WO2011101020A1

WO2011101020A1 - Method and device for obtaining combustible fuels and gases from organic materials

Info

Publication number: WO2011101020A1
Application number: PCT/EP2010/051938
Authority: WO
Inventors: Gernot K. Brueck
Original assignee: Gim Holding Bv
Priority date: 2010-02-16
Filing date: 2010-02-16
Publication date: 2011-08-25
Also published as: EP2536495B1; PT2536495T; ES2734519T3; DK2536495T3; EP2536495A1

Abstract

The invention relates to a method for obtaining combustible fuels and gases from organic materials (1), wherein the organic materials (1) are thermally decomposed and thereby the combustible fuels and gases are formed and carbon is formed. The carbon produced in the thermal decomposition is reacted in a steam atmosphere to form carbon monoxide and hydrogen in a synthesis process following the decomposition. The invention further relates to a corresponding hybrid device, comprising a decomposition reactor (5) and to a synthesis reactor (10).

Description

"Process and apparatus for the recovery of combustible fuels and gases from organic matter"

The invention relates to a process for the recovery of combustible fuels and gases from organic matter, wherein the organic substances are thermally decomposed to form the combustible fuels and gases and to form carbon.

Furthermore, the invention relates to an apparatus for carrying out such a method, with a reactor for the thermal decomposition of organic substances to form combustible fuels and gases and to form carbon.

Processes and apparatuses for extracting combustible fuels and gases from organic matter are well known, for example, as systems for the conversion of biomaterials into biogas which have been in operation for some years, but at the same time they are also the enormous problems that surround the entire industry.

On the one hand, the cost of such processes in the form of the prices for plants containing fat, carbohydrates and proteins is constantly increasing, so that from this alone the urgency of increasing the process efficiency is derived. On the other hand, there is still a share of about 25 to 35% of non-fermentable organic substances completely unused. In addition, the disposal of, for example, plastic waste is often associated either with high technological effort, or it is unfortunately in this sector also largely wasted valuable and usable energy by simply burning useless.

A certain proportion of organic materials is also thermally decomposed, especially in pyrolysis plants, with the formation of combustible fuels and gases and the formation of carbon, but here too the efficiency left much to be desired and this also always requires not inconsiderable investments. The quality of the gases produced in this way is often very inconsistent - on the one hand due to the diversity of the thermally decomposable organic materials, and, on the other hand, depending on the nature of the respectively selected settings in the process control. The method known to be mixed usually with inorganic material such. As with metals or salts, resulting carbon must be disposed of as unusable ashes.

The invention has for its object to provide a method and a device of the type mentioned in a technologically less expensive way, with which the degree of utilization of the organic substances used in the production of combustible fuels and gases can be increased.

According to the process of the invention, this is achieved by reacting the carbon generated in the thermal decomposition in a decomposition downstream synthesis process in steam atmosphere to carbon monoxide and hydrogen.

In the apparatus according to the invention this is achieved in that the reactor for thermal decomposition technologically a synthesis reactor for the formation of carbon monoxide and hydrogen from water vapor and from the reactor in the followed by thermal decomposition of carbon formed, the

Reactors are connected to each other via a feed for the carbon from the thermal decomposition reactor in the synthesis reactor.

With such a hybrid system can be carried out advantageously up to 100% conversion of the organic substances to be decomposed, which also advantageously the production of the hydrogen-containing gas produced in the synthesis reactor can be separated from the generation of the resulting gases in the thermal decomposition step. Although in the thermal decomposition with advantageously high technological flexibility optionally different materials can be used and decomposed with different temperature regimes adapted in each case to their chemical composition, the synthesis unit remains unaffected and always operates identically.

Thus, the thermal decomposition of organic substances can be carried out as so-called flash pyrolysis in a temperature range of 300 ° C to 600 ° C, based on 00% dry matter of organic substances about 75% to 85% combustible fuels and gases and about 15% to 25% carbon arise. Important for full utilization of the energy of the organic substances used according to the invention is the conversion of the carbon. If you take z. As wood as decomposing organic substance or as an energy supplier, which has a calorific value of about 18 MJ / kg of dry matter, then make 20% residual carbon with a calorific value of about 34 MJ / kg at least about 38% of the wood immanent energy which can be used more according to the invention in comparison with a process without a synthesis step.

