EP3580312A1

EP3580312A1 - Producing synthesis gas from carbon-rich substances by means of a combined co-current/counter-current method

Info

Publication number: EP3580312A1
Application number: EP18704520.8A
Authority: EP
Inventors: Leonhard Baumann; Roland Möller
Original assignee: Ecoloop GmbH
Current assignee: Ecoloop GmbH
Priority date: 2017-02-13
Filing date: 2018-02-08
Publication date: 2019-12-18
Anticipated expiration: 2038-02-08
Also published as: WO2018146179A1; DE102017102789A1; EP3580312B1

Abstract

The invention relates to a method for producing synthesis gas (130) from carbon-rich substances (112) in a vertical shaft with a bulk material moving bed (110), wherein a pyrolysis zone (141) and a reduction zone (142) are formed from an oxidation zone (143) in the bulk material moving bed (110) through which the gas flows in order to generate components of the synthesis gas (130), wherein the synthesis gas (130) is withdrawn at a removal point (131) between an upper bulk material zone (114) and a lower bulk material zone (115), and the carbon-rich substances (112) are moved with the bulk material moving bed (110) from the pyrolysis zone (141) in the upper bulk material zone (114), via the central region (104), into the reduction zone (142) and into the oxidation zone (143) in the lower bulk material zone (115) of the bulk material moving bed (110), wherein there is a co-current flowing through the upper bulk material zone (114) and a counter-current flowing through the lower bulk material zone (115).

Description

PREPARATION OF SYNTHESEGAS FROM CARBONATED SUBSTANCES BY MEANS OF A COMBINED DC-CURRENT PROCEDURE

The invention relates to a process for the production of synthesis gas from carbon-rich substances using a vertical shaft furnace with a bulk material moving bed according to the preamble of claim 1. Furthermore, the invention relates to a vertical shaft furnace for carrying out the method according to claims 38 to 44. Furthermore, the invention relates to the claims 45 and 46 the use of the synthesis gas produced by the method. Processes for the production of synthesis gas are known and are carried out in countercurrent gasifiers or in multistage gasifiers.

DE 10 2007 062 414 A1 describes a countercurrent gasifier for the gasification of carbon-rich substances, wherein the countercurrent gasifier has a moving bed of a material which does not participate in the decomposition or gasification of the carbon-rich substance and is itself not decomposed or gasified. A disadvantage of this countercurrent process is that the synthesis gas produced at the reactor outlet has a comparatively low temperature of less than 600 ° C and therefore due to incomplete thermal cleavage still contains undesirable long-chain hydrocarbons, which in a Nachvergasungsanlage both from a technical point of view, as well as from an energetic point of view consuming have to be treated. Only by the aftertreatment can their proportion in the synthesis gas be reduced.

In addition, the flow rate of the synthesis gas, which is taken in principle at an upper end of the countercurrent gasifier, very high because the entire amount of synthesis gas generated process is passed through the pyrolysis zone located in the upper shaft area. Due to this flow velocity, there is a risk that plastics will be entrained by the counterflow already at the upper end of the countercurrent gasifier with the exiting synthesis gas before they can enter the bed of the moving bed. This may result in uncontrolled pyrolysis of plastic particles in the raw gas system and in downstream plant components, as a result of which only insufficiently split plastic particles will cake into lumps. Furthermore, there is the risk for a moving bed used in the cycle that the moving bed is fed to the countercurrent gasifier at too high a temperature. In this way, there is a trade-off between energy-efficient operation and the ability to also use plastics in the process that have a low melting point.

DE 10 2012 014 161 A1 describes a method with two vertical process spaces, in which a carbon-rich substance located in a moving from top to bottom moving carbonaceous substance is gasified in countercurrent with oxygen-containing gas and in a second stage in a second vertical process chamber by means of oxygen-containing gas is vergvergast. In this case, the precompressed, formed in the first vertical process space, synthesis gas flows out at the top of the first vertical process space. Subsequently, the synthesis gas flows in at the top of the second vertical process space, flows through the second vertical process space and is drawn off in the lower area of the second vertical process space. In this process, too, there is the problem in the process space, which is operated countercurrently, that the flow rate of the synthesis gas, which is principally taken off at an upper end of the process space, is very high, because the entire amount of synthesis gas produced is due to the pyrolytes in the upper shaft area - sezone is passed. This results in a very high pressure loss, which complicates the implementation of the method. A disadvantage of the gasification by means of oxygen-containing gas during the flow through the second process chamber is that the post-oxidation energy efficiency of the process and at the same time the quality and the calorific value of the synthesis gas are adversely affected. For the present invention, therefore, the task has been posed to provide an improved process for the production of synthesis gas, with which a high gas quality is achieved and also both the energy use, as well as the technical complexity is kept low.

Main features of the invention are specified in the characterizing part of claim 1. Embodiments are the subject of claims 2 to 37. The claim 38 relates to a vertical shaft furnace for carrying out the method with embodiments according to claims 39 to 44. The use of the synthesis gas is the subject of claim 45, wherein claim 46 indicates an embodiment of the use.

The invention relates to a process for the production of synthesis gas from carbon-rich substances, wherein a bulk material moving bed consists of a bulk material, which is composed of the carbon-rich substances and a self-gasification material and wherein the bulk material moving bed in a vertical shaft of a vertical shaft furnace continuously or at intervals from above travels below and is traversed by gas, wherein the self-gasifying material and residues of the carbon-rich substances are discharged at the bottom of the vertical shaft, wherein formed in the flowed through by the gas bulk material moving bed to produce components of the synthesis gas at least one pyrolysis zone and a reduction zone in which reaction products are reduced from an oxidation zone which is likewise formed in the bulk material moving bed, the synthesis gas being conveyed in an intermediate region of the vertical shaft at an E The carbon-rich substances are at least partially removed with the bulk material moving bed from the pyrolysis zone in the upper bulk goods zone over the central area into the reductant zone, between the upper bulk material zone and a lower bulk material zone. a portion of the synthesis gas is generated in a formed in the upper Schüttgutzone pyrolysis of the bulk material moving bed and another portion of the synthesis gas is generated in a reduction zone in the lower Schüttgutzone and the upper Schüttgutzone in the DC and the lower Schüttgutzone is flowed through in countercurrent.

The provision of the upper Schüttgutzone and the lower Schüttgutzone and the removal of the synthesis gas in the central region between the upper Schüttgutzone and the lower Schüttgutzone is advantageous, since in this way at least two process zones can be formed, in which the bulk of the upper to lower Schüttgutzone extending carbon-rich substances are processable. This results in a further advantage that synthesis gases which arise in the pyrolysis zone can be conducted directly to the extraction point. The same applies to the synthesis gases formed in the reduction zone. In a particularly advantageous manner, this prevents the synthesis gases from coming into contact with the carbon-rich substances which have not yet passed through any of the process zones. Thus, incomplete pyrolysis of the carbon-rich substances at the shaft entrance is effectively prevented by hot synthesis gas. With regard to the quality of the synthesis gas, this is particularly advantageous, since the synthesis gas is essentially composed of the products of the substantially complete pyrolysis and the reduction by this arrangement of the bulk material zones, the removal point in the middle region and the gas streams forming thereby. The oxidation is also preferably at an energy level that is insufficient to melt or decompose the self-gasifiable material. The self-gasifiable material has the task of acting as a transport material to provide through its gap volume for a homogeneous gas permeability and to transport heat between the process zones. Depending on the starting material, it is preferable to use compacted, in particular pelleted, material as the carbon-rich material. In such a compacted, especially pelletized material, a plastic and a mineral constituent form a eutectic. Such a pelleted material migrates intact into the oxidation zone due to its high thermal stability with the self-non-gasifiable material. Thus, the void volume in the bulk material moving bed is largely retained. Depending on the choice of mineral constituents, no or only very small amounts of pollutants are released from the compacted, in particular pelletized material, so that the compacted, in particular pelletized, material can be used largely untreated or unprocessed in the process. In addition, the material which can not be gasified by itself can be comminuted by high shear forces in the bulk material moving bed Take over substances. In addition, by choosing a suitable material that can not be gasified, it is possible to bind certain pollutants out of the synthesis gas.

It is envisaged that a portion of the synthesis gas is generated in a pyrolysis zone of the bulk material moving bed formed in the upper bulk material zone, and a further portion of the synthesis gas is generated in a reduction zone in the lower bulk material zone.

By the partial production of synthesis gas in a pyrolysis zone situated in the upper region of the bulk material moving bed and in a reduction zone which is located in the lower region of the bulk material moving bed, two processes can advantageously be adjusted separately from one another in order to produce a high-quality synthesis gas. The synthesis gas may be partially different both in terms of the nature of the components as well as in terms of the proportions within the synthesis gas in the upper region and in the lower region. In the reduction zone, coke formed in the pyrolysis zone is preferably used for the reduction of carbon dioxide produced in the oxidation zone (Boudouard equilibrium). The heat energy necessary for this reaction is provided by the oxidation zone located in the vertical shaft below the reduction zone. In the reduction, carbon monoxide is advantageously formed, which contributes as an energy carrier to the heating value of the synthesis gas, or as a chemical component in the case of a material utilization of the synthesis gas.

Furthermore, it is provided that the upper bulk material zone is flowed through in direct current and the lower bulk material zone in countercurrent flow.

This results in the advantage that the synthesis gas in the upper region does not flow counter to the direction of the bulk material moving bed. As a result, upper regions of the bulk material moving bed, which have a comparatively low temperature in comparison with the temperatures prevailing in the direction of the course of the bulk material moving bed, are not flowed through by the hot synthesis gases produced in the pyrolysis zone. The direct current in the upper region also has the advantage that the hot, produced in the pyrolysis, synthesis gases come into contact only with the products of the pyrolysis of high-carbon substances and significantly higher gas temperatures are achieved than is the case in the countercurrent principle. Thus, an incomplete thermal cleavage of the pyrolysis and associated formation of oils and tars can be avoid as far as possible. If a partial fission still occurs, the pyrolysis products are not directly deducted, but go through even hotter process stages, in which the thermal decomposition of oils and tars is ensured.

