EP3580312B1 - Preparation de syntheseges a partir de substances carbones au moyen d'une procedure combiné co-courant et contre-courant - Google Patents

Preparation de syntheseges a partir de substances carbones au moyen d'une procedure combiné co-courant et contre-courant Download PDF

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EP3580312B1
EP3580312B1 EP18704520.8A EP18704520A EP3580312B1 EP 3580312 B1 EP3580312 B1 EP 3580312B1 EP 18704520 A EP18704520 A EP 18704520A EP 3580312 B1 EP3580312 B1 EP 3580312B1
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Prior art keywords
bulk material
zone
moving bed
gas
vertical shaft
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EP18704520.8A
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German (de)
English (en)
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EP3580312A1 (fr
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Leonhard Baumann
Roland Möller
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Ecoloop GmbH
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Ecoloop GmbH
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime

Definitions

  • the invention relates to a method for producing synthesis gas from carbon-rich substances using a vertical shaft furnace with a bulk material moving bed
  • Processes for the production of synthesis gas are known and are carried out in countercurrent gasifiers or in multi-stage gasifiers.
  • the flow rate of the synthesis gas which is principally taken from an upper end of the countercurrent gasifier, is very high because the entire amount of synthesis gas produced is passed through the pyrolysis zone located in the upper shaft area due to the process.
  • this flow speed there is a risk that plastics will be carried away by the countercurrent flow at the upper end of the countercurrent gasifier with the emerging synthesis gas before they can enter the bed of the moving bed. This can lead to uncontrolled pyrolysis of plastic particles in the raw gas system and in downstream parts of the system, as a result of which insufficiently split plastic particles bake into lumps.
  • 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 possibility of using plastics in the process that have a low melting point.
  • DE 10 2012 014 161 A1 describes a method with two vertical process rooms, in which a carbon-rich substance located in a moving bed running from top to bottom is gasified in countercurrent with oxygen-containing gas and is post-gasified in a second vertical process room using oxygen-containing gas.
  • the pre-gassed synthesis gas produced in the first vertical process space flows out at the top of the first vertical process space.
  • the synthesis gas then 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 region of the second vertical process space.
  • WO 2005/047435 discloses a method for the production of combustible fuels from the gasification of organic starting materials in a gasification plant.
  • the object of the present invention is therefore to provide an improved method for producing synthesis gas with which a high gas quality is achieved and, moreover, both the energy consumption and the technical effort are kept low.
  • the invention relates to a method for producing synthesis gas from carbon-rich substances, wherein a bulk moving bed consists of a bulk material that is composed of the carbon-rich substances and a non-gasifiable material and wherein the bulk moving bed is in a vertical shaft of a vertical shaft furnace moves continuously or at intervals from top to bottom and is flowed through by gas, whereby the non-gasifiable material and residues of the carbon-rich substances are discharged on the underside of the vertical shaft, in which the bulk material moving bed through which the gas flows to generate components of the synthesis gas at least one pyrolysis zone and a reduction zone are formed in which reaction products are reduced from an oxidation zone also formed in the bulk material moving bed, the synthesis gas in a mi
  • the inner area of the vertical shaft is withdrawn at a removal point between an upper bulk material zone and a lower bulk material zone and the carbon-rich substances are at least partially removed with the bulk
  • the provision of the upper bulk solids zone and the lower bulk solids zone and the removal of the synthesis gas in the middle area between the upper bulk solids zone and the lower bulk solids zone is advantageous, since in this way at least two process zones can be formed, in which those with the bulk solids from the upper to the lower Bulk zone running carbon-rich substances are processable.
  • Another advantage is that synthesis gases that arise in the pyrolysis zone can be directed 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 that have not yet passed through any of the process zones. This effectively prevents incomplete pyrolysis of the carbon-rich substances at the shaft inlet by hot synthesis gases.
  • the synthesis gas is essentially composed of the products of the largely complete pyrolysis and the reduction due to this arrangement of the bulk material zones, the extraction point in the middle area and the gas streams that form.
  • the oxidation is preferably carried out at an energy level which is insufficient to melt or decompose the material which itself cannot be gasified.
  • the non-gasifiable material has the task of acting as a transport material, to ensure homogeneous gas permeability through its gap volume and to transport heat between the process zones.
  • material can preferably be used as the carbon-rich material.
  • a plastic and a mineral component form a eutectic.
  • a pelletized material migrates intact into the oxidation zone with the non-gasifiable material due to its high thermal stability.
  • the void volume in the bulk material moving bed is largely preserved.
  • 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.
  • the material, which itself cannot be gasified can take on a comminution function for the carbon-rich substances due to high shear forces in the bulk material moving bed.
  • a suitable material that cannot itself be gasified it is possible to bind certain pollutants from the synthesis gas.
  • 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.
  • synthesis gas By partially generating synthesis gas in a pyrolysis zone located in the upper area of the moving bulk material bed and in a reduction zone located in the lower area of the moving bulk material bed, two processes can advantageously be set separately from one another in order to produce a high quality synthesis gas.
  • the synthesis gas can be proportionally different both in terms of the type of components and in terms of the proportions within the synthesis gas in the upper region and in the lower region.
  • coke produced in the pyrolysis zone is preferably used for the reduction of carbon dioxide produced in the oxidation zone (Boudouard equilibrium).
  • the thermal energy required for this reaction is provided by the oxidation zone located in the vertical shaft below the reduction zone.
  • carbon monoxide is advantageously formed, which contributes as an energy carrier to the calorific value of the synthesis gas, or as a chemical component in the case of material utilization of the synthesis gas.
  • the upper bulk material zone is flowed through in cocurrent and the lower bulk material zone in countercurrent.
  • the non-gasifiable material itself has a weight proportion of at least 20% of the total bulk material before it is heated in the upper bulk material zone and is heated by heated gas to an intrinsic temperature of at least 350 ° C in the upper bulk material zone. This creates an energy buffer provided to compensate for the endothermic pyrolysis reaction and to ensure a complete thermal breakdown of the carbon-rich substances.
  • the method is particularly advantageous when the carbon-rich substance and the non-gasifiable material are in front of and / or by means of one or more rotating systems, preferably by parallel filling of a rotating tub and / or by common and / or parallel metering via one or more rotating chutes are mixed with one another after entering the vertical shaft.
  • Such a mixing can be achieved particularly effectively, for example, with a rotating bucket which is filled with the two different materials in parallel during its own rotation. It is particularly advantageous that both the different constituents of the bulk material are statistically homogeneously distributed in the bulk material, and a homogeneous distribution of particles of different sizes within the bulk material is also achieved.
  • the rotating bucket is preferably transported up to the feed area of the vertical shaft furnace with a bucket elevator.
  • the bucket can then be fed to the upper end of the vertical shaft, where the contents of the bucket are then fed into the vertical shaft. In this way it can be ensured that the contents of the bucket do not separate or sort or fractionate during the feeding process.
  • Another advantage of this type of feed is that the composition of the bucket contents can be changed for each bucket. This allows the process to be controlled via the material added via the pails.
  • a further preferred embodiment of the method provides that the carbon-rich substance and the non-gasifiable material are individually introduced into the vertical shaft at alternating intervals, resulting in a layered arrangement of the materials in the bulk material moving bed before it migrates from top to bottom through the vertical shaft .
  • the two materials do not need to be mixed.
  • a layer-by-layer and thus inhomogeneous arrangement is formed in the vertical shaft, but the layer heights can be kept very low.
