EP3412754B1 - Charge de fines de charbon pour un gazéificateur sous pression à lit fixe - Google Patents

Charge de fines de charbon pour un gazéificateur sous pression à lit fixe Download PDF

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Publication number
EP3412754B1
EP3412754B1 EP17400030.7A EP17400030A EP3412754B1 EP 3412754 B1 EP3412754 B1 EP 3412754B1 EP 17400030 A EP17400030 A EP 17400030A EP 3412754 B1 EP3412754 B1 EP 3412754B1
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EP
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Prior art keywords
density
heavy
fixed
coal
heavy material
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EP17400030.7A
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German (de)
English (en)
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EP3412754A1 (fr
Inventor
Nicolás Spiegl
Frederic Judas
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to EP17400030.7A priority Critical patent/EP3412754B1/fr
Priority to PCT/EP2018/025142 priority patent/WO2018224186A1/fr
Priority to CN201810576476.8A priority patent/CN109022039B/zh
Priority to CN201820875258.XU priority patent/CN209652248U/zh
Publication of EP3412754A1 publication Critical patent/EP3412754A1/fr
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Publication of EP3412754B1 publication Critical patent/EP3412754B1/fr
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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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B9/00—General arrangement of separating plant, e.g. flow sheets
    • B03B9/005—General arrangement of separating plant, e.g. flow sheets specially adapted for coal
    • 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
    • C10J3/30—Fuel charging devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/04—Gasification
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/24—Mixing, stirring of fuel components
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/28—Cutting, disintegrating, shredding or grinding
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel

Definitions

  • the invention relates to a method and a plant for producing a fine coal insert from raw coal associated with bedrock as a starting material for a fixed bed pressure gasifier of the FBDB type.
  • Synthesis gases are gas mixtures containing hydrogen and carbon oxides, which are used in various synthesis reactions. Examples of this are methanol synthesis, the production of ammonia by the Haber-Bosch process or the Fischer-Tropsch synthesis.
  • a common process for the production of synthesis gases is the gasification of coal by means of fixed-bed pressure gasification reactors using water vapor (hereinafter simply referred to as steam) and oxygen or air as a gasification agent in a shaft reactor under excess pressure to give a synthesis gas containing carbon monoxide and hydrogen, depending on the procedure solid ashes or liquid slag are obtained as by-products from gasification.
  • steam water vapor
  • oxygen or air as a gasification agent in a shaft reactor under excess pressure to give a synthesis gas containing carbon monoxide and hydrogen, depending on the procedure solid ashes or liquid slag are obtained as by-products from gasification.
  • the gasification medium therefore moves through the bed made of granular or particulate fuel or feedstock.
  • This type of gasifier has excellent thermal efficiency, as discharged ash heats the incoming gases and the discharged product gas heats up the solid feed.
  • the long residence times of solid particles moving through the bed typically 1 to 2 hours, together with the typical temperature profile of the countercurrent system, enable high carbon conversion efficiency.
  • a widely used version of the moving bed gasifier is the Lurgi pressure gasifier with dry ash bed (Lurgi FBDB (fixed bed dry bottom) gasifier), which has been used commercially since the 1930s.
  • the carburetor is surrounded by a water jacket for cooling, in which process steam is generated.
  • Storage tanks and a lock system for feeding the coal used as feed material are mounted on top of the carburetor.
  • a motor driven distributor is used to evenly distribute the coal entering the reaction chamber over the coal bed.
  • a mechanical stirrer is included in some versions to allow the use of baking coals.
  • a motorized rotating grate on the bottom of the carburetor is used to draw off the ash that has been created, which is discharged via a corresponding lock system and fed to a storage container.
  • Steam and oxygen or air are introduced at the bottom of the carburetor as a gasifying agent and distributed into the carbon bed via the rotating grate.
  • the grate supports the carbon bed and is constantly rotated to ensure a constant, even discharge of the ashes.
  • Raw synthesis gas as the product gas is at the top of the gasifier with a typical temperature between 400 and 600 ° C discharged and flows through a washer-cooler, where it is cooled and washed. A further cooling, cleaning and conditioning of the gas takes place depending on the desired application.