Vorzugseise is provided that the self-gasifier material a weight of at least 20% of the total bulk material before warming in the upper

Has bulk solids and is heated in the upper Schüttgutzone of heated gas to a temperature of at least 350 ° C. This provides an energy buffer to compensate for the endothermic pyrolysis reaction and to ensure complete thermal cleavage of the carbonaceous substances.

The method is particularly advantageous if the carbon-rich substance and the material which can not be gasified by means of one or more rotating systems, preferably by parallel filling of a rotary bucket and / or via common and / or parallel dosing over one or more rotating chutes before and / or are mixed together after entering the vertical shaft. Such mixing can be achieved particularly effectively, for example, with a rotary bucket, which is filled in parallel with the two different materials during its own rotation. It is particularly advantageous that both the different components of the bulk material statistically distributed homogeneously in the bulk material, as well as a homogeneous distribution of different sized particles within the bulk material is achieved. The swivel bucket is preferably conveyed with a bucket elevator up to the task area of the vertical shaft furnace. The bucket can then be supplied to the upper end of the vertical shaft, where then the contents of the bucket is placed in the vertical shaft. In this way, it can be ensured that the contents of the container do not segregate or sort or fractionate during abandonment. Furthermore, with this type of feed, it is advantageous that the composition of the bucket contents per bucket can be changed. This allows the process to be controlled via the material added via the bucket.

A further preferred embodiment of the method provides that the carbon-rich substance and the self-gasifiable material are introduced individually at alternating intervals in the vertical shaft and thereby results in a layered arrangement of the materials in the bulk material moving bed, before this from top to bottom through the Vertical shaft moves. In this procedure can be dispensed with the mixing of the two materials. Although a layered and thus inhomogeneous arrangement is formed in the vertical shaft, the layer heights can be kept very low. This results about the in relation very high extent of the bulk material moving bed quasi a suitable and sufficient homogeneity for the process, which allows a good implementation of the vertical shaft important chemical and thermal processes.

Preference is given to a further embodiment of the method in which the introduction of the carbon-rich substance and the self-gasified material in the vertical shaft individually and / or as a mixture via a moving or static solids distribution, via a targeted distribution of materials depending on their different grain sizes in the bulk material moving bed is made possible. Such a distribution control is advantageous if one or both of the materials introduced have different particle sizes. In this case, it is advantageous to influence the distribution of coarse and fine material contained in the bulk material moving bed by the selective adjustment of angle of repose. This is done by exploiting different case parabolas which result depending on the particle weights. Thus, it is advantageous, for example, to enrich fine-grained materials in the immediate edge region of the vertical shaft in order to counteract a marginal tendency of the gas phase usually increased there due to the specifically larger gap volumes in the wall region.

Particularly advantageously, the method can be designed when an inner diameter at the lower end of the upper Schüttgutzone is smaller than an inner diameter at the upper end of the lower Schüttgutzone. This takes into account the different amounts of synthesis gas. In the upper bulk zone a lower amount of syngas is formed by pyrolysis than by the gasification reactions in the oxidation zone and the reduction zone in the lower bulk zone. By adjusting the inner diameters, the pressure losses can be kept low, even with different gas generation quantities in the upper and lower Schüttgutzone. This can be counteracted excessive Mitriss of particles in the central region of the vertical shaft at the sampling point.

A further preferred embodiment of the method is that the vertical shaft in the region of the upper Schüttgutzone and / or in the region of the lower Schüttgutzone is completely or partially conical, with an inner diameter increases in the conical regions from top to bottom. With a conical design of the vertical shaft, which provides an increase in the inner diameter of the vertical shaft increasing from top to bottom, account is taken of the process temperatures rising continuously from top to bottom to the oxidation zone, which is accompanied by an expansion of the solid particles of the bulk material. From this possibly resulting tilting or even bridge formations, which can lead to an inhomogeneous and uncontrolled migration of the bulk material moving bed, is counteracted by the conical configuration of the vertical shaft.

A preferred development provides that in the central region of the vertical shaft at least over part of the circumference of the bulk material moving bed one or more radial mixing chamber is formed, in which the proportions of the synthesis gas from the lower Schüttgutzone be mixed with the shares of the synthesis gas from the upper Schüttgutzone.

By providing one or more mixing chambers, the proportions of the synthesis gas, which originate from the lower region of the bulk material moving bed and, due to the process, have a comparatively high temperature can be mixed with the proportions of the synthesis gas originating from the upper region of the bulk material migrating bed in a particularly advantageous manner. and due to the process have a comparatively low temperature, mix. Thus, furthermore, an advantageously homogeneous synthesis gas results with a sufficiently high mixing temperature for the complete thermal cleavage.

Particularly advantageously, the mixing chambers can be produced by one or more breaks in the bulk material moving bed, wherein the bulk material moving bed in the central region of the vertical shaft contains at least 50% by weight of the material itself, which can not be gasified, in order to ensure a fluidized bed behavior necessary for producing the excavations to form a suitable angle of repose ,

Such quenching creates an increased outflow area, whereby the flow rate at the exit of the synthesis gas is kept relatively low. In this way, an entrainment of solid particles is counteracted. Furthermore, the movement of the slopes with the total flow of the bulk material moving bed from the top to the bottom prevents the outflow surface from becoming clogged with dust particles or being blocked asymmetrically.

Particularly preferably, it is provided that the temperature of the synthesis gas at the removal point is between 600 ° C and 1300 ° C. The temperature of the synthesis gas is adjusted so that an incomplete pyrolysis of the carbon-rich substances is advantageously effectively prevented. If the temperature is kept above the lower limit of the specified range, carbon-rich substances are largely completely pyrolyzed. This is ensured, in particular, by the comparatively hot synthesis gas from the lower bulk solids zone, by mixing with the comparatively colder synthesis gas from the upper bulk solids zone, forming a mixing temperature which is sufficiently high to ensure complete thermal decomposition of relatively long-chain constituents, such as oils or tars to ensure in the synthesis gas. Preferably, the mass ratio between the carbon-rich substances and the non-gasifiable material, eg a lime material, is in the range of 4: 1 to 1: 2. This mass ratio ensures that the processes in the process zones are ideal with regard to the transport of heat through the bulk material moving bed and the heat required for the endothermic reactions. The heat demand or the heat released in the process zones and their transition between the different zones also depends on the mass ratio between the carbon-rich substances and the non-gasifiable material.

A particularly expedient embodiment provides that the self-gasifiable material of the bulk material moving bed contains the lime material in a proportion of 10% to 100%, wherein the lime material preferably consists of quicklime and / or limestone.

Lime materials and especially quick lime have a positive influence on the energy requirements of the process. Quicklime, ie CaO or calcium oxide, can be hydrated below about 450 ° C. The hydration is exothermic, which advantageously provides energy in the form of heat for the endothermic processes in the vertical shaft furnace. In particular, the deleted form of quicklime, ie slaked lime, is to be used advantageously, since slaked lime halogens, such as chlorine or bromine and, moreover, also binds sulfur in the form of thermally stable salts as far as possible. This is advantageous in terms of the quality of the synthesis gas. In particular, when chlorine-rich and / or bromine and / or sulfur-containing carbon-rich substances are introduced into the bulk material moving bed. As halogen-rich substances are in particular materials in question, containing polyvinyl chloride or brominated flame retardants, as sulfur-rich substances such as vulcanized rubber or oil sands or oil shale come into consideration. A further preferred embodiment provides that at the upper end of the upper Schüttgutzone a gas space in the vertical shaft is formed, in which an overheated gas formed by oxidative processes, and / or in which a superheated gas is introduced.

By means of such a gas space, it is ensured that the superheated gas enters the bulk material moving bed homogeneously due to the prevailing overpressure, which results inter alia from the pressure loss of the upper bulk material zone. Furthermore, this results in the advantage that the pyrolysis zone is already formed high up in the vertical shaft and thereby results in optimal utilization of the upper Schüttgutzone at maximum residence time of the carbon-rich substances in hot reaction areas. A further preferred embodiment provides that a firing and / or an introduction of superheated gas takes place in the bulk material moving bed, in the region of the oxidation zone and / or in the region of the pyrolysis zone using insertion lances.

The ignition or introduction of superheated gas in the areas of the pyrolysis zone and the oxidation zone is advantageous because it allows the pyrolysis temperature and the oxidation temperature to be set. In this way, as far as possible complete pyrolysis and oxidation of the carbon-rich substance can be achieved. The firing or the introduction of superheated gas can be set flexibly, which is advantageous because the complete pyrolysis and / or oxidation can not only be adjusted via the migration speed of the bulk material moving bed, but can also be effected via the material flows for the insertion lances. By an adjustable firing via the Einstecklanzen can preferably also adjust the location of the process zones in the oven.

A further preferred embodiment provides that heating takes place in the region of the pyrolysis zone by addition of hot, self-gasifiable material as part of the bulk material, wherein the hot self-gasifiable material has an own temperature of more than 450 ° C., and preferably provided by industrial processes.

By the heat input by means of hot, even non-gasifiable material in the pyrolysis zone, the advantage can be achieved in the same way that the temperature and the position of the pyrolysis zone can be adjusted as a result. The material, which can not be gasified by itself, preferably has a temperature of more than 450 ° C., whereby the mass ratio does not itself gasify. The material to the carbon-rich substance is about 3: 1. The setting of the process temperature is largely carried out separately from the setting of the process temperature in the oxidation zone or in the reduction zone. Thus, at a constant traveling speed of the bulk material moving bed, the energy input in the individual processing zones can be controlled in an advantageous manner. It is also possible to use hot solids streams from industrial processes, for example cement clinker, as hot, even non-gasifiable materials. Alternatively, the hot non-gasifiable material may be a product of pig iron production.

In one embodiment, it is provided that water and / or water vapor are added to the bed of bulk material for the hydration of lime material as a constituent of the bulk material and utilization of the process heat released in the process.

