DE102004008621A1 - Transportable or stationary hearth-type furnace reactor, to transform solid and paste organic materials to processed gas, comprises cubic reactor, vapor inlet, a chain conveyor, a cover with passages and a supporting flame mechanism - Google Patents

Abstract

Transportable or stationary hearth-type furnace reactor (I), for the transformation of solid and paste organic materials to processed gas, comprises cubic reactor (1); vapor inlet (8); a chain conveyor (9); a cover with passages (12); and a supporting flame mechanism (16). Transportable or stationary hearth-type furnace reactor (I), for the transformation of solid and pasty, organic materials in gas process, comprises cubic reactor (1) (with an appropriate separator on the side panel outside the reactor, at the funnel (3) with a valve (4) to check air flow and at the lower end of the funnel, a screw-conveyor (5) is arranged that opens or enters by a opening into the reactor wall above a hot plate (6), where the hot plate (6) at the bottom of the reactor as multiple heating elements above heater (7) at lower surface), vapor inlet (8) (arranged under the screw-conveyor above the hot plate), a chain conveyor (9) (arranged over the entire length of the hot plate, in which rake elements (10) are fixed above the hot plate at certain distances, at the end of the chain conveyor, a shaft (11) (for collecting ash and residual substances) is arranged at the bottom of the reactor, which has a valve to check air flow and another screw-conveyor at the bottom), a cover with passage (12) (arranged on the heater (13) present on the upper surface of the chain conveyor, which separates the reactor into a gas production area (14), gas collecting area and a reaction area (15)) and a supporting flame device (16) arranged at the side of reactor space wall in the reaction area and in the cover of the reactor or in the upper side wall of a gas detector (17). Independent claims are also included for: (1) a method of transforming solid and paste, organic materials into processed gases, comprising (I), where on continuous going through the materials, which can be treated by (I) with the help of the mechanically propelled transport devices such as rake elements, scratching broom or hod screw; degassing takes place in the first stage under air-lock with 280-600[deg]C (preferably with approximately 500[deg]C) via an indirect lower heater of the hot plate and via an upper heater in the gas production area, in which the materials can be treated are transported with a high protection of approximately 5-10 cm by transport devices practice-grounded over the hot towards shaft; the gas primarily developed in the second stage under stochiometric air supply burned with approximately 850-950[deg]C in the gas collecting area and reaction area, in which the inflammable components of the volatile content (CH2 and CO) as well as the dampness are converted completely to CO and H2; and in the third stage the developed gases of the second stage are burned by air supply in a following area at approximately 1000-1200[deg]C to carbon dioxide and water; and (2) a method for separating thermal bonding material from construction units and work pieces in the material (in the form of rubber/metal or plastic/metal) for the recovery of the metallic construction units including an open-hearth furnace reactor comprising allowing in and drawing out (I) from the lattice boxes in clockwise direction.

Description

Incinerators for Burning garbage or Other waste materials are in a variety of embodiments known. In the generation of energetic process gases from organic Materials such as rotary kilns, fluidized bed reactors, shaft furnaces and specially designed grates are used. The indirect heating of the rotary kiln is done from the outside by the heating of the Rotary tube shell. The shell inner surface forms the heating surface for the starting materials. The heat transfer is done by convection and radiation and causes the thermal decomposition the hydrocarbons in process gas. In the fluidized bed reactor is formed the vortex effect due to the injection of gases. It is preferably atmospheric Air. Depending on the process engineering design, water vapor comes in parallel for use. The fluidized bed technology requires a so-called Bed material that leaves the reactor by the vortex effect and it is supplied again by appropriate devices. The discontinued feedstocks are shared with the bedding material the vortex effect and are preferably due to the exothermic reaction heated from the partial oxidation of carbon and thermal disassembled or gassed depending on the process. The litigation in shaft furnaces both in the interest of producing energetic process gases in cocurrent as well as in countercurrent with respect to gasification agent and feedstock. Again, the required temperature for the thermal Decomposition preferably produced by partial carbon oxidation.

Of the Rotary kiln limited on the thermal decomposition of hydrocarbons in process gas. The seals of the rotary tube ends are problematic. Since such systems are operated in the negative pressure, the access is of false air can not be excluded. This will produce the quality of the product Process gas reduced in relation to its calorific value. Since the rotary tube jacket from the outside heated evenly is, a differentiated temperature control is not possible. Provided Starting materials after heating to build up on the heating surfaces tend, forms a coating on the rotary tube inner surface, the the heat transfer can significantly reduce. A removal of these attachments is only during a business interruption possible.