Another possibility - if a high hydrogen yield is desired - is to carry out the thermal decomposition of the organic substances as so-called monocarbon thermolysis in a temperature range of 650 ° C to 800 ° C, based on 100% dry matter of organic substances more than 20 % Carbon - together with CO, H ₂ , CH ₄ - is formed, which is then available for the synthesis reaction, the composition depending on the nature of the input material and its moisture.

It should be noted that the amount of carbon formed during thermal decomposition depends on the temperature; the higher this is, the more carbon is liberated because, as will be shown in detail below, it is formed at the thermolytic interfaces of the polymeric organic molecules. The short-chain due to a higher selected temperature, the cuts are, the more elemental carbon can arise.

It is also possible without procedural disadvantages that the thermally decomposable organic substances contain components from which arise in the thermal decomposition of inorganic ash products. Also during the thermal decomposition of the organic substances the process especially in water dissolved functional additives, such as salts and salt formers, such as phosphoric acid or potassium hydroxide, are supplied - so to order z. B. nitrous gases to bind as ammonium phosphates or sulfur oxides as potassium sulfate.

The invention is based on the finding that a combination of thermal decomposition and synthesis in a single reactor space leads to problems. For example, while a thermolysis takes place, around the decomposing particles of the organic matter around expanding gas clouds that would effectively force away the water vapor required for a conversion to hydrogen and carbon monoxide from the reaction site, so that no

Water molecule reaches the carbon. In addition, remains at a thermolysis - as known from the production of activated carbon - always a stable carbon skeleton in the resulting carbon, so that here the surface, although theoretically large, but the water molecules is accessible only to a limited extent, so that no complete implementation can take place. An important step towards full utilization of the energy contained in the organic matter to be decomposed is also the breakdown of the hybrid device in the stage of decomposition with the above middle or above, but compared to the temperature of the synthesis stage, which - Coal and also because of the possibly existing presence of chemically inactive inorganic substances - is performed as Hochternperaturprozess in the temperature range of 850 ° C to 1000 ° C, comparatively lower temperature range.

The CO / H ₂ production can be followed by a water gas shift reaction in another reactor, which at temperatures between 250 ° C and 450 ° C on an iron (III) oxide catalyst, the carbon monoxide in an exothermic Zess is converted in a steam atmosphere to carbon dioxide, wherein the amount of hydrogen approximately doubles.

The method according to the invention with the decomposition and the synthesis process, although anaerobic and in each case as an endothermic reaction - that is not autothermic - led to be realized in the overall balance with high energy efficiency, since on the one hand the energy required for decomposition and synthesis at least more than 80% , preferably more than 95%, by combustion of the combustible fuels and gases obtained from the organic substances and / or by recuperation of the heat generated in the water gas shift process can be provided, only for a first or a possibly After shutdown times repeated commissioning of the device according to the invention is a one-time energy input, for example, with externally supplied combusting fuel gas necessary. In the stationary state, the heat can be provided 100% process-immanent. In addition, the carbon from the stage of decomposition of the organic substances preferably passes directly into the synthesis reactor, ie without cooling and intermediate storage, ie already at the reaction temperature prevailing in the decomposition stage, so that in the synthesis stage only nor the difference amount of energy to reach the relevant temperature is spent.

In the reactors of the device according to the invention, in particular in the reactor for thermal decomposition, it may preferably be carried out by means of screw conveyors. In this case, spatula and / or roller units integrated into the screws can very finely distribute the organic material over the bottom of the oven, so that all particles can be brought directly to an optimum flash temperature, for example about 475 ° C., via contact heat from the reactor wall. Scraper units mounted behind can then free the floor or reactor wall wall of buildup and make it free for subsequent direct contact with the organics. In addition, with a roller system on the screw, the resulting carbon formates can be broken up at the same time so that only pulverized coal, generally mixed with inorganic material, is supplied to the point of discharge from the reactor.

Further advantageous design features and advantages of the invention are contained in the following description and in the subclaims.