Due to the additionally released heat energy from the hydration, endothermic processes in the pyrolysis zone and in the reduction zone can be supplied with energy by the exothermic hydration reaction. In addition, in the process space by the introduction of water vapor, the homogeneous water gas shift reaction proceed, with carbon monoxide acts as a reducing agent for the water vapor to form carbon dioxide and hydrogen. Furthermore, the heterogeneous water gas reaction is promoted, wherein water vapor reacts with pyrolysis to form carbon monoxide and hydrogen.

A further embodiment provides that carbon dioxide-containing gas is added in the bulk material bed for the carbonization of lime material as a constituent of the bulk material and utilization of the process heat released thereby and / or is formed by the addition of air or oxygen-containing gas by oxidation.

When calcium oxide is used as a constituent of the lime material, it is possible in certain temperature ranges to carry out the strongly exothermic carbonation reaction between carbon dioxide and calcium oxide with the formation of calcium carbonate by selective addition and / or oxidative generation of carbon dioxide, wherein the heat released is preferably in the reduction zone and / or the pyrolysis zone for the endothermic reactions occurring there can be used particularly advantageously. If fine calcium oxide is used as a constituent of the lime material and carbon monoxide is fed in at a temperature of about 650 ° C., then calcium carbonate forms exothermically in a temperature window up to about 850 ° C. From a temperature of about 850 ° C begins the endothermic deacidification of Calcium carbonate (lime burning) to CaO. In this way, energy can be conducted from one process zone to another process zone via the lime material of the bulk material moving bed.

Alternatively, it is provided in one embodiment that a cooling gas is introduced at an underside of the vertical shaft to form a post-cooling zone. The introduction of cooling gas at the bottom of the vertical shaft is advantageous, since the cooling gas can at least partially absorb the residual heat of the bulk material moving bed in the post-cooling zone and transported by the rise of the cooling gas in the upper regions of the vertical shaft in which partially endothermic reactions take place.

It is preferably provided that the cooling gas introduced at the bottom of the vertical shaft contains the synthesis gas and / or contains at least one combustible gas or alternatively contains air. Alternatively, it is provided that the cooling gas introduced at the bottom of the vertical shaft contains a mixture of reducible gas and air.

Due to the fact that synthesis gas is provided for the cooling gas, cooling of the bulk material moving bed takes place in an advantageous manner, without the cooling gas having a negative effect on the quality of the resulting synthesis gas. Rather, any proportions of carbon dioxide contained in the synthesis gas used in the reduction zone can be at least partially reduced by reaction with the pyrolysis to carbon monoxide and thus the synthesis gas quality can be improved overall. By providing a combustible gas, which is preferably natural gas, there is the advantage that the combustible gas can absorb the heat of the bulk material moving bed located in the aftercooling zone, while at the same time achieving an increase in the calorific value of the resulting synthesis gas due to the targeted metering of the natural gas or can be adjusted. By providing a reducible gas, preferably carbon dioxide and / or carbon dioxide-containing exhaust gases from combustion processes and / or carbon dioxide-containing gases from industrial production processes, there is the advantage that this gas largely does not participate in the processes taking place in the oxidation zone. Due to the endothermic reduction processes in the reduction zone, the heat conducted into the reduction zone by the reducible gas from the aftercooling zone can be utilized at least partially during the reduction of the reducible gas. When carbon dioxide is used as a reducible gas, the carbon dioxide is reduced to carbon monoxide by the pyrolysis coke after the Boudouard reaction. In this way, there is the particular advantage that pending at the sampling point Synthesis gas receives a higher calorific value by a then contained in the synthesis gas oxidizable gas.

The provision of air and / or a mixture of air with a reducible gas as the cooling gas has the advantage that the oxygen contained in the air in the oxidation zone for the oxidation of oxidizable gases and / or other oxidizable products of the pyrolysis, preferably pyrolysis, can be used completely. The processes in the oxidation zone ideally proceed stoichiometrically based on the pyrolysis coke still present in the oxidation zone, so that the synthesis gas which is withdrawn at the removal point preferably contains no oxygen and no carbonaceous substances reach the bottom of the oxidation zone with the moving bed.

A particularly preferred embodiment provides that the introduced at the bottom of the vertical shaft cooling gas from one or more gas streams from industrial processes, preferably from combustion and / or calcination or gases from the pig iron production, preferably top gas and / or coke gas and / or city gas consists. By using suitable gas streams from industrial processes, the process can be combined particularly efficiently with existing industrial processes. Thus, for example, when operating the method in a plant for pig iron production, a particularly efficient linkage of existing gas networks can be realized with the present method, where, for example, blast furnace gas is used as cooling gas. Its comparatively high content of carbon dioxide can be reduced to carbon monoxide in the reduction zone with the pyrolysis coke present there. As a result, use and simultaneous refinement of the top gas is achieved while, compared to the use of air as the cooling gas, less nitrogen is introduced into the process.

Preferably, it is provided that the bulk material moving bed pure oxygen or a gas mixture is added with air enriched oxygen content.

The addition of pure oxygen or a gas mixture with air enriched oxygen content has the advantage that the gas load of non-participating in the reactions contained in the synthesis gas gases, such as nitrogen, is reduced. In this way, the calorific value of the synthesis gas is increased. Preferably, the pure oxygen or the gas mixture with air enriched oxygen content is added directly by means of insertion lances in the region of the oxidation zone and / or in the region of the pyrolysis zone, while Synthesis gas and / or combustible gases and / or reducible gases may be added as cooling gas at the bottom of the vertical shaft.

Furthermore, it is particularly expedient that at least partially waste plastics and / or organic waste are used as carbon-rich substances. Plastic waste and / or organic waste accumulate in large quantities and have a suitable calorific value for the processes occurring in the process due to their high proportion of carbon. In particular, impure plastic waste, such as, for example, composite materials, plastic-containing waste fractions, shredder fractions from scrap recycling, plastic-containing production residues and the like can preferably be processed by the process into synthesis gas. This also applies to hydrocarbon-rich mixed materials, such as tar sands, oil shale or otherwise mixed with hydrocarbons media. The production of synthesis gas takes place here in a first stage by thermal decomposition of the organic components to pyrolysis gas to form pyrolysis coke. In the underlying reduction zone, the pyrolysis coke reacts in a second stage by the reduction of carbon dioxide to carbon monoxide. Furthermore, the pyrolysis coke with water vapor contained in the process forms additional carbon monoxide and hydrogen by the heterogeneous water gas reaction. In a third stage, almost complete oxidation of the remaining components of pyrolysis coke occurs in the oxidation zone. The oxidation zone is generally referred to in fixed bed or moving bed gasifiers as the reaction front. Any pollutants contained in the synthesis gas are preferably bindable by addition reactions to the bulk material moving bed. Non-gasifiable components of the plastic waste and in particular the impure plastic waste, such as metals and rare earth, remain in the bulk material moving bed and can be treated by downstream processes or can be recycled. In addition, it is provided in a further embodiment that organic high boilers, preferably in liquid form, are used as carbon-rich substances.

High boilers are in particular distillation residues, intermediate distillates and refinery residues. Thanks to the process and the various process zones, high-boiling components can also be gasified in the vertical shaft furnace process down to their non-gasifiable constituents. It is particularly advantageous if the high boilers preferably by means of insertion lances in the region of the pyrolysis zone and / or the reduction zone and / or the Oxida- tion zone introduced directly into the bulk material moving bed and / or metered via the gas space at the upper end of the upper Schüttgutzone in the bulk material moving bed and / or be added directly to the bulk material before entering the vertical shaft.

In one embodiment, it is provided that at least partially phosphorus-containing sewage sludge are used as high-carbon substances.

By using phosphorus-containing sewage sludge, the high organic content of the sewage sludge can be advantageously converted into synthesis gas. The residual products of pyrolysis and oxidation contain phosphorus-enriched ash. This ash can be used advantageously as fertilizer or processed to fertilizer. Particularly advantageous in this case is the use of lime materials as a bulk material moving bed, since in this way the material discharged from the vertical shaft can at least partially be used as a combined lime / phosphorus fertilizer.

A further preferred variant of the method provides that at least partially aluminum-containing residues and / or aluminum-containing waste are used as the high-carbon substance.

The use of aluminum as a constituent of the carbon-rich substance leads to aluminum reacting in particular in the presence of water vapor in the pyrolysis zone and the reduction zone with strong release of heat energy to aluminum hydroxide and hydrogen. As a result, the synthesis gas yield and the hydrogen content in the synthesis gas can be significantly increased. Furthermore, the heat energy released is available to compensate for the endothermic reactions in the pyrolysis zone and in the reduction zone.

In addition, the aluminum hydroxide in the oxidation zone is largely oxidized to alumina, which may optionally be recovered from the bulk moving bed. Due to the almost complete oxidation of the aluminum in the case of a dumping of the ashes from the bulk material moving bed no further hydrogen formation potential, whereby problems with regard to the unwanted hydrogen evolution in the case of so-called Spülversatzes as possible underground disposal are avoided.

Preferably, it is provided that in the carbon-rich substances present metal components, such as those found in electronic scrap in large proportions and / or other valuable substances, such as aluminum, halogens or phosphorus, chemically or physically be recovered from the discharged bulk material. This results in the advantage that the metal components or recyclables, which were not gasified in the process, can be supplied to a further utilization. The enriched residual materials can be prepared, for example, in wet-chemical processes, which applies in particular to rare earths. Alternatively, the enriched residual materials can be recycled directly.

Furthermore, it is particularly expedient that the bulk material moving bed at least partially passes through the vertical shaft several times in the circulation. This results on the one hand in the advantage that the need for non-gasifiable material can be kept to a minimum and on the other hand, the advantage that accumulate residual materials. Such residual materials are, for example, ashes, metals or minerals. The enriched residual materials can then be sorted, optionally treated and recycled.

Alternatively, it is provided in one embodiment that the synthesis gas withdrawn from the bulk material moving bed at the removal point is subsequently passed through a secondary bulk material bed which contains a secondary bulk material with a proportion of at least 10% up to a proportion of 100% of alkaline materials.