Of the Fluidized bed reactor can only operate in a narrow power range be because the gas that produces the vortex effect, at the same time the Task of the reaction agent takes over. The separation in reaction zones is also not possible. Of Furthermore, the fluidized bed reactor places high demands on the Characteristic of the starting materials. Small particle sizes are required. This requires a high conditioning effort for the starting materials.

gratings in conventional design are for the process gas generation unsuitable. There are developments of special Devices of this type, but so far only process gases could be produced with relatively low calorific value.

Of the Shaft furnace reactor places high demands on particle size and particle size distribution of the feedstock, to ensure a uniform flow through the To ensure reactor cross-section. Larger gas quantities flow through the loose bed in the wall area (Randgängigkeit). At unfavorable Particle size distribution form the so-called blowers. This is the shaft furnace reactor to guarantee a consistent process gas quality hardly. The temperature required for thermal decomposition of the hydrocarbons is also preferably by partial oxidation of the carbon reached.

In summary It can be seen that the named methods are a high calorific value Process gas can not guarantee.

Among the multitude as the most obvious solution of the prior art is the DE 44 08 654 listed. In this document, a furnace for the smoldering of solids is described, within a furnace housing a treatment chamber with a belt system and a combustion chamber in which the combustion of a fuel takes place and the carbonization gases from the treatment chamber and possibly air can be supplied. The treatment chamber and the combustion chamber are spatially separated in the furnace. Thus, the heat contained in the combustion gases can be delivered to the treatment chamber maximum and a uniform heating even elongated treatment chambers is possible, the combustion chamber has at one end an axially attached jacket tube which communicates with the combustion chamber and is closed at the other end , The jacket tube has a smaller-diameter inner tube, which ends at a distance in front of the closed end of the jacket tube and is guided through the combustion chamber to the outside and between the inner tube and jacket tube has a guide coil for the burner gases.

By solution after DE 44 08 654 However, no successive process stages that work with different temperature ranges can be realized. The individual steps of the combustion process: preheating, drying, degassing and gasification of the solid residues so As burning of the released gases run largely uncontrolled, which is to be regarded as the cause of the frequently occurring malfunctions. These disturbances are intensified mainly by the dust that is discharged with the gases generated from the combustion chamber. Depending on the nature of the raw materials used and the nature of the softening and melting behavior of the ash fractions in these bars, these dusts can form considerable batches on individual parts of the plant in a very short time, which involves at least a considerable need for repair. Not infrequently, these phenomena even lead to the decommissioning of entire plants. The same applies to pyrolysis plants, which are often preceded by combustion processes. The initially generated pyrolysis gases contain, in addition to rods, condensable hydrocarbons which are deposited on cold parts of the installation and can even intensify the formation of deposits. In addition, the countermeasures to be taken in detail lead to a noticeable deterioration in the energy yield, so that it is then almost impossible to speak of an energetic use of the raw materials used. This is especially the case when the primarily generated combustion gases carry considerable loads of pollutants with it.

Of the The invention is based on the problem, devices and methods for the thermal treatment of solids from solid and / or pasty, organic Substances by thermal decomposition of hydrocarbons an energetic To produce process gas and then preferably in a external thermo-chemical reaction, the process gas to a synthesis gas convert.

With The invention ensures that a clean disposal of solid and / or pasty, organic Substances and biomasses, such. As tar oil residues to trouble ash residues and to carbonaceous residues can, with the carbonaceous residues of another incinerator supplied can be. The be called Exhaust gases from the system are used simultaneously to operate the system. The invention allows the generation of a heat-rich process gas and thus a high efficiency in the context of energy recovery of the gas. It will therefore be an additional Energy production possible.

The inventive method Serves devices that largely affect the process the thermal decomposition of hydrocarbons allows. There is no atmospheric Air is used, the process gas is through the atmospheric nitrogen and forming in greater quantity Carbon dioxide is not "diluted." By the indirect Heating is the thermal decomposition of hydrocarbons by the addition of water vapor and optionally a small amount Amount of air. The resulting process gas is considered to be particularly heat rich classified. The used for indirect heating in a variety Allow heating elements a different temperature control, based on the reaction path, the starting materials within the device according to the invention return. By varying the working speed of the conveyor elements for the Input materials can be influenced directly by their residence time.

