ° C to 950 ° C as constant temperature conditions as possible to adjust the available per unit time at the Dampfauslassstelle usable amount of energy as constant as possible.

Claims (18)

1. Installation for producing energy, in which the pyrolytic utilization of carbon-containing fuels takes place, comprising
   a reaction component (8) provided for the utilization of fuel which is provided with at least one pyrolysis zone in which a gas can be produced by means of pyrolysis,
   at least one combustion device (21) with which the gas produced in the pyrolysis is combustible with input of oxygen, whereby flue gas is formed,
   delivery means (20) for supplying gas from the pyrolysis zone into at least one combustion device (21) ,
   a transfer installation (26) in which the combustion gas and the flue gas resulting from it are feedable from the combustion device (21) to a gas output point, wherein with the transfer installation the combustion gas and/or the resulting flue gas can be led past the pyrolysis zone, in order to use the thermal energy produced by the combustion for heating the pyrolysis zone,
   a heat recovery device (39) with which at least one part of the thermal energy liberated from the installation by the combustion is transformable by use of a heat exchanger (28a) into a useful energy form.
   characterized in that,
   the heat recovery device (39) is arranged so that the combustion gas and/or the resulting flue gas is led in relation to the flow direction by means of a section of the transfer installation (26), essentially simultaneously with being conducted around the pyrolysis zone (8) also past at least a section of a heat exchanger (28a) whereby the heat exchanger (28a) absorbs thermal energy of the gases in a first section (40) and releases it in a second section (41) to a medium of the heat recovery device (39).
2. Installation according to claim 1, characterized in that between a first boundary area and a second boundary area lying opposite the first boundary area of a section of the transfer installation (26) a flow space for the gases is formed, wherein the pyrolysis zone (8) abuts the first boundary area and the second boundary area is a component of heat exchanger (28a).
3. Installation according to one or both of the preceding claims, characterized in that, at least the section of the transfer installation (26) is formed as an annular pipe (28), which surrounds the pyrolysis zone (8) and is an outer wall (29) of the annular pipe (28) component of the heat exchanger (28a).
4. Installation according to one or more of the preceding claims 1 through 3, characterized in that the section of the heat transfer installation (26) is arranged so that at least one component of the flow direction of the gas runs parallel to the longitudinal extension of the pyrolysis zone (8).
5. Installation according to claim 4, characterized in that at least the component of the flow direction is aligned substantially opposite to a flow direction of fuel in the pyrolysis zone.
6. Installation according to one or more of the preceding claims, characterized by a gasification zone in the region of an end of the pyrolysis zone, in which by feeding in oxygen and/or oxygen-containing materials gasification of already pyrolized fuels takes place.
7. Installation according to claim 6, characterized in that the gas from the pyrolysis zone is fed with the feeding-in means to the combustion device together with the gas produced in the gasification zone.
8. Installation according to claim 7, characterized in that in relation to the flow direction of the flue gas between the heat exchanger and the gas outlet point a reduced pressure means, for production of a reduced pressure in the heat transfer installation is arranged.
9. Installation according to claim 8, characterized in that the reduced pressure means is constructed as a suction draft ventilator.
10. Installation according to one or more of the preceding claims, characterized in that the heat exchanger is formed as a multi-pass boiler, especially as a two- or three-pass boiler.
11. Installation according to one or more of the preceding claims, characterized by a modular structure, in which functional modules of the installation can be fastened to the installation by detachable connections and are removable from the installation by detachment of the connections.
12. Method for producing energy, in which a pyrolytic utilization of carbon-containing fuels takes place, comprising
    an entry for fuel materials into at least one pyrolysis zone (8), in which a pyrolysis may be carried out.
    a combustion of the gases produced by means of the pyrolysis by feeding of oxygen, whereby flue gas is produced,
    another piping of the resulting flue gas from the combustion device (21) towards a gas outlet point, wherein by means of a heat transfer installation (26) the burning gas and/or the resulting flue gas is feedable past the pyrolysis zone (8),in order to use the thermal energy produced from the combustion device for heating the pyrolysis zone (8), and the gas is feedable to a heat recovery device (28), where at least one part of the freely developing thermal energy from the combustion is convertible into a useful deliverable energy form by utilization of a heat exchange process,
    characterized in that
    a stream of combustion gas and/or the resulting flue gas is led past in the flow direction in a section of the heat transfer installation essentially simultaneously at the pyrolysis zone (8) and at least one section of a heat exchanger, wherein the heat exchanger (28a) absorbs the thermal energy of the gas in an initial section and this is released in a second section to a medium of the heat recovery device (28).
13. Method according to claim 12, characterized in that the flue gases in the initial section of the heat transfer installation at the pyrolysis zone as well as also at the heat exchanger are led past and flow in a second section exclusively along to the heat exchanger.
14. Method according to one or both of the previous claims 12 and 13, characterized in that the medium is water and steam is produced through the heat exchange process.
15. Method according to one or more of the previous claims 12 through 14, characterized in that in the heat transfer installation a reduced pressure is produced, which is used to produce a flow of the flue gases.
16. Method according to claim 15, characterized in that the reduced pressure is used for feeding the gases provided for the combustion to a point in the installation at which the combustion is carried out.
17. Method according to one or more of the preceding claims 12 through 16, characterized in that the fuels after passing through the pyrolysis zone are carried over into a gasification chamber and there with fed-in oxygen or oxygen-containing materials gas production is carried out by means of gasification.
18. Method according to claim 12, characterized in that by means of a control step, in which one of the dependant parameters of the heat exchange process is measured and based on this measurement the input of fuels into the installation is varied.

Images