  • coal which are intended for use in gasification processes such as the FBDB process, contain a more or less high proportion of minerals as bedrock or - according to mining terminology - mountains.
  • the ash content is normally reduced by a washing process, the so-called coal washing.
  • the main advantages of a reduced ash content are reduced transport costs and the associated reduced emissions from transport, as well as a reduced wear of the equipment and associated lower maintenance costs and a higher thermal efficiency of the process.
  • the ash content is reduced by density separation processes such as coal washing, in which the raw coal is separated into a fraction with a high ash content and a high relative density and into a fraction with a low ash content and a relatively low density.
  • a stable operation of an FBDB coal gasifier also requires an ash bed that is stable enough to support the weight of the coal bed and also enables a uniform and homogeneous distribution of the gas flow through the fixed bed. To achieve this, it is necessary to optimize the ratio of liquid slag and solid minerals in the hottest zone of the gasification reactor by adjusting the vapor-to-oxygen ratio in the gasification agent accordingly.
  • a reduction in the coal ash content is also of interest in order to reduce the wear and maintenance costs of the gasification reactor. It can be done by a known density separation before gasification, which is also referred to as coal washing.
  • the U.S. patent US 8906122 B2 teaches a process for producing a coal insert for coal gasification, in which the raw coal used is subjected to a coal wash, whereby coal fractions with different densities and mineral contents are obtained.
  • the light fraction obtained is fed to entrained-flow gasification and the heavy fraction to fixed-bed pressure gasification.
  • the disadvantage here is that two different gasification technologies have to be used.
  • the object of the present invention is therefore to propose a method and a plant for producing a fine coal insert for a fixed bed pressure gasifier which does not have the disadvantages mentioned of the methods known from the prior art.
  • the invention also relates to a system for carrying out the method according to the invention, and further refinements of the system according to the invention.
  • the method according to the invention permits the production of a fine coal insert for a fixed bed pressure gasifier of the FBDB type and the use of this fine coal insert for producing a synthesis gas comprising hydrogen and carbon oxides.
  • reaction conditions of fixed-bed pressure gasification are to be understood as the reaction and process conditions known per se to the person skilled in the art, in particular of temperature, pressure and residence time, as are discussed in detail in the relevant literature and in which at least a partial conversion, but preferably technically relevant conversions, of the use of fine coal with the gasification agents in synthesis gas products such as CO and hydrogen.
  • a modified coal washing and coal mixing process and a suitable plant which, on the one hand, reduce the amount of rock or ash in the coal and, on the other hand, ensure that the required ratio of liquid slag to solid minerals can be achieved in order to to achieve the desired binding effect, with which smaller ash or clinker particles are combined to form larger and stable particles.
  • This will make it cheap Gassing and support properties of the ash support on the carburetor grate are preserved and the mechanical wear of the gasification reactor is reduced.
  • the lightest fraction is a fine coal fraction as light material with a high carbon content, low proportion of rock and relatively low density
  • the heaviest fraction is a heavy material with low carbon content, high proportion of rock and relatively high density, which can be further processed by homogenization and classification .
  • the latter also speaks of mountains or the mountain fraction.
  • the fine coal fraction is then mixed with the homogenized recovery fraction.
  • the invention is now based on the knowledge that the heavy material or the recovery fraction obtained has a comparatively high proportion of minerals which at least partially melt under the reaction conditions of fixed-bed pressure gasification or - at least on their surface - soften.
  • This fraction is therefore very suitable as a binder, with which smaller ash or clinker particles can be combined to form larger and stable particles.
  • the liquid material acts as a binder or adhesive if it solidifies again at lower temperatures on the underside of the reactor. Larger ash particles or clinker particles form when solid ash particles are connected to one another by means of the liquid slag.
  • the ratio of liquid slag to solid ash particles for a specific coal depends on the maximum temperature, which can be influenced by adjusting the steam-to-oxygen ratio in the gasifying agent.
  • the ratio of liquid slag to solid particles defines not only the size of the clinker particles that are formed, but also their stability. In general a higher proportion of liquid slag leads to the formation of stronger and larger clinker particles.