His particular suitability show procedures and devices during disposal of residues due to their particular characteristics at warming are classified as problematic. There is an extensive one Suitability for feedstocks in different particle sizes. An adaptation the feedstock conveyors within the reactor both on fine-grained material and on Material characterized by larger particles is guaranteed become. A special area of application is found in the thermal Composite separation. Here is a special added value possible because the metal parts have a high processing value. They are in the Composite material rubber / metal and plastic / metal before and can be used for Reuse fully back be won.

Advantageous embodiments of the hearth furnace reactor are described in claims 2 to 18, the method in claim 19 with advantageous method steps in claims 20 to 32. In the development according to claim 2, a trough auger or more are arranged side by side in place of the chain conveyor. The trough slug runs in a trough, on the stove plate stands. However, the stove can also be designed as a trough. In the development according to claim 3, a plurality of successive scratching brush are arranged in place of the chain conveyor. The scratching brushes are all lowered at the same time, laterally movable, liftable, reversible and lowered again. In the development according to claim 4 and 5, instead of the chain conveyor above the hot plate from outside the reactor space electrically driven rollers, z. As steel or other suitable materials, arranged with which grid boxes that take over the material transport through the hearth furnace reactor, are moved through the hearth furnace reactor. Of course, the grid boxes can also have wheels or be moved on slide rails by means of a pusher through the hearth furnace reactor. At the beginning and at the end of the hearth furnace reactor locks are provided for the grid boxes. All these variants each serve for the processing unterschiedli Residues also in terms of their size. According to claim 6, the air gap between the stove plate and the scraping elements or the scratching brush can be reduced within the hearth furnace reactor in the direction of good issue. As a result, the transport of the fabric residues through the reactor can be simplified according to the type of fabric. In the development according to claim 7 and 8, the reaction space is missing. The closed upper heating without passages is located directly on the ceiling of the reactor. This special version is intended for special process steps. In the gas outlet here preferably a coarse filter is arranged. Outside the reactor according to claim 9, a combustion chamber and a fan and a downstream fireplace are arranged. The blower serves to discharge the exhaust gases into the chimney. In the passages of the upper heating in the reactor chamber ceramic filters are provided according to claim 10. Due to the large number of through holes in the ceiling hardly strong air currents occur. However, to avoid further transport of dust particles, these filters are arranged in the through holes. According to claim 11, the hot exhaust gases of the system are used for the indirect heating. Excess exhaust gases can for the heating of other processes or z. B. be used for electric energy. In the development according to claim 12, the upper and lower heating of individual channels. These channels are adjustable in their temperature. Thus, different temperature ranges can be generated in the different sections of the hearth scratch oven. This can be z. B. with a different composition of the residues to be processed and with a blending of other foreign additives and their gasification advantageous. According to claim 13 heating elements can be provided in the side walls of the reactor. According to claim 14, the furnace wall of the portable hearth scratch oven consists of a sheet metal construction with intermediate stiffening profiles and heat insulation material. At appropriate places maintenance openings and additional openings for the measuring and control devices are provided. As a result, an easy cleaning of the furnace is given. In order to facilitate the transport of the furnace, a transport frame is provided according to claim 15 under the oven. To increase the safety of the furnace according to claim 16, all drives, z. B. also arranged for pacemaker system of the scratching brush outside the furnace chamber. According to claim 17, several hearth furnace reactors can be connected in series, the z. B. also different types of funding, z. B. first have a chain conveyor and then a trough auger. Through this series connection of the reactors, coarse residues are processed in the first reactor, which are comminuted by the thermal treatment and further treated thermally in the following reactor. Between two reactors can be interposed according to claim 18, a roller mill for further crushing the piece size of the goods.