Reference to a preferred, illustrated in the accompanying drawings embodiment of the method and two preferred structural variants for a reactor of the device according to the invention, the invention is explained in detail. Showing:

Fig. 1 is a technological diagram of a preferred embodiment of a

device according to the invention for illustrating the method according to the invention, a schematic representation of the interaction of water vapor with particles of a thermally decomposing in the same reaction space organic matter, a representation of the thermal decomposition of an unbranched alkane chain molecule at a relatively higher temperature, a representation of the thermal decomposition of an unbranched alkane chain molecule at a relatively lower temperature, a cross-sectional view of a first preferred embodiment of a reactor which can be used according to the invention in the thermal decomposition of organic substances,

6 to 8 enlarged details of the illustration in FIG. 5 at different working positions of a screw conveyor in the thermal decomposition reactor, FIG.

9 shows a cross-sectional illustration of a further preferred embodiment of a reactor which can be used according to the invention in the thermal decomposition of organic substances,

10 is an enlarged detail view of an assembly of the in Fig. 9

illustrated reactor for thermal decomposition.

According to a method according to the invention, in an installation according to the invention for the production of combustible fuels and gases, an organic moisture-containing substance 1 or else a mixture of substances is set in a heated funnel 2 to a desired content of dry matter. Plant substances such as wood or compost, biomass, household waste, plastic waste, sewage sludge, meat waste, old car tires and the like can be used more as organic substances 1. The organic substances used to form the combustible fuels and gases may contain 5% to 50%, preferably 15% to 20%, moisture, which is preferably adjusted by the drying preceding the thermal decomposition. The thermally decomposable organic substances 1 can also contain constituents from which arise during thermal decomposition inorganic ash products.

It is not shown in FIG. 1 that the organic substance 1 used to form the combustible fuels and gases or the organic substances 1 is comminuted before decomposition and drying, in particular comminuted to mean particle sizes in the range from 2 mm to 5 mm should (n), preferably a dimension in a spatial dimension of the particles (length, width, height) should be smaller than 100 μιη. As a result, the particles have an optimum surface-to-volume ratio for the decomposition reaction and, for the purpose of heat transfer, the thermal attack.

From the funnel 2, the organic substance 1 falls into a sluice 3, which is shown as an example in the drawing as a rotary valve, and passes through the opening 4 in the interior of the reactor 5 for decomposition. The lock 3 closes the reactor also airtight from the material supply point down. In the reactor 5, the thermal decomposition of the organic substance 1 is performed as an anaerobic process, wherein the organic material 1 can also be introduced into the reactor 5, in particular under protective gas. Within the reactor 5 for the decomposition, an axially extending screw conveyor 6 moves the material continuously up to the discharge opening 8, which in turn opens into a gas-tight lock 9, in particular a rotary valve. The decomposition reactor 5 also has a feed 7, via which water, optionally with functional additives dissolved therein, can be supplied.

The screw conveyor 6 always has transverse bars, which extend longitudinally to the housing of the decomposition reactor 5. For this purpose, initially simple scratch and Wenderiegel - like the designated in Fig. 5 by the reference numeral 62 bars - but also may be added with additional functions bolt, as well as the below-described Fig. 5 to 10 can be seen.

At arbitrarily adjustable temperatures, for example in the temperature range between 300 ° C and 600 ° C, the organic material in the reactor 5 is then thermally decomposed, in particular subjected to a thermolysis. The described configuration of the screw conveyor 6 allows not only Hochtemperaturthermolysen and the implementation of the aforementioned flash pyrolysis. In such a quasi-flash pyrolysis, the organic material 1 is heated very rapidly in an intermediate-temperature process, preferably at about 475 ° C., with the exclusion of oxygen. In particular, small particles are decomposed at very high heating and heat transfer rates, whereby usually about 60% to 70% (then at room temperature) liquid products are produced as combustible fuels, and additionally each still about 10% to 20% combustible gas and about 15% to 25% residual carbon, based on 100% dry substance of the organics (organic substance 1). The carbon mixes with any inorganic material which may be present or formed, such as e.g. As metals or salts.

The thermal decomposition of the organic substances 1 can also be carried out as so-called monocarbon thermolysis in a temperature range of 650 ° C to 800 ° C, based on 100% dry matter of the organic substances 1 only CO, H2, CH4 and carbon arise. The resulting gas is decoupled from the gas outlet 1 and passes into a gas cooler 12 in which it is cooled down in a cooling coil 13, for example, to a temperature of 50 ° C. suitable for later use of the gas for power generation. Liquid fractions condense and are collected in the container 14. From this, the liquid fuels and residual water can be withdrawn via an outlet 15.