Furthermore, it is advantageous that at the extraction point withdrawn synthesis gas to pass through a Nebenschüttgutwanderbett, as in this Nebenschüttgutwanderbett any aerosols, tar or other solid constituents that are carried by the synthesis gas, are retained. In this way, the synthesis gas is purified. In addition, it is possible to post-treat the synthesis gas in the Nebenschüttgutwanderbett separately from the running in the vertical shaft processes.

It is preferably provided that the Nebenschüttgutwanderbett is guided in a secondary shaft of the vertical shaft furnace in countercurrent to the synthesis gas, wherein the secondary shaft of the vertical shaft furnace is arranged separately from the vertical shaft of the vertical shaft furnace.

By guiding the Nebenschüttgutwanderbettes in countercurrent to the gas stream of the synthesis gas and by the separate arrangement of Nebenschüttgutwanderbettes in a side shaft of the vertical shaft furnace, the aftertreatment of the synthesis gas from the process zones of the vertical shaft is advantageously decoupled. Any components or entrained elements of the synthesis gas removed from the synthesis gas by the by-product bulk material moving bed can advantageously be bound in the secondary bulk material moving bed and be disposed of separately or post-treated separately from the bulk material moving bed. Passing the gas stream in countercurrent to the fixed bed also has the advantage of effective heat exchange.

Preferably, it is provided that the synthesis gas is supplied in a central region of the secondary shaft and is withdrawn in an upper region of the secondary shaft or on an upper side of the secondary shaft.

This results in the advantage that the Nebenschüttgutmaterial extends over the upper region of the secondary shaft counter to the flow direction of the synthesis gas. A lower region of the secondary shaft, which lies below the upper region, is thus not flowed through by the synthesis gas. However, the down-migrating Nebenschüttgutwanderbett can absorb the heat of the flowing through the Nebenschüttgutwanderbett syngas. This is advantageous because the heat extracted from the synthesis gas is then available in the lower region of the secondary shaft.

Another embodiment of the synthesis gas purification in the secondary shaft provides that the Nebenschüttgutwanderbett is guided in a secondary shaft of the vertical shaft furnace in cocurrent to the synthesis gas, the secondary shaft of the vertical shaft furnace is preferably arranged separately from the vertical shaft of the vertical shaft furnace. This embodiment of the method allows a greatly simplified structural realization, because the synthesis gas can be easily introduced at the upper end of the secondary shaft, for example via a trained cavity. This ensures a homogeneous inflow into the Nebenschüttgutmaterial. In the case of a countercurrent flow, the design of the gas duct, which is structurally more complex, can be omitted in a central region of the secondary duct.

In a further embodiment of the direct-current conduction, it is provided that the synthesis gas is supplied in the upper region of the secondary shaft and withdrawn in the lower region of the secondary shaft. This results in a mixing temperature of the Nebenschüttgutmate- rials and the synthesis gas at the bottom of the secondary shaft.

In a further embodiment of the method it is provided that the Nebenschüttgutmaterial is cooled by means of a heat exchanger. By providing a heat exchanger, in particular in the lower region of the secondary shaft, there is the advantage that the heat released by the synthesis gas to the secondary bulk material moving bed into a heat exchanger. shear medium can be transferred, which gives off the heat at appropriate points of the vertical shaft furnace again. This is preferably done in the pyrolysis zone, or between the oxidation zone and the reduction zone by means of insertion lances. The heat exchange medium is preferably a medium which can be used in the processes taking place in the vertical shaft. Further preferably, the heat exchange medium is a combustible gas, water, steam or synthesis gas. For the advantages of the introduction of combustible gas and / or synthesis gas in the vertical shaft reference is made to the above statements. The introduction of water or steam into the vertical well is advantageous because water reacts with pyrolysis coke according to the Boudouard reaction to form carbon monoxide and hydrogen. Furthermore, there is another advantage when calcium oxide is used as the bulk material. The introduction of water or steam may utilize the hydration of the bulk material, thereby releasing heat energy available for the processes in the vertical well. This happens in particular when the intrinsic temperature of the bulk material at the point of introduction of water or water vapor is kept below 450 ° C.

In a further embodiment of the method it is provided that the Nebenschüttgutmate- rial is discharged uncooled from the side shaft in the lower region of the secondary shaft. The uncooled discharge of Nebenschüttgutmaterials has the advantage that the Nebenschüttgutmaterial that has been heated by the synthesis gas is available as input material for other processes available. The heating of Nebenschüttgutmaterials designed here advantageous if heat energy is required for the connection processes.

A further advantageous embodiment provides that the Nebenschüttgutmaterial taken uncooled in a lower portion of the secondary shaft from the secondary shaft and at least partially used as a hot non-gasifiable material in the vertical shaft and the heat energy contained in the pyrolysis zone is used.

The use of the Nebenschüttgutmaterials as a hot non-gasified material in the vertical shaft allows efficient use of the heat energy contained in the synthesis gas for the endothermic processes in the pyrolysis and reduction zone. The efficiency is realized in particular by the almost ideal heat exchange of the hot synthesis gas with the secondary bulk material in the secondary shaft. In this procedure, the efficiency of the process can be significantly increased because a significant portion of the heat content of the hot synthesis gas is not lost, but is returned to the vertical shaft. A further preferred embodiment provides that the Nebenschuttgutwanderbett is cooled below the central region of the secondary shaft in the lower region of the secondary shaft by countercurrently introduced cooling gas and / or the Nebenschüttgutwan- bed in the lower region of the secondary shaft is cooled by a heat exchanger. The cooling gas may be synthesis gas or a combustible gas. This results in the advantage that the secondary bulk material is discharged cooled from the secondary shaft. In particular, in downstream conveying or fractionating devices that can be used for the promotion or fractionation of Nebenschüttgutmaterials for its reuse, it is advantageous if the Nebenschüttgutmaterial is present so far cooled that the requirements for the heat resistance of the conveying or fractionation are lower.

Furthermore, it is particularly expedient that the mean grain size of the bulk material moving bed is greater than the mean grain size of Nebenschüttgutwanderbettes. By providing a smaller grain size for the Nebenschüttgutwanderbett there is the advantage that the Nebenschüttgutwanderbett can better filter the synthesis gas through its larger effective surface. Thus, both solid and gaseous pollutants of the synthesis gas are advantageously filtered or absorbed by the secondary bulk moving bed, which are not retained by the bulk material moving bed. By downstream of a fine-grained Nebenschüttgutwanderbettes in the synthesis gas stream after the bulk material moving bed, the bulk material moving bed can be made coarser, so that in a particularly advantageous manner, a higher gas flow rate is possible. Therefore, it is preferably provided that the mean grain size of the bulk material and the mean grain size of Nebenschüttgutmaterials in the range of 5 mm to 30 cm, preferably in the range of 5 mm to 15 cm or the mean grain size of the bulk material is greater than 1 cm and the average grain size of Nebenschüttgutmaterials is less than 10 cm.

A preferred embodiment provides that water and / or steam are added to the bulk material moving bed and / or the Nebenschüttgutwanderbett at one or more positions. Water and / or water vapor is preferably added in the upper region of the secondary bulk material moving bed and / or in the lower region of the bulk material migrating bed as cooling medium. The advantage of the addition of water or the addition of water vapor in the pyrolysis zone is that the bulk material moving bed can be specifically hydrated until reaching a temperature of about 450 ° C, provided that the bulk material moving bed consists of calcium oxide. The hydration is exothermic and therefore may require necessary heat energy for the pyrolysis of carbonaceous substances. Furthermore, the hydration by means of water or steam is advantageous because the at least partially forming calcium hydroxide is suitable to bind halogens or sulfur in the form of thermally stable salts as far as possible. In this way, the synthesis gas is purified of halogens and / or sulfur, which are released in the pyrolysis or oxidation of, for example, polyvinyl chlorides or vulcanized rubber. Particularly when water is added or when water vapor is added to the lower region of the bulk material moving bed, the water gas shift reaction in the bulk material moving bed reduces the water vapor to hydrogen by forming carbon dioxide as the reducing agent. In this way, the stable carbon dioxide and the hydrogen desired in the synthesis gas in certain subsequent applications is produced. The carbon dioxide may preferably be reduced to carbon monoxide by the Boudouard balance by the carbon present in the pyrolysis coke. The advantage of the reduction of carbon dioxide to carbon monoxide is that the synthesis gas contains a reactive gas and the cargo is reduced to a large extent to passive gases.

The invention further relates to a vertical shaft furnace for carrying out the method comprising a vertical shaft with a continuously extending in the vertical shaft or at intervals Schüttgutwanderbett, comprising a bulk material of a carbon-rich substance and a self-gasification material, the vertical shaft in a central region a removal point for the Has synthesis gas.

Because the vertical shaft has a removal point in a central region, a plurality of process zones can advantageously be formed in the vertical shaft, which are separated from one another by the removal point. Thus, an upper area and a lower area are formed. As a result of the separation of the areas produced by the removal point, separate vertical spaces are provided by the vertical shaft furnace, in which processes can be carried out separately from one another. This is particularly advantageous when the requirements on the processes with respect to parameters such as temperature, pressure and / or stoichiometry are different.

A further preferred embodiment of the vertical shaft furnace provides that the bulk material can be mixed before and / or after entry into the vertical shaft by a mixing device. In addition, in one embodiment it can be provided that the carbon-rich substance and the material which can not be gasified by means of one or more rotating systems, preferably by parallel filling of a rotary bucket and / or via common and / or parallel metering via one or more rotating chutes before and / or after entry into the vertical shaft are miscible with each other. By providing a mixing device is advantageously ensured that the bulk material of the bulk material moving bed is homogeneous. Alternatively, it can be provided that the carbon-rich substance and the self-gasifiable material can be introduced individually at alternating intervals in the vertical shaft. Due to the individual introduction of the components of the bulk material moving bed, the composition of the bulk material moving bed is controlled adjustable. Because the components can be introduced individually at alternating intervals, the vertical shaft furnace can be moved in different ways. It is preferably provided that a targeted distribution of the materials of the bulk material moving bed as a function of their different particle sizes can be achieved by means of a static solids distributor. By a targeted distribution of the materials as a function of the grain size, an influence on the adjustment of the angle of repose in the bulk material moving bed is vornehmbar.