  • the relatively high expansion of the bulk material moving bed results in a level of homogeneity that is suitable and sufficient for the process, which allows the chemical and thermal processes that are important in the vertical shaft to be implemented well.
  • Another embodiment of the method is preferred in which the introduction of the carbon-rich substance and the non-gasifiable material into the vertical shaft takes place individually and / or as a mixture via a moving or static solids distributor, via which a targeted distribution of the materials depending on their different Grain sizes in the bulk material moving bed is made possible.
  • a distribution control is advantageous when one or both of the introduced materials have different grain sizes.
  • the method can be designed particularly advantageously if an inner diameter at the lower end of the upper bulk material zone is smaller than an inner diameter at the upper end of the lower bulk material zone. This takes into account the different amounts of synthesis gas. In the upper bulk material zone, a smaller amount of synthesis gas is formed by pyrolysis than by the gasification reactions in the oxidation and reduction zone in the lower bulk material zone. By adapting the inner diameter, the pressure losses can be kept low even with different gas generation quantities in the upper and lower bulk material zones. In this way, excessive entrainment of particles in the middle area of the vertical shaft at the extraction point can be counteracted.
  • a further preferred embodiment of the method consists in that the vertical shaft in the area of the upper bulk material zone and / or in the area of the lower bulk material zone is completely or partially conical, with an inner diameter in the conical areas increasing from top to bottom.
  • the process temperatures which increase steadily from top to bottom to the oxidation zone, are taken into account, with which the solid particles of the bulk material expand.
  • the conical design of the vertical shaft counteracts any canting or even bridging that may result from this, which can lead to an inhomogeneous and uncontrolled migration of the bulk material moving bed.
  • a preferred development provides that one or more radial mixing chambers are formed in the middle area of the vertical shaft at least over part of the circumference of the bulk material moving bed, in which the proportions of the synthesis gas from the lower The bulk material zone is mixed with the proportions of the synthesis gas from the upper bulk material zone.
  • the proportions of the synthesis gas that originate from the lower area of the moving bulk material bed and have a comparatively high temperature due to the process can be combined in a particularly advantageous manner with the proportions of synthesis gas that originate from the upper area of the moving bulk material bed and due to the process have a comparatively low temperature, mix. This also results in an advantageously homogeneous synthesis gas with a mixed temperature that is sufficiently high for complete thermal splitting.
  • the mixing chambers can particularly advantageously be created by one or more slopes of the bulk material moving bed, the bulk material moving bed in the middle area of the vertical shaft to ensure the fluid bed behavior necessary for creating the slopes to form a suitable angle of slope contains at least 50% by weight of the non-gasifiable material itself.
  • Such slopes create an enlarged outflow area, as a result of which the flow velocity at the outlet of the synthesis gas is kept comparatively low. In this way, the entrainment of solid particles is counteracted. Furthermore, the movement of the slopes with the total flow of the bulk material moving bed from top to bottom prevents the outflow surface from becoming clogged with dust particles or from being blocked asymmetrically.
  • the temperature of the synthesis gas at the extraction 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. Provided the temperature is kept above the lower limit of the specified range, carbon-rich substances are largely completely pyrolysed. This is ensured in particular by the fact that the comparatively hot synthesis gas from the lower bulk material zone, through mixing with the comparatively colder synthesis gas from the upper bulk material zone, forms a mixed temperature that is sufficiently high to ensure complete thermal splitting of longer-chain components such as oils or tars in the To ensure syngas.
  • the mass ratio is between the carbon-rich substances and the non-gasifiable material, e.g. a lime material, in the range of 4: 1 to 1: 2.
  • This mass ratio ensures that the processes in the process zones run ideally with regard to the heat transport occurring through the bulk material moving bed and the heat required for the endothermic reactions.
  • the heat requirement or the heat released in the process zones and its 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 non-gasifiable material of the bulk material moving bed contains the lime material in a proportion of 10% to 100%, the lime material preferably consisting of quicklime and / or limestone.
  • Lime materials and especially quicklime have a positive influence on the energy requirements of the process.
  • Quicklime i.e. CaO or calcium oxide
  • the hydration is exothermic, as a result of which energy is advantageously available in the form of heat for the endothermic processes in the vertical shaft furnace.
  • the slaked form of quicklime that is slaked lime
  • slaked lime is to be used in an advantageous manner, since slaked lime binds halogens such as chlorine or bromine and also sulfur in the form of thermally largely stable salts. This is advantageous in terms of the quality of the synthesis gas.
  • halogen-rich substances are materials that contain polyvinyl chloride or bromine-containing flame retardants, with vulcanized rubber or oil sands or oil shale being suitable as sulfur-rich substances.
  • a gas space is formed in the vertical shaft at the upper end of the upper bulk material zone, in which an overheated gas is formed by oxidative processes and / or into which an overheated gas is introduced.
  • Such a gas space ensures that the overheated gas enters the bulk material moving bed homogeneously due to the prevailing overpressure, which results among other things from the pressure loss in 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 this results in an optimal utilization of the upper bulk material zone with a maximum residence time of the carbon-rich substances in hot reaction areas.
  • a further preferred development provides that additional firing and / or introduction of superheated gas in the bulk material moving bed, in the area of the oxidation zone and / or in the area of the pyrolysis zone takes place using plug-in lances.
  • the addition or introduction of superheated gas in the areas of the pyrolysis zone and the oxidation zone is advantageous since the pyrolysis temperature and the oxidation temperature can be adjusted in this way. In this way, a largely complete pyrolysis and oxidation of the carbon-rich substance can be achieved.
  • the additional firing or the introduction of overheated gas can be flexibly adjusted, which is advantageous since the complete pyrolysis and / or oxidation can not only be set via the traveling speed of the bulk material moving bed, but also via the material flows for the plug-in lances.
  • the position of the process zones in the furnace can preferably also be adjusted by means of an adjustable additional fire via the plug-in lances.
  • heating takes place in the area of the pyrolysis zone by adding hot, even non-gasifiable, material as part of the bulk material, the hot, non-gasifiable material having an intrinsic temperature of more than 450 ° C and preferably industrial Processes is provided.
  • the material which cannot itself be gasified here preferably has a temperature of over 450 ° C., the mass ratio of the material which cannot itself be gasified to the carbon-rich substance being approximately 3: 1.
  • the setting of the process temperature is done largely separately from the setting of the process temperature in the oxidation zone or in the reduction zone.
  • the energy input in the individual process zones can be controlled in an advantageous manner at a constant migration speed of the bulk material moving bed.
  • Hot solids flows from industrial processes, for example cement clinker can preferably also be used as hot materials that cannot themselves be gasified.
  • the hot non-gasifiable material can be a product of pig iron manufacture.
  • water and / or water vapor are added to the moving bulk bed for hydration of lime material as a component of the bulk material and utilizing the process heat released in the process.
  • the additional heat energy released from hydration enables endothermic processes in the pyrolysis zone and in the reduction zone to be supplied with energy by the exothermic hydration reaction.
  • the homogeneous water-gas shift reaction can take place in the process space through the introduction of water vapor, with carbon monoxide acting as a reducing agent for the water vapor to form carbon dioxide and hydrogen.
  • the heterogeneous water-gas reaction is also promoted, with water vapor reacting with pyrolysis coke to form carbon monoxide and hydrogen.
  • Another embodiment provides that carbon dioxide-containing gas is added to the moving bulk bed for carbonization of lime material as part of the bulk material and utilizing the process heat released and / or is formed by adding air or oxygen-containing gas by oxidation.