When An advantageous variant of the method can according to claim 20 an afterburning in an external combustion chamber, ie outside of the reactor. Likewise, the further processing the process gas to a synthesis gas according to claim 21 also done externally. In the variants of the method according to claim 22 and 23 are in an external downstream apparatus the remaining hydrocarbon fractions of a gasification reaction or incinerated. According to claim 24 is in the reaction chamber at the stoichiometric and used in the afterburning a support flame device. In the variant according to claim 25 is in the gas generating space and in the reaction space of the hearth furnace reactor for the stoichiometric Combustion of water vapor used as a reactant. hereby a strong soot formation is avoided. According to claim 26 becomes Avoidance of uncontrolled air access in the area of the good task and the good issue sealing gas deducted by a barrier gas withdrawal. Thereby the resulting gas is very high in heat. In the claims 27 and 28 become the gases produced at the different places at least partially for used the heating of the system. In the variants according to claim 29 and 30, the method is followed by another Herdofen reactor continued. In terms of the funding system by the hearth furnace reactors Equipped or different conveyor systems be used per hearth furnace reactor. According to claim 31 is a fan outside the hearth furnace reactor as Saugzuggebläse to generate a negative pressure used in the hearth furnace reactor. The blower thus conducts the gas Combustion chamber. According to claim 32 is in the thermal composite material separation at Components of rubber / metal or plastic / metal with inclusion the furnace furnace reactor design according to claim 4 and / or 5, the entry and exit of the grid boxes in the and performed from the hearth furnace reactor in the cycle mode. For this locks are used on the hearth furnace reactor. This is to minimize the heat losses when loading the stove furnace reactor.

The for the Generation of combustible process gases from hydrocarbon-containing firm and pasty However, fabrics described above can also be used for completely different purposes thermal processes with bulk solids, eg. As for burning limestones and similar processes for calcination of bulk goods, to Roast and reducing ores as well as for heating, cooling and drying and so on be used.

Several embodiments The invention will be explained in more detail with reference to the drawing. Show it:

1 a hearth furnace reactor in section with a two-part space above the hotplate and a chain conveyor,

2 a hearth furnace reactor similar to 1 but with a trough auger as a conveyor,

3 a hearth furnace reactor similar to 1 but with a sweeping brush as a conveyor,

4 a hearth furnace reactor with mobile grid boxes and locks at the entrance and exit of the hearth furnace reactor,

5 two interconnected hearth furnace reactors in cascade form with different conveyors,

6 a stove top reactor without reaction space above the upper heating with a chain conveyor,

7 a hearth furnace reactor without reaction space above the upper heating with a trough screw,

8th a hearth furnace reactor without reaction space above the upper heater with scratching brush as a conveyor and

9 two connected hearth furnace reactors in cascade form, both hearth furnace reactors without reaction space.

As can be seen from the schematic representation of the figures, the hearth furnace reactor consists of a preferably cubic reactor space 1 in steel welded construction with appropriate insulation 2 , In the exemplary embodiment, the furnace length is about 14 m, the clear width about 2 m and the height about 2.5 m. The task of feedstocks takes place outside the hearth furnace reactor via a funnel-shaped crop function 3 from which a screw conveyor 5 , preferably in the form of a so-called Stopfchnecke, the material peels off and on the stove top 6 made of ceramic heating elements as under-heating 7 is formed, dumps. In the variant of 1 Material transport takes place over the entire length of the hob 6 by an externally driven chain conveyor 9 on the scraping elements 10 are attached. This conveyor throws the carbon (coke) not covered by the process of thermal decomposition into a good output, a shaft 11 , Another screw conveyor 5 transports the coke into an external reactor in which it is preferably also converted into process gas by gasification. The required process temperature of about 500 ° C generates the already named sub-heater 7 together with the upper heating 13 , which also consists of ceramic heating elements. In addition, laterally arranged heating elements can be arranged to intensify the heating process in the sense of a side heating (in FIG 1 not shown). The ceramic heating elements are either designed as burners which are operated with a partial flow of the self-generated gas or they act in the sense of acted upon by hot combustion gas heat exchangers. As a reaction agent to support the thermo-chemical reactions is in the field of feed task, the addition of water vapor via a steam inlet 8th intended. The avoidance of uncontrolled air oxygen access into the reactor space 1 serve corresponding blocking gas withdrawals 4 , which are designed as a fan. Between the upper heating 13 and the reactor ceiling is one with a support flame means 16 Equipped reaction space 15 formed, in which a substoichiometric combustion of the generated process gases is provided. Under the above-mentioned addition of water vapor soot formation is avoided and the conversion of condensable gaseous hydrocarbons in syngas at least partially run off. The removal of the gas takes place via the gas outlet 16 , supported by a blower 19 as a induced draft fan. This fan upstream is a combustion chamber 18 for the energetic use of the process gases. The resulting combustion gases reach after previous external heat extraction in the sense of energetic use a fireplace. The coarse separation of dusts are ceramic filter elements in passages 12 between the heating elements of the upper heating 13 ,

2 shows the same furnace furnace reactor as in 1 shown, but with an externally driven trough screw 20 as a conveying element. The stove 6 in the area of the underheater 7 is formed trough-shaped in this case. However, it is also conceivable that a trough or more troughs parallel next to each other on the stove top 6 stand.

