WO2018146179A1 - Production de gaz de synthèse à partir de substances riches en carbone au moyen d'un procédé combiné de co-courant et contre-courant - Google Patents

Production de gaz de synthèse à partir de substances riches en carbone au moyen d'un procédé combiné de co-courant et contre-courant Download PDF

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Publication number
WO2018146179A1
WO2018146179A1 PCT/EP2018/053133 EP2018053133W WO2018146179A1 WO 2018146179 A1 WO2018146179 A1 WO 2018146179A1 EP 2018053133 W EP2018053133 W EP 2018053133W WO 2018146179 A1 WO2018146179 A1 WO 2018146179A1
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WIPO (PCT)
Prior art keywords
bulk material
vertical shaft
moving bed
gas
synthesis gas
Prior art date
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PCT/EP2018/053133
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German (de)
English (en)
Inventor
Leonhard Baumann
Roland Möller
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Ecoloop Gmbh
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Application filed by Ecoloop Gmbh filed Critical Ecoloop Gmbh
Priority to EP18704520.8A priority Critical patent/EP3580312B1/fr
Publication of WO2018146179A1 publication Critical patent/WO2018146179A1/fr

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Classifications

    • 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 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.
  • 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.
  • 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.
  • the precompressed, formed in the first vertical process space synthesis gas flows out at the top of the first vertical process space.
  • 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.
  • 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 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.
  • compacted, in particular pelleted, material as the carbon-rich 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.
  • 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 can not be gasified by itself can be comminuted by high shear forces in the bulk material moving bed Take over substances.
  • a suitable material that can not be gasified it is possible to bind certain pollutants out of 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 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.
  • 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.
  • 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.
  • the upper bulk material zone is flowed through in direct current and the lower bulk material zone in countercurrent flow.
  • the synthesis gas in the upper region does not flow counter to the direction of the bulk material moving bed.
  • 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.
  • 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
  • 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.
  • 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.
  • a distribution control is advantageous if one or both of the materials introduced have different particle sizes.
  • 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.
  • 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.
  • 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.
  • an advantageously homogeneous synthesis gas results with a sufficiently high mixing temperature for the complete thermal cleavage.
  • 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 ,
  • 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.
  • the mass ratio between the carbon-rich substances and the non-gasifiable 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
  • the hydration is exothermic, which advantageously provides energy in the form of heat for the endothermic processes in the vertical shaft furnace.
  • 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.
  • chlorine-rich and / or bromine and / or sulfur-containing carbon-rich substances are introduced into the bulk material moving bed.
  • 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.
  • 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.
  • 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.
  • 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.
  • the energy input in the individual processing zones can be controlled in an advantageous manner.
  • hot solids streams from industrial processes, for example cement clinker as hot, even non-gasifiable materials.
  • the hot non-gasifiable material may be a product of pig iron production.
  • 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.
  • 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.
  • 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.
  • 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.
  • the cooling gas introduced at the bottom of the vertical shaft contains a mixture of reducible gas and air.
  • 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.
  • 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.
  • a combustible gas which is preferably natural gas
  • 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.
  • 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 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • plastic waste 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • At least partially phosphorus-containing sewage sludge are used as high-carbon substances.
  • 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.
  • the synthesis gas yield and the hydrogen content in the synthesis gas can be significantly increased.
  • the heat energy released is available to compensate for the endothermic reactions in the pyrolysis zone and in the reduction zone.
  • 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.
  • 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.
  • metal components such as those found in electronic scrap in large proportions and / or other valuable substances, such as aluminum, halogens or phosphorus
  • 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.
  • the bulk material moving bed at least partially passes through the vertical shaft several times in the circulation.
  • residual materials are, for example, ashes, metals or minerals.
  • the enriched residual materials can then be sorted, optionally treated and recycled.
  • 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.
  • the Fine thoroughlygutwanderbett 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.
  • 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.
  • 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.
  • Another embodiment of the synthesis gas purification in the secondary shaft provides that the Mau oftengutwanderbett 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 Mau wellgutmaterial.
  • the design of the gas duct which is structurally more complex, can be omitted in a central region of the secondary duct.
  • 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 Mau oftengutmate- rials and the synthesis gas at the bottom of the secondary shaft.
  • the Mau wellgutmaterial is cooled by means of a heat exchanger.
  • 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.
  • 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.
  • the Maucetmate- rial is discharged uncooled from the side shaft in the lower region of the secondary shaft.
  • the uncooled discharge of Volunteer cangutmaterials has the advantage that the Maucetmaterial that has been heated by the synthesis gas is available as input material for other processes available.
  • the heating of Volunteer cangutmaterials designed here advantageous if heat energy is required for the connection processes.
  • a further advantageous embodiment provides that the Super thoroughlygutmaterial 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 Mauschuttgutwanderbett 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 Mau frequentlygutwan- 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.