The gas then flows into a gas scrubbing 6. In this gas scrubbing 16 of the gases formed by the thermal decomposition, oils, in particular vegetable oils, preferably rapeseed oil, can be used as scrubbing liquids. Rapeseed oil has a particularly good ability to bind tars. The scrubbing liquid laden with solids, in particular with carbon, is sucked off via an outlet 19 and can be supplied as input material to the process of thermal decomposition of the organic substances 1. This can happen, in particular, if so much pulverized coal has formed in the reactor that the viscosity has increased so much that the gas can only pass through the washing liquid to a limited extent.

The purified gas is sucked by means of a pump 17 and pressed into a gas supply system 18, wherein gas sensors and flow meters are located.

The mixture of pure carbon and inorganic material passes through the aforementioned gas-tight lock 9 directly into a synthesis reactor 10. The fact that the reactors 5, 10 are arranged one above the other, the carbon can also under the action of its own weight from the reactor 5 for thermal Decomposition in the synthesis reactor 10 flow. The delivery energy is kept low.

In the synthesis reactor 10, the carbon produced in the decomposition is removed in a synthesis process which is connected downstream of the decomposition in space and time. steam atmosphere at temperatures ranging from 850 ° C to 1000 ° C converted to carbon monoxide and hydrogen. The water vapor necessary for the synthesis is sprayed via a feed line 20.

With a conveyor screw 21 arranged in the interior of the synthesis reactor 10, the carbon is continuously conveyed, swirled in the chamber and fed to an outlet 22 in the inorganic material remaining in the synthesis reaction. Here this is then passed as ash or residual waste via a further rotary valve 23 in an ash pan 24.

The resulting CO / H ₂ gas mixture is decoupled at the gas outlet 25 and then tempered down in a cooler 26. Any existing residual water from unreacted water vapor is separated and removed via a water outlet 27.

From the cooler 26, the gas flows into a gas scrubber 28 and is freed from residual dust there. A sump 29 of the scrubber 28 is then sucked in an overload with dust on the Sumpfabsaugung 30, wherein the liquid can also be fed back to the reactor 5 for thermal decomposition.

From the gas scrubber 28, the gas mixture is sucked off via a pump 31, controlled in the gas stream by means of sensors 32 and then into a

Gas line 33 pressed.

Optionally, this then - regardless of the gas composition, which has the emerging from the decomposition reactor 5 gas - advantageously always identical gas mixture via a shift reactor 34 for the water gas are further treated by in the shift reactor 34 with supply of water vapor

Iron (III) oxide catalysts 35 at temperatures in the range of 250 ° C to 450 ° C, the carbon monoxide is converted into carbon dioxide, wherein additionally hydrogen arises: Complete conversion of CO into CO ₂ doubles the production of hydrogen.

The carbon dioxide contained in the gas mixture can in a further optional refrigeration unit 38, which z. B. is filled with liquid nitrogen as a coolant, are liquefied by passing it through a cooling coil 39 and thereby cooled to below - 60 ° C. The liquid CO2 then flows at a pressure of more than 6 bar into the collecting vessel 41 and can be removed from there via the outlet 42. The pure hydrogen gas is then available in the gas line 40.

FIG. 2 shows how water vapor 45 is prevented from a thermally decomposing organic particle 43, since permanent decomposition gas 44 flows out of the particle 43. The figure thus illustrates that, as already stated above, it is technologically unfavorable to carry out thermal decomposition and synthesis in a single reactor because complete conversion of the organic substances 1 can not take place. Instead, with the hybrid system according to the invention, organic material can advantageously be converted 100% into combustible fuels and gases.

FIGS. 3 and 4 show a model of an alkane, as it is conceivable to produce the pure carbon from an organic substance 1. As first shown in FIG. 3, the thermal energy 46 attacks a C-C bond 47 and separates the hydrocarbon chain 48. This gives rise to free H-C-H radicals 50 and longer radical portions 49 which snatch hydrogen from the H-C-H radicals 50 and thus complete themselves into molecules. By way of example, in this regard, ethane is designated by reference numeral 51 in FIG. 3. In the process, the pure carbon 52 freed from hydrogen is formed as a residuum.