The transport of the feedstocks by the hearth furnace reactor take over at the in 3 illustrated variant a variety of scratching brush 21 , one behind the other above the stove 6 are arranged, and are driven by an out-of-reactor mechanism. The individual scraping elements are all lowered at the same time, laterally displaceable, liftable, retractable and lowered guided and thus take over the transport of material over the entire cooking plate length.

4 shows an alternative of the hearth furnace reactor for the thermal composite material separation of components and workpieces in the composite material rubber / metal or plastic / metal in the sense of recovery of the metallic component. The material is stored in grid boxes 23 on externally driven steel rollers 22 proceed over the entire cooking plate length. The entry and exit of the lattice boxes 23 takes place in cyclic operation, with locks in the retraction and extension area 24 are arranged. The sealing of the locks serve special closure elements 25 ,

In 5 is shown a further variant in which two hearth furnace reactors are connected in series, for example, feedstocks, which consist of larger particles in the first, with a chain conveyor 9 thermally decomposed reactor in a first stage and the resulting reduced particle size material in the second, with a trough screw 20 thermally decomposed reactor in a second stage.

The 6 . 7 . 8th and 9 show variants where over the upper heating 13 no reaction space 15 and the substoichiometric combustion of the process gases in a combustion chamber arranged above the hearth furnace reactor 18 expires. The dust coarse separation is carried out by a coarse filter arranged centrally in the gas path 26 ,

The process for degassing and disposal of z. As tar residues with a humidity of 25%, using a hearth furnace reactor is characterized by a three-stage process. In the first stage, the estate is under heat by means of indirect heating (underheating 7 and upper heating 13 ) and under exclusion of air in the gas generation room 14 degassed at about 500 ° C to 600 ° C. This will be done on the stove top 6 the tar oil residues in a dumping height of about 5 cm to 10 cm through the scraping elements 10 towards good issue 11 transported. In the second stage, the primary generated gas in the reaction chamber 15 combusted stoichiometrically at about 850 ° C to 950 ° C by air supply, in such a way that the combustible components of the volatile (CH ₂ and CO) and the moisture are completely converted into CO and H ₂ . The amount of air required for this corresponds to an air ratio of λ = 0.25 to 0.30. Finally, in the third stage, this gas becomes CO ₂ and H ₂ O by supplying air at about 1000 ° C to 1200 ° C in the simplest case in an external combustion chamber 18 burned. The combustion gas then serves to heat the first stage. The excess of hot combustion gases can otherwise be used for energy.

Tar oil residues are characterized by a particularly low oxygen content. from that follows that a disposal of this substance in particular by possible Formations of soot and condensable constituents of the degassing gas is at risk. The process control of the invention first and second stage with the selected temperatures and the Staged air supply is suitable for such buildup to avoid.

There the process gas generation without the influence of atmospheric Air is ensured, a high calorific value of the gaseous hydrocarbons is secured. The Although gas conditioning using a support burner is required a small amount of combustion air, but the calorific value only negligible Dimensions reduced.

1

reactor chamber

2

insulation

3

material feed

4

Locking gas extraction

5

Auger

6

hotplate

7

underheater

8th

steam inlet

9

chain conveyors

10

scraping elements

11

Gutausgabe / shaft

12

passages

13

top heater

14

Gas generating space

15

reaction chamber

16

Supporting flame device

17

gas vent

18

combustion chamber

19

fan

20

trough auger

21

scratch broom

22

steel rollers

23

mesh boxes

24

smuggle

25

closure elements

26

coarse filter

Claims (32)