  • a cooling gas is introduced on an underside of the vertical shaft to form a post-cooling zone.
  • cooling gas on the underside of the vertical shaft is advantageous because the cooling gas can at least partially absorb the residual heat of the bulk material moving bed in the post-cooling zone and, as the cooling gas rises, transports it into the upper areas of the vertical shaft, in which endothermic reactions sometimes take place.
  • the cooling gas introduced on the underside of the vertical shaft contains the synthesis gas and / or contains or contains at least one combustible gas alternatively contains air.
  • the cooling gas introduced on the underside of the vertical shaft contains a mixture of reducible gas and air.
  • synthesis gas is provided for the cooling gas
  • the bulk material moving bed is advantageously cooled without the cooling gas negatively influencing the quality of the synthesis gas produced. Rather, any proportions of carbon dioxide contained in the synthesis gas used can at least partially be reduced to carbon monoxide in the reduction zone by reaction with the pyrolysis coke and thus the synthesis gas quality overall can be improved.
  • Providing a flammable gas, which is preferably natural gas, has the advantage that the flammable gas can absorb the heat from the moving bulk material bed located in the post-cooling zone, while at the same time the targeted dosage of the natural gas increases the calorific value of the synthesis gas produced. can be adjusted.
  • 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
  • this gas largely does not take part in the processes taking place in the oxidation zone.
  • the heat conducted by the reducible gas from the after-cooling zone into the reduction zone can be used at least in part during the reduction of the reducible gas.
  • carbon dioxide is reduced to carbon monoxide by the pyrolysis coke after the Boudouard reaction.
  • 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 is used completely for the oxidation of oxidizable gases and / or other oxidizable products of the pyrolysis zone, preferably pyrolysis coke can be.
  • the processes in the oxidation zone ideally run stoichiometrically based on the pyrolysis coke still present in the oxidation zone, so that the synthesis gas that is withdrawn at the extraction point preferably does not contain any oxygen and no carbon-containing substances with the moving bed get down from the oxidation zone.
  • cooling gas introduced on the underside of the vertical shaft consists of one or more gas flows from industrial Processes, preferably from combustion and / or calcining processes or gases from pig iron production, preferably furnace gas and / or coke gas and / or town gas.
  • the process can be combined particularly efficiently with existing industrial processes.
  • a particularly efficient linking of existing gas networks with the present method can be realized, where, for example, 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. This enables the furnace gas to be used and refined at the same time, while less nitrogen is introduced into the process compared to the use of air as a cooling gas.
  • pure oxygen or a gas mixture with a proportion of oxygen enriched in relation to air is added to the moving bulk material bed.
  • the addition of pure oxygen or a gas mixture with a proportion of oxygen that is enriched compared to air has the advantage that the gas load of gases not participating in the reactions, such as nitrogen, contained in the synthesis gas is reduced. In this way, the calorific value of the synthesis gas is increased.
  • the pure oxygen or the gas mixture with a proportion of oxygen enriched compared to air is preferably added directly by means of plug-in lances in the area of the oxidation zone and / or in the area of the pyrolysis zone, while synthesis gas and / or combustible gases and / or reducible gases are preferably added as cooling gas on the underside of the vertical shaft will.
  • At least some of the carbon-rich substances used are plastic waste and / or organic waste.
  • Plastic waste and / or organic waste occur in large quantities and, due to their high carbon content, have a suitable calorific value for the processes taking place in the process.
  • impure plastic waste such as composite materials, plastic-containing waste fractions, shredder fractions from scrap recycling, plastic-containing production residues and the like, can preferably be processed into synthesis gas by the method.
  • This also applies to mixed materials rich in hydrocarbons, such as tar sands, oil shale or other media mixed with hydrocarbons.
  • the production of synthesis gas takes place in a first stage by thermal cleavage of the organic components Pyrolysis gas with the formation of pyrolysis coke.
  • the pyrolysis coke reacts in a second stage by reducing carbon dioxide to carbon monoxide. Furthermore, the pyrolysis coke forms additional carbon monoxide and hydrogen with the water vapor contained in the process through the heterogeneous water gas reaction. In a third stage, the pyrolysis coke constituents still present are almost completely oxidized in the oxidation zone.
  • the oxidation zone is generally referred to as the reaction front in fixed or moving bed gasifiers. Any pollutants contained in the synthesis gas can preferably be bound to the moving bulk material bed by attachment reactions. Non-gasifiable components of the plastic waste and in particular the impure plastic waste, such as metals and rare earths, remain in the bulk material moving bed and can be processed by downstream processes or can be recycled.
  • a further embodiment provides 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.
  • high boilers can also be gasified down to their non-gasifiable components in the process with the vertical shaft furnace. It is particularly advantageous if the high boilers are introduced directly into the bulk material moving bed by means of plug-in lances in the area of the pyrolysis zone and / or the reduction zone and / or the oxidation zone and / or dosed and / or dosed into the bulk material moving bed via the gas space at the upper end of the upper bulk material zone are added directly to the bulk material before entry into the vertical shaft.
  • sewage sludge containing phosphorus is at least partially used as carbon-rich substances.
  • the high organic content of the sewage sludge can advantageously be converted into synthesis gas.
  • the residual products of pyrolysis and oxidation contain ash enriched with phosphorus. This ash can be used advantageously as fertilizer or processed into fertilizer.
  • the use of lime materials as bulk material moving bed is particularly advantageous, since in this way the material discharged from the vertical shaft can at least partially be used as a combined lime / phosphorus fertilizer.
  • Another preferred embodiment variant of the method provides that at least partially aluminum-containing residues and / or aluminum-containing waste are used as the carbon-rich substance.
  • the use of aluminum as a component of the carbon-rich substance leads to the fact that aluminum reacts to aluminum hydroxide and hydrogen, especially when water vapor is present in the pyrolysis zone and the reduction zone, with a strong release of heat energy.
  • the synthesis gas yield and the hydrogen content in the synthesis gas can be increased significantly.
  • the heat energy released is available to compensate for the endothermic reactions in the pyrolysis zone and in the reduction zone.
  • the aluminum hydroxide is largely oxidized in the oxidation zone to aluminum oxide, which can optionally be recovered from the moving bulk bed. Due to the almost complete oxidation of the aluminum, if the ashes are dumped from the bulk material moving bed, there is no further potential for hydrogen formation, which avoids problems with the undesired hydrogen development in the case of the so-called flushing backfill as possible underground disposal.
  • metal components present in the carbon-rich substances as e.g. can be found in large proportions in the case of electronic scrap and / or other valuable materials, such as aluminum, halogens or phosphorus, are chemically or physically recovered from the discharged bulk material.
  • metal components or valuable materials that were not gasified in the process can be recycled.
  • the enriched residual materials can be processed, for example, in wet chemical processes, which is particularly true for rare earths. Alternatively, the enriched residual materials can be recycled directly.
  • the bulk material moving bed at least partially circulates through the vertical shaft several times.
  • residual materials are, for example, ash, metals or minerals.
  • the accumulated residual materials can then be sorted, processed if necessary and sent for recycling.
  • the synthesis gas withdrawn from the bulk material moving bed at the extraction point is subsequently passed through a secondary bulk material moving bed which contains a secondary bulk material with a proportion of at least 10% up to a proportion of 100% alkaline materials.