According to FIG. 4, the heat attack (heat energy 53) on the molecular chain 54 is lower because the process of thermal decomposition is comparatively lower Temperature is performed. In this case, on the one hand less, but longer molecule sections 55 and longer molecules - exemplarily in this regard in FIG. 4 propane is denoted by reference numeral 56 - as well as a smaller number of HCH radicals and thus less pure carbon 58 arise.

By Fig. 5 to 10 some structural details of the device according to the invention are illustrated, which is also attributed independent inventive significance and take into account the fact that the thermal decomposition of the organic substances and the synthesis process run as endothermic processes, the energy required allotropic fed to the process, d. H. that it is coupled in particular indirectly via walls of the reactors 5, 10 or alternatively or additionally also via a heat transfer medium guided through, for example, heating coils in each case through the reaction space.

The reactors 5, 10 of the device according to the invention may preferably be tube furnaces in which conveyor screws 6, 21 are arranged. Alternatively, as reactors 5, 10 but also rotary kilns can be used, wherein during the thermal decomposition and the synthesis process, the organic matter 1 and the carbon are continuously conveyed by kiln rotation.

In particular, an improvement in terms of intensifying the reaction of thermal decomposition by changing the inside of the decomposition reactor 5 (denoted by the reference numeral 62 in Fig. 5) may be brought about (indicated by reference numeral 60 in Fig. 5). As already mentioned, this screw conveyor 60 initially has scraping and turning bars 62. These are at least partially longitudinally to a housing of the reactor 5 extending, in particular approximately in cross-section approximately trapezoidal, transverse bar, which are shaped and arranged so that they the organic matter 1, the inorganic substances and / or the carbon in a Turn over movement through the reactor 5, if appropriate, also vortex and / or scrape off from a wall 59 of the reactor 5.

For the mentioned improvement - as shown in FIGS. 5 to 8 - on the screw 60 additionally Aufpressriegel 61 are attached, which are also designated by the reference numerals 64, 66 and 69 in their various possible working positions in Fig. 6 to 8. It is preferred, as the drawing illustrates, to longitudinally to a housing of the reactor 5 extending, in particular wing-like, in cross-section approximately crescent-shaped, obliquely to radial rays R through the reactor 5 arranged longitudinal bars which are shaped and arranged such that they distribute the organic substances 1, the inorganic substances and / or the carbon in a movement through the reactor 5 in a few millimeters thick layer on the wall of the reactor 5 and press against the wall 59 of the reactor 5.

In detail, this shows the sequence of figures 6 to 8, that the material (in Fig. 6 by reference numeral 65 and in Fig. 7 denoted by 68) of the organic material 1, which lies on a lower inner wall 63 of the reactor 5, from Aufpressriegel 64th taken and brought in the rotational movement of the screw conveyor 60 as a thin layer 67 in direct contact with the hot housing surface 63. When the pressure bar then reaches the position 69 (FIG. 8), the entire material 71 is pressed in a thin layer onto the hot surface 70 and evaporates or decomposes in direct contact with the wall very spontaneously and in a few seconds.

As further shown in FIGS. 9 and 10, it is also possible for pressure rollers 75 to be attached to the worm (here denoted by reference numeral 73) in addition to scraping and turning seals (designated here by reference numeral 74). These are preferably longitudinal bars extending longitudinally of the housing of the reactor 5, which are designed as rollers which are freely movable in the radial direction and are fastened to the conveyor screw 73 in such a manner that they guide the organic components. see inorganic substances and / or press the carbon in a few millimeters thick layer to the wall 72 of the reactor 5 and crushed by a roll on the wall of the reactor 5 crushed. Such pressure rollers 75 can react more easily to strongly cohesively shaped fittings of inorganic material and thus also avoid jamming. Furthermore, these rollers 75 roll the resulting carbon small. To fulfill their function, the rollers (denoted by reference numeral 77 in FIG. 10) should have inherent severity and be mounted on the worm in a guide bar 76 such that the axle 78 of the roller is free in a recess (slot 79). of the guide bar 76 can move.

As already apparent from the foregoing, the present invention is not limited to the illustrated embodiment, but includes all means and measures in the sense of the invention equally effective. Furthermore, the invention is not limited to the feature combinations defined in the independent claims but may be defined by any other combination of particular features of all the individual features disclosed overall. This means that in principle virtually every individual feature of the independent claims can be omitted or replaced by at least one individual feature disclosed elsewhere in the application. In this respect, the claims are to be understood merely as a first formulation attempt for an invention.