Portable or stationary hearth furnace reactor for converting solid and pasty, organic substances into process gas, characterized by the following features, preferably the cubic reactor space ( 1 ) with appropriate insulation ( 2 ) has on one side wall outside the reactor space ( 1 ) a funnel-shaped material task ( 3 ) with a blower for blocking gas withdrawal ( 4 ) and at the lower end of the material task ( 3 ) a screw conveyor ( 5 ) to an opening or through the opening in the wall of the reactor space ( 1 ) above a stove top ( 6 ) ends, with the stove plate ( 6 ) as the bottom of the reactor space ( 1 ) of a plurality of heating elements as sub-heating ( 7 ), - under the screw conveyor ( 5 ) but also above the stove plate ( 6 ) is a steam inlet ( 8th ), - above the hotplate ( 6 ) is over the entire length of the stove plate ( 6 ) a chain conveyor ( 9 ) arranged on the scraping elements ( 10 ) are fixed at certain intervals, - at the end of the chain conveyor ( 9 ) is a good issue, a shaft ( 11 ) for ash and / or residues in the bottom of the reactor space ( 1 ), which is also a blower for Sperrgasentnahme ( 4 ) and at the end of the shaft ( 11 ) another screw conveyor ( 5 ), - above the chain conveyor ( 9 ) is a ceiling with passages ( 12 ) as upper heating ( 13 ) arranged the reactor space ( 1 ) into an underlying gas generating room ( 14 ) and in an overlying gas collecting space or reaction space ( 15 ) separates, - on one side of the reactor space wall in the reaction space ( 15 ) is a support flame device ( 16 ) and in the ceiling of the reactor space ( 1 ) or in the upper side wall area a gas outlet ( 17 ) intended. Oven furnace reactor according to claim 1, characterized in that instead of the chain conveyor ( 9 ) with the scraping elements ( 10 ) a trough slug ( 20 ) is arranged with a trough or more trough screws ( 20 ) with troughs side by side on the stove top ( 6 ) or the stovetop ( 6 ) has a trough shape. Oven furnace reactor according to claim 1, characterized in that instead of the chain conveyor ( 9 ) a plurality of consecutive scratch brooms ( 21 ), wherein the individual scratch brooms ( 21 ) all at the same time lowerable, laterally displaceable, liftable and are designed to be reversible, Oven furnace reactor according to claim 1, characterized in that instead of the chain conveyor ( 9 ) above the cooking plate from outside the reactor space ( 1 ) driven rollers ( 22 ) are arranged on which grid boxes ( 23 ) take over the material transport over the entire stove plate length, with at the beginning and at the end locks ( 24 ) are provided whose sealing special closure elements ( 25 ) take. Oven furnace reactor according to claim 4, characterized in that the grid boxes ( 23 ) are successively on slide rails and are displaceable by a pusher through the hearth furnace reactor. Oven furnace reactor according to claim 1 and 3, characterized in that the air gap between the cooking plate ( 6 ) and the scraping elements ( 10 ) or the scratch broom ( 21 ) towards good issue ( 11 ) of the hearth furnace reactor. Oven furnace reactor according to one of the preceding claims, characterized in that above the closed upper heating ( 13 ) without passages ( 12 ) no reaction space ( 15 ) consists. Oven furnace reactor according to claim 7, characterized in that in the gas outlet ( 17 ) between the hearth furnace reactor and the outer combustion chamber ( 18 ) a ceramic coarse filter ( 26 ) is arranged for dust separation. Oven furnace reactor according to one of the preceding claims, characterized in that after the gas outlet ( 17 ) a combustion chamber ( 18 ) and a blower ( 19 ), which have a fireplace ( 27 ) can be connected downstream. Oven furnace reactor according to one of the preceding claims, characterized in that in the passages ( 9 ) of the ceiling in the reactor space ( 1 ) Coarse filters are arranged in the form of ceramic filters. Oven furnace reactor according to one of the preceding claims, characterized in that hot exhaust gases are used as heating means. Oven furnace reactor according to one of the preceding claims, characterized in that the underheater ( 7 ) and upper heating ( 13 ) consists of individual ceramic channels and their respective temperature is adjustable. Oven furnace reactor according to one of the preceding claims, characterized characterized in that in the reactor walls in addition heating elements as side heating are integrated. Oven furnace reactor according to one of the preceding claims, characterized characterized in that the reactor walls of a sheet metal construction with intermediate stiffening profiles and heat insulation material, wherein at appropriate locations maintenance openings and additional openings for measuring and control devices are provided. Oven furnace reactor according to one of the preceding claims, characterized characterized in that in the transportable execution of the entire hearth scratch reactor resting on a transport frame. Oven furnace reactor according to one of the preceding claims, characterized in that all drives for the screw conveyors ( 5 ), the trough slug ( 20 ), the chain conveyor ( 9 ) and the Pacemaker system of scratch brooms outside of the reactor space ( 1 ) lie. Oven