Furthermore, it is particularly expedient for the vertical shaft furnace that a lower end of an upper bulk cargo zone of the vertical shaft has a smaller inner diameter than an upper end of a lower bulk cargo zone of the vertical shaft. By providing different diameters are pressures that arise in the vertical shaft furnace, advantageously compensated or influenced, so that the production of a certain pressure profile in the vertical shaft furnace can be achieved. A further advantageous embodiment of the vertical shaft furnace provides that the vertical shaft in the region of the upper Schüttgutzone and / or in the region of the lower Schüttgutzone is completely or partially conical. Preferably, the inner diameter in the conical regions increases from top to bottom. The conical shape of the regions affords the advantage that a material expansion of the bulk material can be taken into account, so that the bulk material in the vertical shaft does not jam with the wall of the vertical shaft.

The vertical shaft furnace can be further developed in that in the central region of the vertical shaft at least over part of the circumference of the bulk material moving bed one or more radial mixing chambers are formed, preferably at the level of the extraction point for the synthesis gas. An advantage of the radial mixing chambers in the middle region is that a particularly homogeneous mixing of the synthesis gas produced by the process can be achieved. In a further embodiment of the vertical shaft furnace it is provided that the bulk material moving bed has one or more slopes in the area of the mixing chambers. The bulk material moving bed preferably has a suitable angle of repose in the middle region of the vertical shaft in order to ensure a fluidized bed behavior necessary for the production of the quarries. An advantage of this is that the boundary surface between the bulk material moving bed and the mixing chambers in the central region increases due to the provision of excavations. Thus, there is the advantage that synthesis gases produced in the process are particularly easily derivable via this interface.

In an alternative embodiment, it is provided for the vertical shaft furnace that the vertical shaft furnace has a secondary shaft arranged separately from the vertical shaft and there is a flow connection between the secondary shaft and the vertical shaft. By providing a secondary shaft there is the advantage that the synthesis gas produced in the process can be cleaned in the secondary shaft. In addition, additional facilities can be provided in the secondary shaft which make it possible to treat the synthesis gas after treatment.

Moreover, the invention relates to the use of the synthesis gas produced by a method according to any one of the preceding claims as a fuel gas for thermal utilization and / or as a fuel gas for power generation and / or as a raw material in chemical processes. It is particularly advantageous here that the synthesis gas can be used directly on site, ie where the process is taking place. In this way, exhaust gases and / or any waste heat can be supplied to the process, whereby the energy requirement of the process can be further reduced.

Preferably, it is provided that the synthesis gas is filtered prior to its use and optionally cooled depending on further use. Filtering ensures a dust-free syngas, which can be used in filtered form and, where appropriate, also after cooling, for demanding applications, for example in internal combustion engines.

Further features, details and advantages of the invention will become apparent from the wording of the claims and from the following description of exemplary embodiments with reference to the drawings. Show it: Figure 1 is a schematic representation of a vertical shaft furnace with a vertical shaft for carrying out the process for the production of synthesis gas.

Fig. 2 is a schematic representation of a vertical shaft furnace with a vertical shaft and a secondary shaft for carrying out the process for the production of synthesis gas, wherein in the secondary shaft a countercurrent mode is realized and

Fig. 3 is a schematic representation of a vertical shaft furnace with a vertical shaft and a secondary shaft for carrying out the method for the production of synthesis gas, wherein in the secondary shaft a Gleichstromfahrweise is realized.

1 shows a vertical shaft furnace 1 for carrying out the method for producing synthesis gas 130 from carbon-rich substances 1 12. The vertical shaft furnace 1 has a vertical shaft 100, in which a bulk material moving bed 1 10 moves from top to bottom. The bulk material moving bed 1 10 consists of bulk material 1 1 1, which is fed from a bulk material source 120. The bulk material 1 1 1 is composed of two materials. The first material consists of the carbon-rich substance 1 12, which is processed to synthesis gas 130. The second material is a self-gasifiable material 13, which is not processed into syngas 130. To ensure a homogeneous distribution of the carbon-rich substance 1 12 and the self-gasifiable material 1 13 in the bulk material 1 1 1 is preferably an unrepresented spin tub with the two materials mate- rials filled under rotation before the bulk material is introduced as a mixture in the vertical shaft.

The bulk material 1 1 1 is introduced from the rotary bucket on an upper side 101 of the vertical shaft 100 in the vertical shaft 100 via a gas space 103 and passes through the vertical shaft 100 by gravity. The introduction can preferably take place via a moving or static solids distributor 16, via which a targeted distribution of the bulk material material can be effected as a function of its different particle sizes in the bulk material moving bed 110.

The bulk material 1 1 1 is removed at the bottom 102 of the vertical shaft 100 and fed to a post-treatment to be described later. As an alternative to the above-described introduction of the carbon-rich substance 1 12 and the self-gasifiable material 1 13 as a mixture, both materials can also be introduced individually at alternating intervals in the vertical shaft, whereby the materials are quasi-layered in the bulk material moving bed 1 10. In this case, the introduction can also preferably take place via a moving or static solids distributor 16, via which a targeted distribution of the materials depending on their different particle sizes in the bulk material moving bed 110 can take place.

For example, as high-carbon substance 1 12, high-carbon wastes such as e.g. Biomass, plastics, sewage sludge, oily sands or oil shale can be used. The self-gasifiable material 1 13 is preferably made of a mineral material, preferably of a calcitic material, particularly preferably of calcium oxide.

The flow of the bulk material 1 1 1 takes place from the top 101 of the vertical shaft 100 to the bottom 102 of the vertical shaft 100, wherein the bulk material 1 1 1 different process zones of the vertical shaft 100 passes. First, the bulk material 1 1 1 passes through a pyrolysis 141. In the pyrolysis zone 141 organic compounds are thermally split. In doing so, organic molecules are split into molecules that are shorter than the parent molecules. The splitting takes place in a temperature range between 200 ° C and 900 ° C

After the pyrolysis zone 141 in the direction of the underside 102 of the vertical shaft 100 there is an oxidation zone 143. In the oxidation zone 143, a residue of the pyrolysis is oxidized to carbon dioxide or carbon monoxide. This residue of pyrolysis is also referred to as pyrolysis coke.

Between the oxidation zone 143 and the pyrolysis zone 141 there is a reduction zone 142, in which the carbon dioxide is reacted with elemental carbon by the Boudouard equilibrium in carbon monoxide. This reaction is endothermic and is supplied with heat energy by the oxidation zone 143 below the reduction zone 142, in which the exothermic oxidation of the pyrolysis coke occurs. An additional supply of heat energy takes place from the sensible heat of the bulk material moving bed coming from the pyrolysis zone 141. After the oxidation zone 143 is followed by a post-cooling zone 144, in which the bulk material moving bed is cooled. The bulk material moving bed 1 10 is discharged from the vertical shaft 100 via a discharge device 150.

About the control of the discharged through the discharge device 150 material flow of the bulk material moving bed 1 10 can be the residence time in the vertical shaft 100 control. In this way, the process is adjustable by the residence time of the carbon-rich substance 1 12 or its residues in the different process zones 141, 142, 143, 144.

The bulk material 1 1 1 of the bulk material moving bed 1 10 is passed after discharge at the bottom 102 of the vertical shaft 100 in a separation device 10, where the bulk material 1 1 1 is fractionated into coarse grain 151, middle grain 152 and fine grain 153 in three particle size fractions.

The fraction of the coarse grain 151 can be returned to the bulk material source 120 and supplements the self-gasifiable material 1 13 in the bulk material source 120.

The mid-grain fraction 152 is disposed of or is available for further use. The fine grain fraction 153, which also partially contains the ashes produced in the pyrolysis zone 141 and / or in the oxidation zone 143, forms a fine waste 154 which is disposed of or utilized in the enrichment of valuable residual materials.

The vertical shaft 100 is traversed in addition to the bulk material moving bed 1 10 with a gas stream. The gas stream runs in an upper bulk material zone 14 of the vertical shaft 100 in direct current with the bulk material moving bed 1. That is, the gas stream runs in the direction from the upper side 101 of the vertical shaft 100 in the direction of the underside 102 of the vertical shaft 100 and in this case the pyrolysis zone 141 flows through ,

In a lower bulk material zone 1 15 of the vertical shaft 100, the gas stream runs in countercurrent to the bulk material moving bed 1 10. That is to say, the gas stream runs in the direction from the lower side 102 of the vertical shaft 100 to the upper side 101 of the vertical shaft 100.

Between the upper Schüttgutzone 1 14 of the vertical shaft and the lower Schüttgutzone 1 15 of the vertical shaft is a central portion 104 of the vertical shaft. In this central region 104, the gas flow which runs with the bulk material moving bed 100 is discharged the upper bulk material zone 14 and the gas flow flowing from the lower bulk zone 15 against the bulk material moving bed 110. The pressure within the vertical shaft 100 is lowest in the central area 104.

In the middle region 104 of the vertical shaft 100, the gases originating from the pyrolysis zone 141 located in the upper bulk material zone 14 and the gases originating from the reduction zone 142 located in the lower bulk zone 15 are withdrawn at a removal point 131 of the vertical shaft 100.

The bulk material moving bed 1 10 forms, in the middle region 104 of the vertical shaft 100, together with the vertical shaft 100, a radial mixing chamber 105, which is formed over at least part of the circumference of the bulk material moving bed 1 10. In this radial

Mixing chamber 105 of the resulting from the lower Schüttgutzone 1 15 gas stream and from the upper Schüttgutzone 1 14 derived gas stream are mixed.