  • synthesis gas withdrawn at the extraction point is passed through a secondary moving bulk material bed, since any aerosols, tar or other solid constituents carried along by the synthesis gas are retained in this secondary bulk material moving bed. In this way the synthesis gas is cleaned.
  • the secondary moving bed of bulk material is guided in a secondary shaft of the vertical shaft furnace in countercurrent to the synthesis gas, the secondary shaft of the vertical shaft furnace being arranged separately from the vertical shaft of the vertical shaft furnace.
  • the aftertreatment of the synthesis gas is advantageously decoupled from the process zones of the vertical shaft.
  • Any constituents or elements of the synthesis gas removed from the synthesis gas by the secondary bulk material moving bed can advantageously be bound in the secondary bulk material moving bed and disposed of or post-treated separately from the bulk material moving bed. Guiding the gas flow in countercurrent to the fixed bed also has the advantage of an effective heat exchange.
  • the synthesis gas is fed in in a central region of the secondary shaft and is drawn off in an upper region of the secondary shaft or on an upper side of the secondary shaft.
  • a further embodiment of the synthesis gas cleaning in the secondary shaft provides that the secondary bulk material moving bed 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 preferably being arranged separately from the vertical shaft of the vertical shaft furnace.
  • This refinement of the method allows a greatly simplified structural implementation, because the synthesis gas can simply be introduced at the upper end of the secondary shaft, for example via a cavity formed. This ensures a homogeneous flow into the secondary bulk material. In the case of a countercurrent flow, the structurally more complex gas flow into a central area of the secondary shaft can be dispensed with.
  • the synthesis gas is fed in in the upper region of the secondary shaft and is drawn off in the lower region of the secondary shaft. This results in a mixed temperature of the secondary bulk material and the synthesis gas at the lower end of the secondary shaft.
  • the secondary bulk material is cooled by means of a heat exchanger.
  • a heat exchanger in particular in the lower area of the auxiliary shaft, has the advantage that the heat given off by the synthesis gas to the moving bed of auxiliary bulk material can be transferred to a heat exchange medium which gives off the heat again at suitable points in the vertical shaft furnace. This is preferably done in the pyrolysis zone, or between the oxidation zone and the reduction zone by means of plug-in lances.
  • the heat exchanger medium is preferably a medium that can be used in the processes taking place in the vertical shaft.
  • the heat exchange medium is preferably a combustible gas, water, steam or synthesis gas.
  • the secondary bulk material in the lower area of the secondary shaft is discharged from the secondary shaft without being cooled.
  • the uncooled discharge of the secondary bulk material results in the advantage that the secondary bulk material which has been heated by the synthesis gas is available as input material for further processes.
  • the heating of the secondary bulk material is advantageous if thermal energy is required for the connection processes.
  • Another advantageous embodiment provides that the secondary bulk material in a lower area of the secondary shaft is removed uncooled from the secondary shaft and at least partially used as hot non-gasifiable material in the vertical shaft and the thermal energy contained is used in the pyrolysis zone.
  • the use of the secondary bulk material as hot, non-gasifiable material in the vertical shaft enables the thermal energy contained in the synthesis gas to be efficiently used for the endothermic processes in the pyrolysis and reduction zone.
  • the efficiency is achieved in particular through the almost ideal heat exchange between the hot synthesis gas and the secondary bulk material in the secondary shaft. With this procedure, the efficiency of the process can be significantly increased, since a considerable part of the heat content of the hot synthesis gas is not lost, but is returned to the vertical shaft.
  • the secondary bulk material moving bed is cooled below the middle area of the secondary shaft in the lower area of the secondary shaft by cooling gas introduced in countercurrent and / or the secondary bulk material moving bed in the lower area of the secondary shaft is cooled by a heat exchanger.
  • the cooling gas can be synthesis gas or a combustible gas.
  • the mean grain size of the bulk material moving bed is larger than the mean grain size of the secondary bulk material moving bed.
  • the Secondary bulk material moving bed can better filter the synthesis gas due to its larger effective surface.
  • both solid and gaseous impurities of the synthesis gas which are not retained by the moving bulk material bed are advantageously filtered or absorbed by the secondary bulk material moving bed.
  • the mean grain size of the bulk material and the mean grain size of the secondary bulk material are in the range from 5 mm to 30 cm, preferably in the range from 5 mm to 15 cm, or the mean grain size of the bulk material is over 1 cm and the mean grain size of the secondary bulk material is less than 10 cm.
  • a preferred development provides that water and / or water vapor are added to the moving bulk bed and / or the auxiliary moving bed at one or more positions.
  • Water and / or water vapor is preferably added as a cooling medium in the upper region of the secondary moving bed and / or in the lower region of the moving bulk bed.
  • the advantage of adding water or steam to the pyrolysis zone is that the moving bulk bed can be specifically hydrated until it reaches its own temperature of approx. 450 ° C, provided the moving bulk bed consists of calcium oxide. The hydration is exothermic and can therefore provide the necessary heat energy for the pyrolysis of the carbon-containing substances.
  • the calcium hydroxide which is at least partially formed is suitable for binding halogens or sulfur in the form of salts that are largely thermally stable.
  • the synthesis gas is cleaned of halogens and / or sulfur, which are released during the pyrolysis or oxidation of, for example, polyvinyl chlorides or vulcanized rubber.
  • the water gas shift reaction in the bulk material moving bed reduces the water vapor with the formation of carbon dioxide to hydrogen using the carbon monoxide as a reducing agent. This creates the stable carbon dioxide and the hydrogen, which is required in the synthesis gas for certain subsequent applications.
  • the carbon dioxide can preferably be reduced to carbon monoxide by the Boudouard equilibrium through the carbon present in the pyrolysis coke.
  • the reduction of carbon dioxide to carbon monoxide results in the advantage that the synthesis gas contains a reactive gas and the load of largely passive gases is reduced.
  • the method can be carried out in a vertical shaft furnace having a vertical shaft with a bulk material moving bed running continuously or at intervals in the vertical shaft, comprising a bulk material made of a carbon-rich substance and a material which itself cannot be gasified, the vertical shaft having an extraction point for the synthesis gas in a central area will.
  • the vertical shaft has an extraction point in a central area, several process zones can advantageously be formed in the vertical shaft, which are separated from one another by the extraction point. So an upper area and a lower area are formed.
  • the vertical shaft furnace provides separate process rooms in which processes can be carried out separately from one another. This is particularly advantageous when the requirements for the processes are different in terms of parameters such as temperature, pressure and / or stoichiometry.
  • the vertical shaft furnace provides that the bulk material can be mixed by a mixing device before and / or after entering the vertical shaft.
  • a mixing device before and / or after entering the vertical shaft.
  • the carbon-rich substance and the non-gasifiable material by means of one or more rotating systems, preferably by parallel filling of a rotating tub and / or by common and / or parallel metering via one or more rotating chutes in front of and / or can be mixed with one another after entering the vertical shaft.
  • the provision of a mixing device advantageously ensures that the bulk material of the bulk moving bed is homogeneous.
  • the carbon-rich substance and the material which itself cannot be gasified can be introduced into the vertical shaft individually at alternating intervals.
  • the composition of the bulk material moving bed can be adjusted in a controlled manner. Because the components can be introduced individually at alternating intervals, the vertical shaft furnace can be operated in different modes. It is preferably provided that, by means of a static solids distributor, a targeted distribution of the materials of the bulk material moving bed can be achieved depending on their different grain sizes. A targeted distribution of the materials as a function of the grain size can be used to influence the setting of the angle of repose in the bulk material moving bed.