  • the mean grain size of the bulk material moving bed is greater than the mean grain size of Mau commonlygutwanderbettes.
  • the mean grain size of the bulk material moving bed is greater than the mean grain size of Maucetwanderbettes.
  • the mean grain size of the bulk material and the mean grain size of Mau oftengutmaterials 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 Mau oftengutmaterials 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 Mau commonlygutwanderbett 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • a mixing device is advantageously ensured that the bulk material of the bulk material moving bed is homogeneous.
  • the carbon-rich substance and the self-gasifiable material can be introduced individually at alternating intervals in the vertical shaft.
  • 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 vorappelbar.
  • 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.
  • 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.
  • 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.
  • synthesis gases produced in the process are particularly easily derivable 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 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.
  • 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.
  • 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.
  • the vertical shaft furnace 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • the bulk material 1 1 1 passes through a pyrolysis 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
  • 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 residue of pyrolysis is also referred to as pyrolysis coke.
  • 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.
  • 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.
  • material flow of the bulk material moving bed 1 10 can be the residence time in the vertical shaft 100 control.
  • 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 ,
  • 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.
  • a central portion 104 of the vertical shaft 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.
  • 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.
  • a radial mixing chamber 105 which is formed over at least part of the circumference of the bulk material moving bed 1 10.
  • 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.
  • 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.
  • 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.
  • 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.
  • water vapor 70 is introduced via lower insertion lances 108.
  • 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.
  • water vapor 70 can also be introduced in the upper bulk material zone 14 via the upper insertion lances 106.
  • light oil 30 and / or heavy oil 80 can be introduced into the bulk material moving bed 1 10 through middle insertion lances 107.
  • the amount of synthesis gas and the calorific value of the synthesis gas 130 can be increased.
  • 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.
  • 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.
  • a supply of oxygen-containing gas 90 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.
  • the oxygen-containing gas can be used 50 and / or a gas mixture with a proportion of oxygen become.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • the Supercomachtgut 210 runs a Maucetwanderbett 220 from top to bottom continuously.
  • the Mau frequentlygutwanderbett 220 is fed by a Maucetetti 230 with Maucetmaterial 221 and extends from a top 21 1 of the secondary shaft 210 to a bottom 212 of the secondary shaft 210th
  • the Mau frequentlygutwanderbett 220 consists of a Maucetmaterial 221, preferably a mineral material, preferably from calcium oxide and / or calcium carbonate.
  • the average particle size of Volunteer whogutmaterials 221 is less than the mean grain size of the bulk material 1 1 1.
  • extracted synthesis gas 130 is introduced.
  • the Maucetwanderbett 220 forms with the secondary shaft 210 a radial chamber 213, which is formed over at least a portion of the circumference of Maucetwanderbettes 220.
  • 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
  • the use of calcium oxide as Mau frequentlygutmaterial 221 in the Mau frequentlygutwanderbett 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 Maueinstecklanzen
  • Halogens and, in particular, chlorine are formed, for example, in the oxidation or pyrolysis of polyvinyl chlorides.
  • synthesis gas 130 can be purified by providing calcium oxide as a minor bulk material of sulfur compounds.
  • the Maucetwanderbett 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 Mau frequentlygutwanderbett 220 and the rising synthesis gas 130, the heat absorption by the Mau oftengutwanderbett 220 can make efficient.
  • the secondary bulk material moving bed 220 is discharged from the secondary shaft 210 via a secondary discharge device 240.
  • the residence time of Maucetwanderbettes 220 can be controlled in the secondary shaft 210.
  • the Supernetgutmaterial 221 discharged through the Mauaus effetsvoriques 240 is fed to the separation device 10, where the Maucetmaterial 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.
  • 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.
  • a heat exchanger 20 is arranged in the lower region 215 of the secondary shaft 210.
  • the heat exchanger 20 receives the heat of Mauisgutwanderbettes 220, which was discharged through the synthesis gas 130 to the Mau usuallygutwanderbett 220.
  • 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 Mau oftengutwanderbett 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.
  • a suitable heat medium which is, for example, water vapor 70, air 50, natural gas 60 or synthesis gas 130.
  • a synthesis gas filtration also not shown, wherein in the synthesis gas 130 contained particulate matter is deposited.
  • 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 / orchtol 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 Maueinstecklanzen 217 in the secondary shaft 210.
  • the filtered and freed by condensation of heavy oil 80,chtol 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.
  • the bulk material moving bed 1 10 as carbon-rich substances 1 12 sewage sludge, for example in compacted form, fed.
  • 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.
  • the briquetted Mau featuregut- 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.
  • 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 Mau thoroughlygutwanderbett 320 is fed by a Maucetetti 330 with Maucetmaterial 321.
  • the Maucetwanderbett 320 has a Maucetmaterial 321, preferably a mineral material, preferably calcium oxide and / or calcium carbonate.
  • the synthesis gas 130 flows through the Mau—gutwanderbett 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.
  • the use of calcium carbonate as Mau frequentlygutmaterial 321 in the Mauschuttgutwanderbett 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 Mau usuallygutmaterial 321 is hydrated , As a result, an efficient direct cooling in the secondary bulk moving bed 320 can be realized.
  • the Super oftengutwanderbett 320 is discharged from the secondary shaft 310 via a secondary discharge device 340.
  • the residence time of Maucetwanderbettes 320 in the secondary shaft 310 can be controlled.
  • the Supernetgutmaterial 321 discharged through the Mauaus effetsvoriques 340 is fed to the separation device 10, where the Mau frequentlygutmaterial 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.
  • 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.
  • Heat exchange medium 141 pyrolysis zone