In a preheating region 145 in the upper region of the pyrolysis zone 141 and / or within the pyrolysis zone 141, air 50 and / or natural gas 60 and / or a heat exchange medium 21 are introduced through upper insertion lances 106. Flammable gases are at least partially burned in this upper bulk zone 14 to provide thermal energy. Introduced media 50, 60, 21, which carry heat energy, give their heat energy in this preheating area 145 to the bulk material 1 1 1 from. In any case, the bulk material 1 1 1 first passes through a preheating area 145, in which the bulk material 1 1 1 is preheated. Alternatively, the media 50, 60, 21 may also be introduced directly into the gas space 103, where combustible gases are at least partially combusted to provide thermal energy. Introduced media 50, 60, 21, the heat energy carry and or the oxidizing gas, flow due to the prevailing overpressure in the gas space 103 in the bulk material moving bed 1 10 and give their heat to the bulk material 1 1 1 from. Instead of the natural gas 60, other combustible gases may be introduced. It is also possible to use flammable gases superheated by the injectors 106 and / or the gas space, or a superheated, reducible gas, such as e.g. To introduce carbon dioxide.

By the combustion of natural gas 60 or the introduction of heat energy-carrying media 50, 60, 21, the temperature of the bulk material moving bed 1 10 of a temperature below Increased 200 ° C when entering the vertical shaft 100 to a temperature above 200 ° C in the pyrolysis 141.

Below the oxidation zone 143, it may be provided that water vapor 70 is introduced via lower insertion lances 108. In this case, the steam is used as the cooling gas to cool the moving bed to a temperature above 450 ° C. This lower temperature limit is maintained to preclude undesirable hydration at this point when calcium oxide is used as the non-gasifiable material.

Optionally, water vapor 70 can also be introduced in the upper bulk material zone 14 via the upper insertion lances 106. Here is when using calcium oxide as self-gasifying material 1 13, the energy released by the hydration for the pyrolysis of the carbon-rich substance 1 12 available.

Between the oxidation zone 143 and the reduction zone 142, light oil 30 and / or heavy oil 80 can be introduced into the bulk material moving bed 1 10 through middle insertion lances 107. By introducing light oil 30 and / or heavy oil 80, the amount of synthesis gas and the calorific value of the synthesis gas 130 can be increased. Furthermore, the temperature in the oxidation zone 143 can be controlled so that the oxidation of the carbon-rich pyrolysis residues and the carbon-rich residues from the reduction zone is ensured to the greatest possible extent without oxidative overheating taking place. By introducing water 40 between the oxidation zone 143 and the reduction zone 142 via the middle insertion lances 107, the water 40 is used as a coolant, which allows the control of the temperature in the oxidation zone 143 by its enthalpy of vaporization and heat absorption, so that a most extensive oxidation of the carbon-rich pyrolysis residues and the carbon-rich residues from the reduction zone 142 are ensured without oxidative overheating taking place.

For complete oxidation of the carbon-rich residues from the pyrolysis zone 141 and the reduction zone 142 in the oxidation zone 143 takes place at the bottom 102 of the vertical shaft 100, a supply of oxygen-containing gas 90. As the oxygen-containing gas can be used 50 and / or a gas mixture with a proportion of oxygen become. Preferably, the supply of oxygen-containing gas 90 via the bottom of the vertical shaft 100 is adjusted so that the oxidation zone 143 and the reduction zone 142 are stoichiometrically oxygenated so that no oxygen is transferred to the central region 104 of the vertical shaft 100. In this way, there is the synthesis gas 130, which forms in the central region 104 from the gas flow flowing parallel to the bulk material moving bed 1 10 in the upper Schüttgutzone 1 14 and the gas stream from the lower Schüttgutzone 1 15, from a gas mixture containing no oxygen. By the introduction of air 50 or oxygen-containing gas 90 at the bottom 102 of the vertical shaft 100, the bulk material moving bed 110 is cooled in the lower bulk zone 15 of the vertical shaft 100 and in particular in the aftercooling zone 144.

Particularly preferably, the supply of oxygen-containing gas 90 and / or air 50 takes place via the underside of the vertical shaft via two separately adjustable partial flows. In order to achieve an optimum gas distribution in the aftercooling zone 144, a cooling gas edge stream 91 is introduced into the aftercooling zone 144 via the outer edge region of the bulk material moving bed 1 10, while a central cooling gas stream 92 is introduced into the region of the center of the bulk material moving bed 1 10 Aftercooling zone 144 is initiated.

The process can be supplied as high-carbon substances solid or liquid high boilers 109 on the bulk material. In addition, liquid high boilers 109 may be supplied to the process via the upper insertion lances 106, the middle insertion lances 107 and / or the lower insertion lances 108.

The supplied at the bottom 102 of the vertical shaft 100 cooling gas is in the bulk material moving bed in a cooling gas edge stream 91 on the outside of the bulk material moving bed 1 10 and in a central cooling gas stream 92 in a central region of the bulk material moving bed 1 10 feasible. FIG. 2 shows the vertical shaft furnace 1 with a secondary shaft 210 which is likewise designed in the form of a vertical shaft and through which the synthesis gas formed is conducted in countercurrent to the secondary bulk material moving bed 220.

In Nebenschachtgut 210 runs a Nebenschüttgutwanderbett 220 from top to bottom continuously. The Nebenschüttgutwanderbett 220 is fed by a Nebenschüttgutquelle 230 with Nebenschüttgutmaterial 221 and extends from a top 21 1 of the secondary shaft 210 to a bottom 212 of the secondary shaft 210th The Nebenschüttgutwanderbett 220 consists of a Nebenschüttgutmaterial 221, preferably a mineral material, preferably from calcium oxide and / or calcium carbonate.

Preferably, the average particle size of Nebenschüttgutmaterials 221 is less than the mean grain size of the bulk material 1 1 1. In the Nebenschüttgutwanderbett 220 from the middle portion 104 of the vertical shaft 100 at the removal point 131 extracted synthesis gas 130 is introduced.

For this purpose, the Nebenschüttgutwanderbett 220 forms with the secondary shaft 210 a radial chamber 213, which is formed over at least a portion of the circumference of Nebenschüttgutwanderbettes 220. Through this radial chamber 213, the synthesis gas 130 flows into the secondary bulk material moving bed 220.

The synthesis gas 130 flows through the secondary bulk material moving bed 220 in an upper region 214 of the secondary shaft 210 in countercurrent. The synthesis gas 130 is in the upper portion 214 of the secondary shaft 210 from the secondary shaft 210 at a discharge point

216 derived. In particular, the use of calcium oxide as Nebenschüttgutmaterial 221 in the Nebenschüttgutwanderbett 220 is advantageous because portions of the synthesis gas 130, the halogens and chlorine in particular, are bound by calcium hydroxide, resulting from the introduction of water 40 or steam 70, for example via Nebeneinstecklanzen

217 in the upper region of the secondary shaft 210 can be generated by hydration. Halogens and, in particular, chlorine are formed, for example, in the oxidation or pyrolysis of polyvinyl chlorides.

In addition, synthesis gas 130 can be purified by providing calcium oxide as a minor bulk material of sulfur compounds.

The Nebenschüttgutwanderbett 220 also serves to dissipate heat from the synthesis gas 130, which leaves the vertical shaft 100 with the bulk material moving bed 1 10 at the removal point 131 at a temperature of about 600 ° C. The countercurrent, which is formed between the running Nebenschüttgutwanderbett 220 and the rising synthesis gas 130, the heat absorption by the Nebenschüttgutwanderbett 220 can make efficient.

The secondary bulk material moving bed 220 is discharged from the secondary shaft 210 via a secondary discharge device 240. By controlling the Nebenausleitungsvorrichtung 240, the residence time of Nebenschüttgutwanderbettes 220 can be controlled in the secondary shaft 210.

The Nebenschüttgutmaterial 221 discharged through the Nebenausleitungsvorrichtung 240 is fed to the separation device 10, where the Nebenschüttgutmaterial 221, as well as the bulk material 1 1 1, according to coarse grain 151, center grain 152 and fines 153 is fractionated.

The middle grain 152 separated in the separation device 10 can be at least partially added to the secondary bulk material source 230 and, together with the secondary bulk material 221, can form the secondary bulk material moving bed 220. Here, both the fractionated bulk material 1 1 1 of the bulk material moving bed 1 10 of the vertical shaft 100 and the fractionated secondary bulk material 221 of the secondary bulk material moving bed 220 of the secondary shaft 200 in a common fraction form the middle grain 152.

In the lower region 215 of the secondary shaft 210, a heat exchanger 20 is arranged. The heat exchanger 20 receives the heat of Nebenschüttgutwanderbettes 220, which was discharged through the synthesis gas 130 to the Nebenschüttgutwanderbett 220. A heat exchanger medium 21, which transports the heat toward the upper insertion lances 106 of the vertical shaft 100, flows through the heat exchanger 20. Natural gas 60, synthesis gas 130, water 40 or steam 70 can be used as the heat exchanger medium 21.

The heat exchanger medium 21 is introduced through the upper insertion lances 106 into the bulk material moving bed 110 and discharges the heat there to the bulk material moving bed 110. In this way, the self-gasifiable material 1 13 and the carbon-rich substances 1 12 are warmed or heated to the required pyrolysis temperature.

The heat input through the heat exchanger medium 21 contributes to a reduction in the energy requirement in the pyrolysis zone 141 and in the subsequent reduction zone 142 and oxidation zone 143. Furthermore, the quality of the synthesis gas is improved because the dosage of air 50 for the firing may be omitted in whole or in part. As a result, less nitrogen reaches the pyrolysis zone, which reduces the calorific value of the synthesis gas 130.

The minor bulk moving bed 220 is preferably cooled by introduction of cold syngas 130 into at the bottom 212 of the secondary shaft 210. The synthesis gas 130 flows through the Nebenschüttgutwanderbett 220 in countercurrent and meets in a central region 218 of the secondary shaft 210 on the synthesis gas 130, which emerges at the removal point 131 of the vertical shaft 100 and is introduced into the radial chamber 213 of the secondary shaft 210.