  • a lower end of an upper bulk material zone of the vertical shaft has a smaller inner diameter than an upper end of a lower bulk material zone of the vertical shaft.
  • a further advantageous embodiment of the vertical shaft furnace provides that the vertical shaft is completely or partially conical in the area of the upper bulk material zone and / or in the area of the lower bulk material zone.
  • the inner diameter preferably increases from top to bottom in the conical regions.
  • a conical shape of the areas results in 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 cant with the wall of the vertical shaft.
  • the vertical shaft furnace can be developed in that one or more radial mixing chambers are formed in the middle area of the vertical shaft at least over part of the circumference of the bulk material moving bed, preferably at the level of the extraction point for the synthesis gas.
  • One advantage of the radial mixing chambers in the middle area is that particularly homogeneous mixing of the synthesis gas produced by the process can be achieved.
  • the bulk material moving bed has one or more slopes in the area of the mixing chambers.
  • the moving bed of bulk material preferably has a suitable angle of slope in the central region of the vertical shaft in order to ensure the fluidized bed behavior required for generating the slopes.
  • One advantage here is that the provision of slopes increases the boundary surface between the bulk material moving bed and the mixing chambers in the central area. This results in the advantage that synthesis gases which are produced in the process can be diverted particularly easily via this interface.
  • 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.
  • the provision of a secondary shaft has the advantage that the synthesis gas produced in the process can be cleaned in the secondary shaft.
  • further devices can be provided in the secondary shaft, which allow post-treatment of the synthesis gas.
  • the synthesis gas produced by a method according to one of the preceding claims can be used as fuel gas for thermal utilization and / or as fuel gas for power generation and / or as raw material in chemical processes. It is particularly advantageous that the synthesis gas can be used directly on site, i.e. where the process takes place. In this way, exhaust gases and / or any waste heat can be fed to the process, whereby the energy requirement of the process can be further reduced.
  • the synthesis gas is filtered before it is used and, depending on the further application, is optionally cooled.
  • a filter ensures a dust-free synthesis gas that can be used in filtered form and, if necessary, also after cooling, for demanding applications, for example in internal combustion engines.
  • Figure 1 shows a vertical shaft furnace 1 for carrying out the method for producing synthesis gas 130 from carbon-rich substances 112.
  • the vertical shaft furnace 1 has a vertical shaft 100 in which a bulk material moving bed 110 moves from top to bottom.
  • the bulk material moving bed 110 consists of bulk material 111 which is fed from a bulk material source 120.
  • the bulk material 111 is composed of two materials.
  • the first material consists of the carbon-rich substance 112, which to Synthesis gas 130 is processed.
  • the second material is a non-gasifiable material 113 which is not processed into synthesis gas 130.
  • a rotating bucket (not shown) is preferably filled with the two materials while rotating before the bulk material is introduced into the vertical shaft as a mixture.
  • the bulk material 111 is introduced from the rotating bucket on an upper side 101 of the vertical shaft 100 into the vertical shaft 100 via a gas space 103 and passes through the vertical shaft 100 due to gravity.
  • the introduction can preferably take place via a moving or static solids distributor 116, via which a targeted distribution of the bulk material can take place depending on its different grain sizes in the bulk material moving bed 110.
  • the bulk material 111 is removed from the underside 102 of the vertical shaft 100 and fed to an after-treatment to be described later.
  • the two materials can also be introduced individually at alternating intervals into the vertical shaft, so that the materials are present in layers in the bulk material moving bed 110.
  • the introduction can also preferably take place via a moving or static solids distributor 116, via which a targeted distribution of the materials can take place in the moving bulk material bed 110 depending on their different grain sizes.
  • carbon-rich substance 112 for example, carbon-rich wastes such as Biomass, plastics, sewage sludge, oily sands or oil shale can be used.
  • the material 113 which itself cannot be gasified consists preferably of a mineral material, preferably of a calcitic material, particularly preferably of calcium oxide.
  • the flow of the bulk material 111 occurs from the top 101 of the vertical shaft 100 to the bottom 102 of the vertical shaft 100, the bulk material 111 passing through various process zones of the vertical shaft 100.
  • the bulk material 111 passes through a pyrolysis zone 141.
  • organic compounds are thermally split.
  • organic molecules in Split up molecules that are shorter-chain than the parent molecules. The splitting takes place in a temperature range between 200 ° C and 900 ° C
  • oxidation zone 143 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 pyrolysis residue is also known as pyrolysis coke.
  • a reduction zone 142 in which the carbon dioxide and elemental carbon are converted into carbon monoxide by the Boudouard equilibrium.
  • This reaction is endothermic and is supplied with thermal energy by the oxidation zone 143 located below the reduction zone 142, in which the exothermic oxidation of the pyrolysis coke takes place.
  • An additional supply of thermal energy takes place from the sensible heat of the moving bulk material bed coming from the pyrolysis zone 141.
  • the oxidation zone 143 is followed by an after-cooling zone 144 in which the moving bulk material bed is cooled.
  • the bulk material moving bed 110 is diverted from the vertical shaft 100 via a diverting device 150.
  • the process can be set by the dwell time of the carbon-rich substance 112 or its residues in the different process zones 141, 142, 143, 144.
  • the bulk material 111 of the bulk material moving bed 110 after being discharged from the underside 102 of the vertical shaft 100, is passed into a separation device 10, where the bulk material 111 is fractionated into three grain size fractions of coarse grain 151, medium grain 152 and fine grain 153.
  • the fraction of the coarse grain 151 can be returned to the bulk material source 120 and supplements the non-gasifiable material 113 in the bulk material source 120.
  • the medium grain fraction 152 is disposed of or is available for further use.
  • the fine-grain fraction 153 which partly also contains the ash produced in the pyrolysis zone 141 and / or in the oxidation zone 143, forms a fine material waste 154, which is disposed of or, if valuable residual materials are enriched, recycled.
  • a gas flow flows through the vertical shaft 100.
  • the gas flow runs in an upper bulk material zone 114 of the vertical shaft 100 in cocurrent with the bulk material moving bed 110. This means that the gas flow runs in the direction from the top 101 of the vertical shaft 100 in the direction of the bottom 102 of the vertical shaft 100 and thereby flows through the pyrolysis zone 141.
  • the gas flow runs in countercurrent to the moving bulk material bed 110. This means that the gas flow runs in the direction from the bottom 102 of the vertical shaft 100 to the top 101 of the vertical shaft 100.
  • a central region 104 of the vertical shaft is located between the upper bulk material zone 114 of the vertical shaft and the lower bulk material zone 115 of the vertical shaft. In this middle area 104, the gas flow from the upper bulk material zone 114 running with the moving bulk material bed 100 and the gas flow from the lower bulk material zone 115 running against the moving bulk material bed 110 meet. The pressure within the vertical shaft 100 is lowest in the central region 104.
  • the gases originating from the pyrolysis zone 141 located in the upper bulk material zone 114 and the gases originating from the reduction zone 142 located in the lower bulk material zone 115 are drawn off at an extraction point 131 of the vertical shaft 100.
  • the bulk material moving bed 110 forms, 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 110.
  • this radial mixing chamber 105 the gas stream originating from the lower bulk material zone 115 and the gas stream originating from the upper bulk material zone 114 are mixed.