Claims

claims:

Anspruch [en] A process for obtaining combustible fuels and gases from organic matter (1), wherein the organic matter (1) is thermally decomposed to form the combustible fuels and gases and to form carbon,

characterized in that the carbon generated in the thermal decomposition is converted in a decomposition downstream synthesis process in steam atmosphere to carbon monoxide and hydrogen.

2. The method according to claim 1,

characterized in that the thermal decomposition and the synthesis process in two separate technologically connected in series reactors (5, 10), a decomposition reactor (5) for thermal decomposition of the organic matter (1) and a synthesis reactor (10) for the formation of the carbon monoxide and of hydrogen takes place, wherein as reactors (5, 10) in particular gas-tight separate furnace sections or furnaces, preferably tube furnaces are used.

3. The method according to claim 1 or 2,

characterized in that during the thermal decomposition and the synthesis process, the organic substances (1) and the carbon, in particular by means of screw conveyors (6, 21, 60, 73) and / or by furnace rotation, are conveyed continuously.

4. The method according to any one of claims 1 to 3,

characterized in that as organic substances (1) for the formation of combustible fuels and gases plant residues, such as wood or compost, biomass, household waste, plastic waste, sewage sludge, meat waste, used tires and the like are used.

5. The method according to any one of claims 1 to 4,

characterized in that the organic substances (1) used to form the combustible fuels and gases contain 5% to 50%, preferably 15% to 20%, moisture, which is preferably adjusted by a drying preceding the thermal decomposition.

6. The method according to any one of claims 1 to 5,

characterized in that the organic substances (1) used for the formation of the combustible fuels and gases are comminuted prior to decomposition to particles, in particular with an average particle size in the range of 2 mm to 5 mm, wherein preferably a dimension of the particles in a spatial Dimension of the particles is less than 100 μηη.

7. The method according to any one of claims 1 to 6,

characterized in that the thermally decomposable organic substances (1) contain components from which arise during thermal decomposition inorganic ash products.

8. The method according to any one of claims 1 to 7,

characterized in that during the thermal decomposition of the organic substances (1) the process in particular dissolved in water functional additives, such as salts and salt formers, for example phosphoric acid or potassium hydroxide, are supplied.

9. The method according to any one of claims 1 to 8,

characterized in that the carbon generated in the thermal decomposition, in particular together with incurred in the thermal decomposition of inorganic ash products directly - without cooling and intermediate storage - via a lock (9) is supplied to the synthesis process.

10. The method according to any one of claims 1 to 9,

characterized in that in the synthesis process, the entire carbon generated in the thermal decomposition is reacted, wherein in particular incurred only in the decomposition of inorganic ash products are discharged as residual waste.

11. The method according to any one of claims 1 to 10,

characterized in that the resulting by the thermal decomposition combustible fuels and gases and the resulting in the synthesis process carbon monoxide-hydrogen gas mixture treated separately, in particular in each case condensed and / or a gas scrubbing (16, 28) subjected.

12. The method according to any one of claims 1 to 11,

characterized in that in a gas scrubbing (16) of the resulting by the thermal decomposition of the gases as scrubbing oils, in particular vegetable oils, preferably rapeseed oil, are used.

13. The method according to any one of claims 1 to 12,

characterized in that after a gas scrubbing (16) of the resulting by the thermal decomposition gases and / or the carbon monoxide-hydrogen mixture with a solid, in particular with carbon, loaded scrubbing liquid as input material to the process of

thermal decomposition of the organic substances (1), in particular for

Increase of their fluidity, is supplied.

14. The method according to any one of claims 1 to 13,

characterized in that the resulting in the synthesis process carbon monoxide is catalytically reacted in a water gas shift process in a temperature range of 250 ° C to 450 ° C with further water vapor to carbon dioxide and further water vapor.

15. The method according to claim 14,

characterized in that the resulting in the water gas shift process carbon dioxide, in particular by cooling to below - 60 ° C, is separated from the hydrogen.

16. The method according to any one of claims 1 to 15,

characterized in that the thermal decomposition of the organic substances (1) is performed as an anaerobic process, in which the organic substances (1) are introduced in particular under protective gas.