The synthesis gas 130 derived from the secondary shaft 210 at the discharge point 216 is passed through a synthesis gas heat exchanger, not shown, wherein the synthesis gas 130 is further cooled in this synthesis gas heat exchanger. The heat extracted from the synthesis gas 130 can be supplied to the vertical shaft 100 at the upper insertion lances 106 via a suitable heat medium, which is, for example, water vapor 70, air 50, natural gas 60 or synthesis gas 130. In the further course of the synthesis gas 130 passes through a synthesis gas filtration, also not shown, wherein in the synthesis gas 130 contained particulate matter is deposited.

Thereafter, the syngas 130 filtered by the particulate matter passes through a second synthesis gas heat exchanger and is fed to a quench circuit wherein the synthesis gas 130 is separated from heavy oil 80, light oil 30 and water 40 in various process steps. The separated heavy oil 80 and / or Leichtol 30 and / or water 40 can be supplied via the middle Einstecklanzen 107 between the oxidation zone 143 and the reduction zone 142 to the vertical shaft 100. The separated water 40 can also be introduced via the insertion lances 106 into the preheating area 145 of the vertical shaft 100 and / or via the Nebeneinstecklanzen 217 in the secondary shaft 210. The filtered and freed by condensation of heavy oil 80, Leichtol 30 and water 40 synthesis gas 130 is available as a fuel for engines, for example for power generation. Furthermore, the synthesis gas 130 recovered in the process may be used thermally, for example as a substitute for fossil fuels or as a material. Especially in the generation of electricity from the synthesis gas 130 heat and engine exhaust gases containing water vapor and carbon dioxide, which can be supplied to the process at suitable locations, preferably via the insertion lances 106, 108.

In another, not shown, embodiment of the bulk material moving bed 1 10 as carbon-rich substances 1 12 sewage sludge, for example in compacted form, fed. In this case, the process is carried out analogously to the first exemplary embodiment, preferably with the exception that the secondary bulk material 221 discharged through the secondary diverter 240 is compacted and is no longer supplied to the cycle of the secondary bulk material bed 220. Alternatively, the briquetted Nebenschüttgut- material to enrich the accumulating by the processing of sewage sludge phosphates are also used several times in the bulk material moving bed 100.

FIG. 3 shows a further exemplary embodiment of a vertical shaft furnace 1 with a secondary shaft 310, which is likewise embodied in the form of a vertical shaft and through which the synthesis gas 130 formed is guided in direct current to the secondary bulk material moving bed 320 and passed therethrough.

The vertical shaft 100 corresponds to the vertical shaft 100 according to the embodiments of FIGS. 1 and 2, to which reference will be made at this point.

In the secondary shaft 310, the secondary bulk material moving bed 320 runs continuously from an upper side 31 1 of the secondary shaft 310 to an underside 312 of the secondary shaft 310. The Nebenschüttgutwanderbett 320 is fed by a Nebenschüttgutquelle 330 with Nebenschüttgutmaterial 321.

The Nebenschüttgutwanderbett 320 has a Nebenschüttgutmaterial 321, preferably a mineral material, preferably calcium oxide and / or calcium carbonate.

In the Nebenschüttgutwanderbett 320 from the central region 104 of the vertical shaft 100 at the removal point 131 extracted synthesis gas 130 is introduced via a cavity 322 at an upper portion 314 of the secondary shaft 320.

The synthesis gas 130 flows through the Nebenschüttgutwanderbett 320 in cocurrent and is derived in a lower portion 315 of the auxiliary shaft 310 from the secondary shaft 310 at a discharge point 316. In particular, the use of calcium carbonate as Nebenschüttgutmaterial 321 in the Nebenschuttgutwanderbett 320 designed in the DC advantageous, since in this case a cooling by metering of water 40 or water vapor 70 via spray nozzles 317 can be done directly through the cavity 322 without the Nebenschüttgutmaterial 321 is hydrated , As a result, an efficient direct cooling in the secondary bulk moving bed 320 can be realized.

The Nebenschüttgutwanderbett 320 is discharged from the secondary shaft 310 via a secondary discharge device 340. By controlling the Nebenausleitungsvorrichtung 340, the residence time of Nebenschüttgutwanderbettes 320 in the secondary shaft 310 can be controlled.

The Nebenschüttgutmaterial 321 discharged through the Nebenausleitungsvorrichtung 340 is fed to the separation device 10, where the Nebenschüttgutmaterial 321, as well as the bulk material 1 1 1, according to coarse grain 151, center grain 152 and fines 153 is fractionated. The middle grain 152 separated in the separation device 10 can be added at least partially to the secondary bulk material source 330 and, together with the secondary bulk material 321, can form the secondary bulk material moving bed 320. Here, both the fractionated and discharged from the discharge device 150 bulk material 1 1 1 of the bulk material moving bed 1 10 of the vertical shaft 100, as well as the fractionated Nebenschüttgutmaterial 321 of Nebenschüttgutwanderbettes 320 of the auxiliary shaft 310 in a common fraction, the middle grain 152.

In the lower region 315 of the secondary shaft 310, a heat exchanger 20 is arranged, which is analogous to the description of Figure 2 application. Natural gas 60, synthesis gas 130, water 40 or steam 70 can be used as the heat exchanger medium 21.

The synthesis gas 130 derived from the secondary shaft 310 in the lower region 315 of the secondary shaft 310 at the discharge point 316 can be further processed and used analogously to the description of FIG.

The invention is not limited to one of the above-described embodiments, but can be modified in many ways. All resulting from the claims, the description and the drawing features and advantages, including design details, spatial arrangements and decay renssch ridden, can be essential to the invention both in itself and in various combinations.

Reference numeral vertical shaft furnace

120 bulk material source

Sorting device 130 synthesis gas

131 sampling point

heat exchangers

Heat exchange medium 141 pyrolysis zone

142 reduction zone

light oil

143 oxidation zone

water

144 post-cooling zone

air

145 preheating area

natural gas

Water vapor 150 discharge device

Heavy oil 151 coarse grain

152 middle grain

oxygen-containing gas

153 fine grain

Cooling gas Rand

154 fine waste

Cooling gas central power

210, 310 side shaft

vertical shaft

21 1, 31 1 Top side of the secondary shaft Top side of the vertical shaft

212, 312 Bottom of the secondary shaft Bottom of the vertical shaft

213 radial chamber of the secondary shaft gas space

214, 314 upper area of the secondary shaft middle area

215, 315 lower area of the secondary shaft radial mixing chamber

216, 316 derivation point

upper insertion lances

217 side insertion lances

medium plug-in lances

218 middle section of the secondary shaft lower insertion lances

high boiler

220, 320 Nebenschüttgutwanderbett

Bulk material bed 221, 321 Nebenschüttgutmaterial

bulk material

carbon-rich substance 230, 330 Nebenschüttgutquelle

self-gasifiable material 240, 340 side skim upper skimmed zone

lower bulk solids 317 spray nozzles

Solids distributor 322 cavity

Claims

Patentans praise

A process for the production of synthesis gas (130) from carbon-rich substances (1 12), wherein a bulk material moving bed (1 10) consists of a bulk material (1 1 1), which consists of the carbon-rich substances (1 12) and a self-gasifiable material ( 1 13) and wherein the bulk material moving bed (1 10) in a vertical shaft (100) of a vertical shaft furnace (1) moves continuously or at intervals from top to bottom and is traversed by gas, the self-gasification material (1 13) and residues the carbon-rich substances (1 12) at the bottom (102) of the vertical shaft (100) are discharged, wherein in the flowed through by the gas bulk material moving bed (1 10) for generating components of the synthesis gas (130) at least one pyrolysis zone (141) and a Reduction zone (142) can be formed, in which reaction products from a likewise formed in the bulk material moving bed oxidation zone (143) Reduzi be distinguished, characterized in that the synthesis gas (130) in a central region (104) of the vertical shaft (100) at an extraction point (131) between an upper Schüttgutzone (1 14) and a lower Schüttgutzone (1 15) is subtracted and the carbon-rich substances (1 12) at least partially with the bulk material moving bed (1 10) of the pyrolysis zone (141) in the upper Schüttgutzone (1 14) over the central region (104) in the reduction zone (142) and in the oxidation zone (143) a portion of the synthesis gas (130) in one in the upper Schüttgutzone (1 14) formed pyrolysis zone (141) of the bulk material moving bed (1 10) is generated and another Proportion of the synthesis gas (130) in a reduction zone (142) in the lower Schüttgutzone (1 15) is generated and the upper Schüttgutzone (1 14) in cocurrent and the lower Schüttgutzone (1 15) in countercurrent is being streamed.

A method according to claim 1, characterized in that in the upper Schüttgutzone (1 14) introduced itself non-gasifiable material (1 13) prior to warming a weight fraction of the bulk material (1 1 1) of at least 20% and that Even non-gasifiable material (1 13) in the bulk material (1 1 1) in the upper bulk material zone (1 14) is warmed up to a temperature of more than 350 ° C by means of heated gas.

Method according to one of the preceding claims, characterized in that the carbon-rich substance (1 12) and the self-gasifiable material (1 13) by means of one or more rotating systems, preferably by parallel filling of a rotary bucket and / or via common and / or parallel Dosing over one or more rotating chutes before and / or after entering the vertical shaft (100) are mixed together.

A method according to claim 2, characterized in that the carbon-rich substance (1 12) and the self-gasifiable material (1 13) are introduced individually at alternating intervals in the vertical shaft and thereby a layered arrangement of the materials in the bulk material moving bed (1 10) results before it moves from top to bottom through the vertical shaft (100).

Method according to one of the preceding claims, characterized in that the introduction of the carbon-rich substance (1 12) and the self-gasification material (1 13) in the vertical shaft (1 10) individually and / or as a mixture via a moving or static solids distribution ( 1 16) takes place, via which a targeted distribution of the materials as a function of their different particle sizes in the bulk material moving bed (1 10).

Method according to one of the preceding claims, characterized in that the lower end of the upper Schüttgutzone (1 14) has a smaller inner diameter than the upper end of the lower Schüttgutzone (1 15).