  • a preheating area 145 in the upper area of the pyrolysis zone 141 and / or within the pyrolysis zone 141 air 50 and / or natural gas 60 and / or a heat exchanger medium 21 are introduced through upper plug-in lances 106. Combustible gases are at least partially burned in this upper bulk material zone 114 in order to provide thermal energy. Introduced Media 50, 60, 21, which carry thermal energy, give off their thermal energy in this preheating area 145 to the bulk material 111. In any case, the bulk material 111 first passes through a preheating area 145 in which the bulk material 111 is preheated.
  • the media 50, 60, 21 can also be introduced directly into the gas space 103, where combustible gases are at least partially burned in order to provide thermal energy. Introduced media 50, 60, 21, which carry thermal energy and / or the oxidizing gas, flow into the bulk material moving bed 110 due to the prevailing overpressure in the gas space 103 and give off their heat to the bulk material 111.
  • combustible gases can also be introduced. It is also possible, through the plug-in lances 106 and / or through the gas space, to feed overheated combustible gases or an overheated reducible gas, e.g. Initiate carbon dioxide.
  • an overheated reducible gas e.g. Initiate carbon dioxide.
  • the temperature of the bulk material moving bed 110 is increased from a temperature below 200 ° C when entering the vertical shaft 100 to a temperature above 200 ° C in the pyrolysis zone 141.
  • water vapor 70 is introduced via lower plug-in lances 108.
  • the water vapor is used as a cooling gas to cool the moving bed down to its own temperature, which is above 450 ° C.
  • This lower temperature limit is adhered to in order to rule out hydration which is undesirable at this point when calcium oxide is used as the material 113 which itself cannot be gasified.
  • water vapor 70 can also be introduced into the upper bulk material zone 114 via the upper plug-in lances 106.
  • the energy released by the hydration is available for the pyrolysis of the carbon-rich substance 112.
  • light oil 30 and / or heavy oil 80 can be introduced into the bulk material moving bed 110 through central plug-in lances 107.
  • the amount of synthesis gas and the calorific value of synthesis gas 130 can be increased.
  • the temperature in the oxidation zone 143 can be controlled, so that an extensive Oxidation of the carbon-rich pyrolysis residues and the carbon-rich residues from the reduction zone is ensured without oxidative overheating taking place.
  • the water 40 is used as a coolant, which allows the temperature in the oxidation zone 143 to be controlled through its enthalpy of vaporization and heat absorption, so that the carbon-rich pyrolysis residues are oxidized to the greatest possible extent and the carbon-rich residues from the reduction zone 142 are ensured without oxidative overheating taking place.
  • a supply of oxygen-containing gas 90 takes place on the underside 102 of the vertical shaft 100.
  • Air 50 and / or a gas mixture with a proportion of oxygen can be used as the oxygen-containing gas will.
  • the supply of oxygen-containing gas 90 via the underside of the vertical shaft 100 is preferably set in such a way that the oxidation zone 143 and the reduction zone 142 are sub-stoichiometrically supplied with oxygen, so that no oxygen is transferred into the central region 104 of the vertical shaft 100.
  • the synthesis gas 130 which is formed in the middle area 104 from the gas stream running concurrently with the bulk material moving bed 110 in the upper bulk material zone 114 and the gas stream from the lower bulk material zone 115, consists of a gas mixture that does not contain any oxygen.
  • the supply of oxygen-containing gas 90 and / or air 50 is particularly preferably carried out via the underside of the vertical shaft via two separately adjustable partial flows.
  • a cooling gas edge flow 91 is introduced into the post-cooling zone 144 via the outer edge region of the bulk material moving bed 110, while a cooling gas central flow 92 is introduced into the area of the center of the bulk material moving bed 110 in the post-cooling zone 144 .
  • Solid or liquid high boilers 109 as carbon-rich substances can be fed to the process via the bulk material.
  • liquid high boilers 109 can be fed to the process via the upper insert lances 106, the middle insert lances 107 and / or the lower insert lances 108.
  • the cooling gas supplied to the underside 102 of the vertical shaft 100 can be conducted in the moving bulk material bed in a cooling gas edge flow 91 on the outside of the moving bulk material bed 110 and in a central cooling gas flow 92 in a central area of the moving bulk material bed 110.
  • Figure 2 shows the vertical shaft furnace 1 with a secondary shaft 210, which is also designed in the form of a vertical shaft and through which the synthesis gas formed is guided in countercurrent to the secondary bulk material moving bed 220.
  • a secondary bulk material moving bed 220 runs continuously from top to bottom.
  • the secondary bulk material moving bed 220 is fed with secondary bulk material 221 by a secondary bulk material source 230 and runs from an upper side 211 of the secondary shaft 210 to a lower side 212 of the secondary shaft 210.
  • the secondary bulk material moving bed 220 consists of a secondary bulk material 221, preferably a mineral material, preferably calcium oxide and / or calcium carbonate.
  • the mean grain size of the secondary bulk material 221 is preferably smaller than the mean grain size of the bulk material 111.
  • the synthesis gas 130 withdrawn from the central region 104 of the vertical shaft 100 at the withdrawal point 131 is introduced into the secondary bulk material moving bed 220.
  • the secondary moving bulk material bed 220 forms with the secondary shaft 210 a radial chamber 213 which is formed over at least part of the circumference of the secondary moving bulk material bed 220.
  • the synthesis gas 130 flows through this radial chamber 213 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 discharged in the upper region 214 of the secondary shaft 210 from the secondary shaft 210 at a discharge point 216.
  • the use of calcium oxide as secondary bulk material 221 in secondary bulk moving bed 220 is advantageous since portions of synthesis gas 130 that contain halogens and in particular chlorine are bound by calcium hydroxide, which can be generated by the introduction of water 40 or water vapor 70, for example via secondary plug-in lances 217 in the upper region of the secondary shaft 210 by hydration.
  • halogens and especially chlorine are formed, for example, during the oxidation or pyrolysis of polyvinyl chlorides.
  • the synthesis gas 130 can be purified of sulfur compounds by the provision of calcium oxide as a bypass bulk material.
  • the secondary moving bulk material bed 220 also serves to dissipate heat from the synthesis gas 130, which leaves the vertical shaft 100 with the moving bulk material bed 110 at the removal point 131 at a temperature of over 600 ° C.
  • the heat absorption by the secondary bulk material moving bed 220 can be designed efficiently.
  • the auxiliary moving bed for bulk goods 220 is discharged from the auxiliary shaft 210 via a secondary discharge device 240.
  • the dwell time of the secondary bulk material moving bed 220 in the secondary shaft 210 can be controlled via the control of the secondary diversion device 240.
  • the secondary bulk material 221 discharged through the secondary discharge device 240 is fed to the separation device 10, where the secondary bulk material 221, like the bulk material 111, is fractionated into coarse grain 151, medium grain 152 and fine grain 153.
  • the central grain 152 separated in the separation device 10 can at least partially be added to the secondary bulk material source 230 and, together with the secondary bulk material material 221, can form the secondary bulk material moving bed 220.
  • Both the fractionated bulk material 111 of the bulk material moving bed 110 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 medium grain 152.
  • a heat exchanger 20 is arranged in the lower region 215 of the secondary shaft 210.
  • the heat exchanger 20 absorbs the heat from the secondary bulk material moving bed 220 which was given off by the synthesis gas 130 to the secondary bulk material moving bed 220.
  • Through the heat exchanger 20 flows a heat exchanger medium 21, which the heat to the upper Insertion lances 106 of the vertical shaft 100 transported.