17. The method according to any one of claims 1 to 16,

characterized in that the thermal decomposition of the organic substances (1) takes place as flash pyrolysis in a temperature range of 300 ° C to 600 ° C, in particular at about 475 ° C, based on 100% dry matter of the organic substances about 75% to 85% combustible fuels and gases and about 15% to 25% carbon arise.

18. The method according to any one of claims 1 to 16,

characterized in that the thermal decomposition of the organic substances (1) takes place as monocarbon thermolysis in a temperature range from 650 ° C to 800 ° C, based on 100% dry matter of the organic substances predominantly CO, H ₂ , CH ₄ and carbon is formed ,

19. The method according to any one of claims 1 to 18,

characterized in that the synthesis process in the temperature range of 850 ° C to 1000 ° C is performed.

20. The method according to any one of claims 1 to 18,

characterized in that the thermal decomposition of the organic substances (1) and the synthesis process run as endothermic processes, wherein the energy required for allothermic process is supplied, in particular indirectly via walls of the reactors (5, 10) and / or via a Heat transfer is coupled.

21. The method according to any one of claims 1 to 20,

characterized in that the thermal decomposition of the organic substances (1) and the synthesis process run as endothermic processes, wherein the energy required for this purpose at least more than 80%, preferably more than 95%, by combustion of the organic substances (1) combustible fuels and gases and / or provided by heat generated in a water gas shift process.

22. A device for carrying out a method according to one of claims 1 to 21, with a reactor (5)) for the thermal decomposition of organic substances (1) to form combustible fuels and gases and to form carbon,

characterized in that the reactor (5) for thermal decomposition is technologically followed by a synthesis reactor (10) for forming carbon monoxide and hydrogen from water vapor and carbon formed in the reactor (5) for thermal decomposition, the reactors (5, 10) via a feed for the carbon from the reactor (5) for thermal decomposition in the synthesis reactor (10) are interconnected.

23. Device according to claim 22,

characterized in that the feed for the carbon is a gas-tight lock (9), such as a rotary valve.

24. Device according to claim 22 or 23,

characterized in that the reactors (5, 10) are arranged one above the other so that the carbon under the action of its own weight from the reactor (5) for thermal decomposition in the synthesis reactor (10) can flow.

25. Device according to one of claims 22 to 24,

characterized in that the reactors (5, 10) are tube furnaces, such as rotary kilns.

26. Device according to one of claims 22 to 25,

characterized in that at least one reactor (5, 10) at least one axially extending screw conveyor (6, 21, 60, 73) is arranged, on the one hand, the organic substances (1) inorganic substances and / or the carbon through the reactor ( 5, 10) and on the other hand from the walls (59) of the reactor (5, 10) scraped and circulated.

27. The device according to claim 26,

characterized in that the at least one screw conveyor (6, 21, 60, 73), preferably in the reactor (5) for thermal decomposition, at least partially along a housing of the reactor (5) extending, in particular approximately in cross-section approximately trapezoidal, cross bar (62) shaped and arranged to swirl the organic matter (1), the inorganic matter and / or the carbon when moving through the reactor (5), and / or from a wall (59) scrape off the reactor (5).

28. Device according to claim 26 or 27,

characterized in that the at least one screw conveyor (6, 21, 60, 73), preferably in the reactor (5) for thermal decomposition, extending obliquely along a housing of the reactor (5), in particular wing-like, approximately crescent-shaped in cross-section Longitudinal bars (61, 64, 66, 69) arranged in radial direction through the reactor, which are shaped and arranged such that they move the organic substances (1), the inorganic substances and / or the carbon when moving through the reactor (5 ) in a few millimeters thick layer (67) on the wall of the reactor and press against the wall (59, 63) of the reactor (5).

29. Device according to one of claims 26 to 28,

characterized in that the at least one screw conveyor (6, 21, 60, 73), preferably in the reactor (5) for thermal decomposition, has longitudinal bars extending longitudinally relative to a housing of the reactor (5) which are freely movable in the radial direction Formed on the screw conveyor (6, 21, 60, 73) and are designed such that they the organic matter (1), the inorganic substances and / or the carbon in a few millimeters thick layer to the wall ( 72) of the reactor (5) press and comminute by a Zerwalzen on the wall (72) of the reactor (5).

30. Device according to one of claims 22 to 29,

characterized in that the reactors (5, 10) have feeds (7, 20) for water vapor and / or water, optionally with functional additives dissolved therein.