Method according to one of the preceding claims, characterized in that the vertical shaft (100) in the region of the upper Schüttgutzone (1 14) and / or in the region of the lower Schüttgutzone (1 15) is completely or partially conical, wherein the inner diameter in the conical areas increases from top to bottom.

Method according to one of the preceding claims, characterized in that in the central region (104) of the vertical shaft (100) at least over part of the circumference of the bulk material moving bed one or more radial mixing chambers (105) are formed, in which the proportions of the synthesis gas (130) from the lower Schüttgutzone (1 15) with the proportions of the synthesis gas from the upper Schüttgutzone (1 14) are mixed.

9. The method according to claim 8, characterized in that for the formation of the mixing chambers (105) one or more Abböschungen the bulk material moving bed (1 10) are generated, wherein the bulk material moving bed (1 10) in the central region (104) of the vertical shaft (100 ) to ensure a necessary for the production of Abböschungen fluidized bed behavior to form a suitable slope angle at least 50% by weight of the self-gasification material (1 13) contains. 10. The method according to any one of the preceding claims, characterized in that the temperature of the synthesis gas (130) at the removal point (131) is between 600 ° C and 1300 ° C.

1 1. A method according to any one of the preceding claims, characterized in that the material is not self-gasifiable (1 13) of the bulk material moving bed (1 10) lime material in a proportion of 10% to 100%, wherein the lime material is preferably

Quicklime and / or limestone.

12. The method according to any one of the preceding claims, characterized in that at the upper end of the upper Schüttgutzone (1 14) a gas space (103) in the vertical shaft (100) is formed in which an overheated gas formed by oxidative processes, and / or in an overheated gas is introduced.

13. The method according to any one of the preceding claims, characterized in that a firing and / or an introduction of superheated gas in the bulk material moving bed (1 10), in the region of the oxidation zone (143) and / or in the region of the pyrolysis zone (141) using Insertion lances (106, 107) takes place. 14. The method according to any one of the preceding claims, characterized in that in the region of the pyrolysis zone (141) is a heating by adding hot self not gasifiable material (1 13) as part of the bulk material (1 1 1), wherein the hot itself is not gasifiable material has an inherent temperature of more than 450 ° C and is preferably provided by industrial processes.

15. The method according to any one of the preceding claims, characterized in that water (40) and / or steam (70) in the bulk material moving bed (1 10) for hydration of lime material as part of the bulk material (1 1 1) and utilization of the released process heat be added.

16. The method according to any one of the preceding claims, characterized in that carbon dioxide-containing gas in the bulk material moving bed (1 10) for the carbonization of lime material as part of the bulk material (1 1 1) and utilization of the process heat released thereby added and / or by adding air ( 50) or oxygen-containing gas (90) is formed by oxidation.

17. The method according to any one of the preceding claims, characterized in that on a lower side (102) of the vertical shaft (100) for forming a Nachkühlzone (144), a cooling gas is introduced.

18. Method according to claim 17, characterized in that the cooling gas introduced at the lower side (102) of the vertical shaft (100) contains the synthesis gas (130) and / or contains at least one combustible gas (60) or alternatively contains air (50).

19. The method according to claim 17, characterized in that on the underside (102) of the vertical shaft (100) introduced cooling gas includes a mixture of reducible gas and air.

20. The method according to any one of the preceding claims, characterized in that the bulk material moving bed (1 10) pure oxygen or a gas mixture is added with air enriched oxygen content.

21. The method according to any one of the preceding claims, characterized in that as high-carbon substances (1 12) at least partially plastic waste and / or organic waste are used.

22. The method according to any one of the preceding claims, characterized by the use of high boilers (109) as carbon-rich substances (1 12), wherein the high boilers preferably in liquid form preferably by means of insertion lances (106, 107) in the region of the pyrolysis zone (141) and / or reduction zone (142) and / or oxidation zone (143) introduced directly into the bulk material moving bed (1 10), and / or via the gas space (103) at the upper end of the upper Schüttgutzone in the bulk material moving bed dosed, and / or directly the bulk material (1 1 1) before entering the vertical shaft (100) are added.

23. The method according to any one of the preceding claims, characterized in that are used as high-carbon substances (1 12) at least partially phosphorus-containing sewage sludge.

24. The method according to any one of the preceding claims, characterized in that as carbon-rich substance (1 12) at least partially aluminum-containing residues and / or aluminum-containing wastes are used.

25. The method according to any one of the preceding claims, characterized in that in the high-carbon substances (1 12) existing metal components and / or other valuable substances are chemically or physically recovered from the discharged bulk material.

26. The method according to any one of the preceding claims, characterized in that the bulk material moving bed (1 10) at least partially passes through the vertical shaft (100) several times in the circulation.

27. The method according to any one of the preceding claims, characterized in that at the removal point (131) from the bulk material moving bed (1 10) withdrawn synthesis gas (130) is subsequently passed through a Nebenschüttgutwanderbett (220) comprising a Nebenschüttgutmaterial (221) with a Contains at least 10% to a proportion of 100% of alkaline materials.

28. The method according to claim 27, characterized in that the Nebenschüttgutwanderbett (220) in a secondary shaft (210) of the vertical shaft furnace (1) in countercurrent to the synthesis gas (130) is guided, wherein the secondary shaft (210) of the vertical shaft furnace (1) of the vertical shaft (100) of the vertical shaft furnace (1) is arranged separately.

29. The method according to any one of claims 27 to 28, characterized in that the synthesis gas (130) in a central region (218) of the secondary shaft (210) is fed and in an upper portion (214) of the secondary shaft (210) or on a Top side (21 1) of the secondary shaft (210) is deducted.

30. The method according to claim 27, characterized in that the Nebenschüttgutwan- derbett (320) in a secondary shaft (310) of the vertical shaft furnace (1) is guided in cocurrent to the synthesis gas (130), wherein the secondary shaft (310) of the vertical shaft furnace (1 ) is arranged separately from the vertical shaft (100) of the vertical shaft furnace (1).

31. The method according to claims 27 and 30, characterized in that the synthesis gas (130) in the upper region of the secondary shaft (31 1) is fed and in the lower region (315) of the secondary shaft (310) is withdrawn.

32. Method according to claim 27, characterized in that the secondary bulk material (221) is discharged uncooled from the secondary shaft (210) in a lower region (215) of the secondary shaft (210) or by means of a heat exchanger ( 20) is cooled.

33. The method according to any one of the preceding claims 27 to 32, characterized in that the Nebenschüttgutmaterial (221) in a lower portion (215) of the secondary shaft (210) uncooled from the secondary shaft (210) removed and at least partially as a hot non-gasifiable material ( 1 13) in the vertical shaft (100) is used and the heat energy contained in the pyrolysis zone (141) is used.

34. Method according to claim 27, characterized in that the secondary bulk material moving bed (220) below the middle region (218) of the secondary shaft (210) in the lower region (215) of the secondary shaft (210) is introduced by countercurrent flow Cooling gas is cooled and / or the Nebenschüttgutwanderbett (220) in the lower portion (215) of the secondary shaft (210) by a heat exchanger (20) is cooled.

35. The method according to any one of claims 27 to 34, characterized in that the average grain size of the bulk material moving bed (1 10) is greater than the mean grain size of the secondary bulk material moving bed (220).

36. The method according to any one of claims 27 to 35, characterized in that the mean grain size of the bulk material (1 1 1) and the average grain size of the Nebengutgutgutmaterials (221) in the range of 5 mm to 30 cm, preferably in the range of mm to 15 cm or the mean grain size of the bulk material (1 1 1) is over 1 cm and the mean grain size of Nebenschüttgutmaterials (221) is less than 10 cm.

37. The method according to any one of claims 27 to 36, characterized in that water (40) and / or steam (70) at one or more positions of the bulk material moving bed (1 10) and / or the Nebenschüttgutwanderbett (220) are added.

38. vertical shaft furnace (1) for performing the method according to one of the preceding claims comprising a vertical shaft (100) with a in the vertical shaft (100) extending continuously or at intervals Schüttgutwanderbett (1 10), comprising a bulk material (1 1 1) from a High-carbon substance (1 12) and a self-gasifiable material (1 13), characterized in that the vertical shaft (100) in a central region (104) has a removal point (131) for the synthesis gas.

39. Vertical shaft furnace (1) according to claim 38, characterized in that the bulk material (1 1 1) before and / or after entry into the vertical shaft (100) can be mixed by a mixing device.

40. vertical shaft furnace (1) according to any one of claims 38 to 39, characterized in that a lower end of an upper Schüttgutzone (1 14) of the vertical shaft (1 10) has a smaller inner diameter than an upper end of a lower Schüttgutzone (1 15) of the vertical shaft (1 10).

41. vertical shaft furnace (1) according to one of claims 38 to 40, characterized in that the vertical shaft (100) in the region of the upper Schüttgutzone (1 14) and / or in the region of the lower Schüttgutzone (1 15) is wholly or partly conical ,

42. vertical shaft furnace (1) according to one of claims 38 to 41, characterized in that in the central region (104) of the vertical shaft (100) at least over part of the circumference of the bulk material moving bed (1 10) one or more radial mixing chambers (105) are formed.

43. vertical shaft furnace (1) according to claim 42, characterized in that the bulk material moving bed (1 10) in the region of the mixing chambers (105) has one or more Abböschun- conditions.

44. vertical shaft furnace (1) according to one of claims 38 to 43, characterized in that the vertical shaft furnace (1) (1) of the vertical shaft (1 10) arranged separately secondary shaft (210) and between the secondary shaft (210) and the Vertical shaft (1 10) has a flow connection.

45. Use of the synthesis gas (130) produced by a method according to any one of claims 1 to 37 as a fuel gas for mobility purposes, for thermal utilization and / or as fuel gas for power generation and / or as raw material in chemical processes. 46. Use of the synthesis gas (130) according to claim 45, characterized in that the synthesis gas (130) is filtered prior to its utilization.