  • Natural gas 60, synthesis gas 130, water 40 or water vapor 70 can be used as the heat exchange medium 21.
  • the heat exchanger medium 21 is introduced into the bulk material moving bed 110 through the upper plug-in lances 106 and there gives off the heat to the bulk material moving bed 110. In this way, the non-gasifiable material 113 and the carbon-rich substances 112 are warmed or heated to the necessary pyrolysis temperature.
  • the introduction of heat 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, since the metering of air 50 for the additional firing can be completely or partially omitted. As a result, less nitrogen reaches the pyrolysis zone, which reduces the calorific value of the synthesis gas 130.
  • the secondary bulk material moving bed 220 is preferably cooled by introducing cold synthesis gas 130 into the underside 212 of the secondary shaft 210.
  • the synthesis gas 130 flows through the secondary bulk material moving bed 220 in countercurrent and meets the synthesis gas 130 in a central region 218 of the secondary shaft 210, which exits at the extraction point 131 of the vertical shaft 100 and is introduced into the radial chamber 213 of the secondary shaft 210.
  • the synthesis gas 130 diverted from the secondary shaft 210 at the discharge point 216 is passed through a synthesis gas heat exchanger (not shown), the synthesis gas 130 being further cooled in this synthesis gas heat exchanger.
  • the heat extracted from the synthesis gas 130 can be fed to the vertical shaft 100 at the upper plug-in lances 106 via a suitable heating medium, which is, for example, water vapor 70, air 50, natural gas 60 or synthesis gas 130.
  • the synthesis gas 130 passes through a synthesis gas filtration (also not shown), with fine dust contained in the synthesis gas 130 being separated off.
  • the synthesis gas 130 filtered from the fine dust then passes through a second synthesis gas heat exchanger and is fed to a quench circuit, in which 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 light oil 30 and / or water 40 can be fed to the vertical shaft 100 via the central plug-in lances 107 between the oxidation zone 143 and the reduction zone 142.
  • the separated water 40 can also be introduced into the preheating area 145 of the vertical shaft 100 via the plug-in lances 106 and / or into the secondary shaft 210 via the auxiliary plug-in lances 217.
  • the synthesis gas 130 which has been filtered and freed from heavy oil 80, light oil 30 and water 40 by condensation, is available as fuel for engines, for example for generating electricity. Furthermore, the synthesis gas 130 obtained in the process can be used thermally, for example as a substitute for fossil fuels or as a material.
  • sewage sludge for example in compacted form
  • 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 discharge device 240 is compacted and is no longer fed to the circuit of the secondary bulk moving bed 220.
  • the briquetted secondary bulk material can also be used several times in the moving bulk material bed 100 in order to enrich the phosphates produced by the processing of sewage sludge.
  • Figure 3 shows a further embodiment of a vertical shaft furnace 1 with a secondary shaft 310, which is also designed in the form of a vertical shaft and through which the synthesis gas 130 formed is fed in cocurrent to the secondary bulk moving bed 320 and passed through it.
  • the vertical shaft 100 corresponds to the vertical shaft 100 according to the explanations relating to Figures 1 and 2 , which is referred to at this point.
  • the secondary bulk material moving bed 320 runs continuously from an upper side 311 of the secondary shaft 310 to a lower side 312 of the secondary shaft 310.
  • the secondary bulk moving bed 320 is fed secondary bulk material 321 by a secondary bulk source 330.
  • the secondary bulk material moving bed 320 has a secondary bulk material 321, preferably a mineral material, preferably calcium oxide and / or calcium carbonate.
  • the synthesis gas 130 withdrawn from the central area 104 of the vertical shaft 100 at the extraction point 131 is introduced into the secondary bulk material moving bed 320 via a cavity 322 in an upper area 314 of the secondary shaft 320.
  • the synthesis gas 130 flows through the secondary bulk material moving bed 320 in cocurrent and is diverted in a lower region 315 of the secondary shaft 310 from the secondary shaft 310 at a discharge point 316.
  • secondary bulk material 321 in secondary bulk moving bed 320 is advantageous, since in this case cooling by metering water 40 or water vapor 70 via spray nozzles 317 directly via cavity 322 without the secondary bulk material 321 being hydrated .
  • efficient direct cooling in the secondary bulk material moving bed 320 can be implemented.
  • the secondary bulk material moving bed 320 is diverted from the secondary shaft 310 via a secondary diversion device 340.
  • the dwell time of the secondary bulk material moving bed 320 in the secondary shaft 310 can be controlled via the control of the secondary diversion device 340.
  • the secondary bulk material 321 diverted by the secondary discharge device 340 is fed to the separation device 10, where the secondary bulk material 321, like the bulk material 111, is fractionated into coarse grain 151, medium grain 152 and fine grain 153.
  • the middle grain 152 separated in the separation device 10 can at least partially be added to the secondary bulk material source 330 and, together with the secondary bulk material 321, can form the secondary bulk material moving bed 320.
  • Both the fractionated bulk material 111 of the bulk material moving bed 110 of the vertical shaft 100 and the fractionated secondary bulk material 321 of the secondary bulk material moving bed 320 of the secondary shaft 310 in a common fraction form the medium grain 152.
  • a heat exchanger 20 is arranged, which is similar to the description of FIG Figure 2 Applies. Natural gas 60, synthesis gas 130, water 40 or water vapor 70 can be used as the heat exchange medium 21.
  • the synthesis gas 130 diverted from the secondary shaft 310 in the lower region 315 of the secondary shaft 310 at the discharge point 316 can analogously to the description of FIG Figure 2 further processed and used.

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Claims (15)

  1. Procédé de fabrication de gaz de synthèse (130) à partir de substances riches en carbone (112), dans lequel un lit mobile de matière en vrac (110) est constitué d'une matière en vrac (111) qui est composée des substances riches en carbone (112) et d'une matière (113) non auto-gazéifiable, et dans lequel le lit mobile de matière en vrac (110) se déplace en continu ou par intervalles de haut en bas dans un puits vertical (100) d'un four de puits vertical (1) et est traversé par du gaz, dans lequel la matière (113) non auto-gazéifiable et les résidus des substances riches en carbone (112) sont évacués sur le côté inférieur (102) du puits vertical (100), dans lequel au moins une zone de pyrolyse (141) et une zone de réduction (142) pour la génération de composants du gaz de synthèse (130) sont formées dans le lit mobile de matière en vrac (110) traversé par le gaz, dans lequel les produits de réaction provenant d'une zone d'oxydation (143) également formée dans le lit mobile de matière en vrac sont réduits dans la zone de réduction, caractérisé en ce que le gaz de synthèse (130) est prélevé dans une zone centrale (104) du puits vertical (100) à un point de prélèvement (131) entre une zone supérieure de matière en vrac (114) et une zone inférieure de matière en vrac (115), et les substances riches en carbone (112) sont au moins partiellement déplacées avec le lit mobile de matière en vrac (110) de la zone de pyrolyse (141) dans la zone supérieure de matière en vrac (114) via la zone centrale (104) dans la zone de réduction (142) et dans la zone d'oxydation (143) dans la zone inférieure de matière en vrac (115) du lit mobile de matière en vrac (110), dans lequel une partie du gaz de synthèse (130) est générée dans une zone de pyrolyse (141) du lit mobile de matière en vrac (110) formée dans la zone supérieure de matière en vrac (114) et une autre partie du gaz de synthèse (130) est générée dans une zone de réduction (142) dans la zone inférieure de matière en vrac (115) et la zone supérieure de matière en vrac (114) est traversée à co-courant et la zone inférieure de matière en vrac (115) à contre-courant.