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Abstract

Procédé pour la production de gaz de synthèse (130) à partir de substances riches en carbone (112) dans un puits vertical avec un lit mobile à matière en vrac (110), le lit mobile à matière en vrac (110) traversé par le gaz étant formé, pour la production des composants du gaz de synthèse (130), d'une zone d'oxydation (143), d'une zone de pyrolyse (141) et d'une zone de réduction (142), le gaz de synthèse (130) étant extrait à un point de prélèvement (131) entre une zone de matière en vrac supérieure (114) et une zone de matière en vrac inférieure (115) et les substances riches en carbone (112) étant déplacées avec le lit mobile à matière en vrac (110) de la zone de pyrolyse (141) dans la zone de matière en vrac supérieure (114) à travers la zone centrale (104) vers la zone de réduction (142) et vers la zone d'oxydation (143) dans la zone de matière en vrac inférieure (115) du lit mobile à matière en vrac (110), la zone de matière en vrac supérieure (114) étant traversée en co-courant et la zone de matière en vrac inférieure (115) en contre-courant.
PCT/EP2018/053133 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 WO2018146179A1 (fr)

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EP18704520.8A EP3580312B1 (fr) 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

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020095866A1 (en) * 2000-12-04 2002-07-25 Hassett Scott E. Multi-faceted gasifier and related methods
WO2005047435A2 (fr) * 2003-11-04 2005-05-26 Iti Limited Gazeification
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
DE102007062414A1 (de) 2007-12-20 2009-07-02 Conera Process Solutions 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

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020095866A1 (en) * 2000-12-04 2002-07-25 Hassett Scott E. Multi-faceted gasifier and related methods
WO2005047435A2 (fr) * 2003-11-04 2005-05-26 Iti Limited Gazeification
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
DE102007062414A1 (de) 2007-12-20 2009-07-02 Conera Process Solutions 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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