furnace reactor according to one of the preceding claims, characterized characterized in that at least two or more hearth furnace reactors than Cascade or tower are arranged, with the good output of the upstream Furnace furnace reactor at the same time the Gutaufgabe the downstream hearth furnace reactor is and this Gutaufgabe or output is designed to be heated. Oven furnace reactor according to claim 17, characterized in that in that a roller mill is arranged between the first and the second hearth furnace reactor is. Process for the conversion of solid and pasty, organic substances into process gases, including a hearth furnace reactor, characterized in that, within a hearth furnace reactor, during the continuous passage of the substances to be treated through the hearth furnace reactor with the aid of mechanically driven transport devices, such as scraper elements ( 10 ), Scratch broom ( 21 ) or trough slug ( 20 ) proceed in the following stages - in the first stage, the degassing takes place under exclusion of air at least 280 ° C to a maximum of 600 ° C, preferably at about 500 ° C by an indirect sub-heating ( 7 ) of the stove plate ( 6 ) and by an upper heating ( 13 ) in the gas generation room ( 14 ), wherein the substances to be treated at a bed height of about 5 cm to 10 cm by means of transport devices on the stove in the direction Gutausgabe / Schacht ( 11 ), in the second stage the gas which has formed primarily is substoichiometrically at approximately 850 ° C. to 950 ° C. in the gas collecting space or reaction space by air supply ( 15 ), whereby the combustible constituents of the volatiles (CH ₂ and CO) as well as the moisture are completely converted to CO and H ₂ , - in the third stage the resulting second stage gases are produced by supplying air in a subsequent room at about 1000 ° C burned to 1200 ° C to CO ₂ and H ₂ O. A method according to claim 19, characterized in that the resulting by thermal decomposition process gases after the stoichiometric combustion in the reactor chamber ( 1 ) in an additional external combustion chamber ( 18 ) are burned to the energetic use. Method according to claims 19 and 20, characterized that the process gases produced by thermal decomposition in an external plant to synthesis gas, which is used as a fuel or fuel in gas engines or fuel cells comes. Method according to claims 19 to 21, characterized that after the thermal decomposition of hydrocarbon fractions of the feed remaining carbon residues in an external, downstream apparatus by the gasification reaction also in Process gas to be implemented. Method according to claims 19 to 22, characterized that after the thermal decomposition of hydrocarbon fractions of the feed remaining carbon residues in an external, downstream apparatus means are used by combustion energetically. Process according to claim 19 to 23, characterized in that in the reaction space ( 15 ) in the substoichiometric and in the afterburning support flame facilities ( 16 ) operate. Process according to claims 19 to 24, characterized in that in the gas generation room ( 14 ) and in the reaction space ( 15 ) of the hearth furnace reactor for the stoichiometric combustion water vapor is entered as a reaction partner for thermo-chemical reactions. A method according to claim 19 to 25, characterized in that in order to avoid the entry of air in the area of the crop ( 3 ) and the Gutausgabe ( 11 ) Sealing gas by a barrier gas withdrawal ( 4 ) is deducted. Method according to claim 19 to 26, characterized in that the combustion of the third stage in an external combustion chamber ( 18 ), or that in the case of conversion of the generated process gas into synthesis gas, a partial flow of the same is used as fuel gas for heating. Method according to one of claims 19 and 27, characterized that's hot Third stage combustion gases for first stage heating be used. Method according to one of claims 19 to 28, characterized that in the process according to claim 19 to 21 resulting residues in a treated further furnace furnace reactor. Method according to one of claims 19 to 29, characterized in that two hearth furnace reactors are connected in series according to claim 17, for example, feedstocks, which consist of larger particles in the first, with a chain conveyor ( 9 ) equipped stove furnace in egg thermal decomposition in the first stage and the material resulting therefrom with reduced particle size in the second, with a trough screw ( 20 ) Herdofen reactor in a second stage thermally further decomposed. Method according to one of claims 19 to 30, characterized in that a fan arranged outside the hearth furnace reactor ( 19 ) a negative pressure within the reactor space ( 1 ) and withdraw the resulting process gas for delivery to external facilities for direct thermal utilization or conversion to synthesis gas. Process for the thermal composite material separation of components and workpieces in the composite material rubber / metal or plastic / metal for the recovery of the metallic components including a hearth furnace reactor according to claim 4 and / or 5, characterized in that the entry and exit of the grid boxes ( 23 ) into and out of the reactor space ( 1 ) takes place in clock mode.