  2. Procédé selon la revendication 1, caractérisé en ce que la matière non auto-gazéifiable (113) introduite dans la zone supérieure de matière en vrac (114) présente une proportion en poids de la matière en vrac (111) d'au moins 20 % avant le chauffage et en ce que la matière non auto-gazéifiable (113) dans la matière en vrac (111) est chauffée dans la zone supérieure de matière en vrac (114) au moyen de gaz chauffé à une température propre de plus de 350 °C.
  3. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la substance riche en carbone (112) et la matière non auto-gazéifiable (113) sont mélangées l'une à l'autre avant et/ou après l'entrée dans le puits vertical (100) au moyen d'un ou plusieurs systèmes rotatifs, de préférence par remplissage parallèle d'une benne rotative et/ou par dosage commun et/ou parallèle d'une ou de plusieurs goulottes rotatives et/ou sont introduites individuellement à intervalles alternés dans le puits vertical, résultant en un agencement en couches des matières dans le lit mobile de matière en vrac (110) avant que celui-ci se déplace de haut en bas à travers le puits vertical (100).
  4. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que dans la zone centrale (104) du puits vertical (100), au moins sur une partie de la circonférence du lit mobile de matière en vrac, une ou plusieurs chambres de mélange radiales (105) sont formées, dans lesquelles les proportions du gaz de synthèse (130) provenant de la zone inférieure de matière en vrac (115) sont mélangées avec les proportions du gaz de synthèse provenant de la zone supérieure de matière en vrac (114) et la température du gaz de synthèse (130) au point de prélèvement (131) est réglée entre 600 °C et 1 300 °C.
  5. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la matière non auto-gazéifiable (113) du lit mobile de matière en vrac (110) contient une matière calcaire dans une proportion de 10 à 100 %, la matière calcaire étant de préférence constituée de chaux vive et/ou de calcaire.
  6. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'un espace gazeux (103) est formé à l'extrémité supérieure de la zone supérieure de produit en vrac (114) dans le puits vertical (100), dans lequel un gaz surchauffé est formé par des processus d'oxydation, et/ou dans lequel un gaz surchauffé est introduit et/ou une introduction de gaz surchauffé se produit dans le lit mobile de matière en vrac (110) au niveau de la zone d'oxydation (143) et/ou au niveau de la zone de pyrolyse (141) en utilisant des lances d'insertion (106, 107).
  7. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que du gaz contenant du dioxyde de carbone est ajouté dans le lit mobile de matière en vrac (110) pour la carbonisation de la matière calcaire en tant que partie constituante de la matière en vrac (111) et utilisation de la chaleur de processus alors libérée et/ou est formé par addition d'air (50) ou de gaz contenant de l'oxygène (90) par oxydation.
  8. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'un gaz de refroidissement est introduit sur un côté inférieur (102) du puits vertical (100) pour former une zone de post-refroidissement (144) et le gaz de refroidissement introduit contient le gaz de synthèse (130) et/ou contient au moins un gaz combustible (60) ou bien contient de l'air (50) et/ou un gaz réductible.
  9. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que de l'oxygène pur ou un mélange gazeux avec une concentration d'oxygène enrichie par rapport à l'air est ajouté au lit mobile de matière en vrac (110).
  10. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que des déchets plastiques et/ou des déchets organiques et/ou des substances à haut point d'ébullition (109) sont au moins partiellement utilisés comme substances riches en carbone (112), dans lesquelles les substances à haut point d'ébullition sont introduites directement dans le lit mobile de matière en vrac (110) de préférence sous forme liquide, de préférence au moyen de lances d'insertion (106, 107) au niveau de la zone de pyrolyse (141) et/ou de la zone de réduction (142) et/ou de la zone d'oxydation (143), et/ou sont dosées dans le lit mobile de matière en vrac par l'espace gazeux (103) à l'extrémité supérieure de la zone supérieure de matière en vrac et/ou sont ajoutées directement à la matière en vrac (111) avant d'entrer dans le puits vertical (100).
  11. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le lit mobile de matière en vrac (110) passe au moins partiellement par le puits vertical (100) plusieurs fois dans le circuit.
  12. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le gaz de synthèse (130) retiré du lit mobile de matière en vrac (110) au point de prélèvement (131) est ensuite dirigé à travers un lit mobile de matière en vrac secondaire (220) qui contient une matière en vrac secondaire (221) avec une proportion d'au moins 10 % jusqu'à une proportion de 100 % de matières alcalines.
  13. Procédé selon la revendication 12, caractérisé en ce que le lit mobile de matière en vrac secondaire (320) est conduit dans un puits secondaire (310) du four de puits vertical (1) à co-courant vers le gaz de synthèse (130), dans lequel le puits secondaire (310) du four de puits vertical (1) est disposé séparément du puits vertical (100) du four de puits vertical (1) et le gaz de synthèse (130) est introduit dans la partie supérieure du puits secondaire (311) et est prélevé dans la partie inférieure (315) du puits secondaire (310).
  14. Procédé selon l'une quelconque des revendications 12 à 13, caractérisé en ce que la granulométrie moyenne de la matière en vrac (111) et la granulométrie moyenne de la matière en vrac secondaire (221) sont dans la plage de 5 mm à 30 cm, de préférence dans la plage de 5 mm à 15 cm, ou la granulométrie moyenne de la matière en vrac (111) est supérieure à 1 cm et la granulométrie moyenne de la matière en vrac secondaire (221) est inférieure à 10 cm.
  15. Procédé selon l'une des revendications 12 à 14, caractérisé en ce que de l'eau (40) et/ou de la vapeur (70) sont ajoutées dans une ou plusieurs positions au lit mobile de matière en vrac (110) et/ou au lit mobile de matière en vrac secondaire (220).
EP18704520.8A 2017-02-13 2018-02-08 Preparation de syntheseges a partir de substances carbones au moyen d'une procedure combiné co-courant et contre-courant Active EP3580312B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102017102789.0A DE102017102789A1 (de) 2017-02-13 2017-02-13 Herstellung von Synthesegas aus kohlenstoffreichen Substanzen mittels eines Gleichstrom-Gegenstrom-Verfahrens
PCT/EP2018/053133 WO2018146179A1 (fr) 2017-02-13 2018-02-08 Production de gaz de synthèse à partir de substances riches en carbone au moyen d'un procédé combiné de co-courant et contre-courant

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DE102020208690B4 (de) 2020-07-10 2022-02-24 Vyacheslav Ivanov A. Gaserzeugungsanlage und Gaserzeugungsverfahren zur Erzeugung von wasserstoffhaltigem Synthesegas

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GB0325668D0 (en) * 2003-11-04 2003-12-10 Dogru Murat Intensified and minaturized gasifier with multiple air injection and catalytic bed
WO2007081296A1 (fr) * 2006-01-16 2007-07-19 Gep Yesil Enerji Uretim Teknolojileri Ltd. Sti. Gazogene a ecoulement descendant/ascendant pour production de gaz de synthese a partir de dechets solides
DE102007062414B4 (de) 2007-12-20 2009-12-24 Ecoloop Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
DE102012014161A1 (de) 2012-07-18 2014-02-20 Ecoloop Gmbh Gegenstrom-/Gleichstrom-Vergasung von kohlenstoffreichen Substanzen

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EP3580312A1 (fr) 2019-12-18
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