  • the clinker particles must be stable enough to be able to bear the weight of the carbon bed on them and at the same time their particle size distribution must be such that it ensures a homogeneous and uniform distribution of the gasification agent over the cross section of the gasification reactor.
  • a light fraction which is characterized by a low ash content and a low relative density and which contains the particles which consist of a carbon matrix which is intimately mixed with clay mineral particles.
  • Particles that consist of pure mineral content (so-called bedrock or mountains) and particles with a very high content of minerals and only a very low content of coal are separated into a waste fraction that has a high ash content and a high relative density. If necessary, a so-called medium-good fraction is also obtained, which has a medium ash content and a medium specific density.
  • the majority of the minerals in the light fraction consist of clay minerals, especially kaolinite. At high temperatures, kaolinite converts to mullite, which has a melting temperature of 1840 ° C and therefore remains solid under the reaction conditions in the gasification reactor.
  • the proportion of kaolinite is very high compared to the other remaining minerals, a situation can arise in the light fraction in which there is not enough material available that can serve as an adhesive, i.e. can form liquid slag that acts as a binder between the kaolinite or mullite particles can serve. A stable clinker bed can therefore not be formed.
  • the proportion of minerals which are converted into liquid slag and can thus serve as an adhesive or binder is increased.
  • the ash portion of the fine coal insert for the fixed-bed pressure gasifier is also significantly reduced compared to the raw coal, which also reduces the mechanical wear of the gasifier during operation with the fine coal insert produced according to the invention.
  • the crushing and mixing action of the rotating grate from the fine coal insert obtained according to the invention results in an ash bed with gasification conditions obtained under gasification conditions, which is improved compared to ash beds which are obtained from fine coal inserts according to the prior art are.
  • the raw coal is associated with bedrock that contains at least two different mineral types, the first mineral type at least partially melting or softening under the reaction conditions of the fixed bed pressure gasification and the second mineral type remaining solid under the same reaction conditions and the second mineral type being stronger attached to the coal or more intimately associated with it. It is advantageous that mechanical processing and separation processes such as crushing and subsequent density separation, separation or at least enrichment of the two mineral types can take place.
  • the first type of mineral is enriched due to its relatively higher density in the heavy material, the mountain fraction; the second type of mineral remains in the light fraction due to its intimate association with coal.
  • a light fraction is obtained which is characterized by a low ash content and a low relative density and which contains the particles which consist of a carbon matrix which is intimately mixed with clay mineral particles, especially kaolinite. Walks at high temperatures kaolinite turns into mullite, which has a melting temperature of 1840 ° C and therefore remains solid under the reaction conditions in the gasification reactor.
  • the proportion of kaolinite is very high compared to the other remaining minerals, a situation can arise in the light fraction in which there is not enough material available that can serve as an adhesive, i.e. can form liquid slag that acts as a binder between can serve the kaolinite or mullite particles. A stable clinker bed can therefore not be formed.
  • the proportion of minerals which are converted into liquid slag and can thus serve as an adhesive or binder is increased.
  • the ash portion of the fine coal insert for the fixed-bed pressure gasifier is also significantly reduced compared to the raw coal, which also reduces the mechanical wear of the gasifier during operation with the fine coal insert produced according to the invention.
  • the second mineral type is therefore formed from clay minerals, in particular from kaolinite.
  • the first defined limit density is preferably between 1.8 and 2.1 g / cm 3 , preferably 1.9 g / cm 3 . It is further preferred if, in the method according to the invention, the second defined limit density is between 1.4 and 1.8 g / cm 3 , preferably 1.6 g / cm 3 .
  • common raw coal can be separated with certain density separation steps into a carbon-enriched light material, a heavy material enriched with minerals of the first type and a medium-density medium material, the latter, for example, being discarded as a waste fraction.
  • At least one, preferably both, density separation stages is designed as heavy turbidity separation devices, and the respective cloud density corresponds to the first and / or second defined limit density.
  • Appropriate devices are provided by the trade.
  • the setting of the respective cloud density by using suitable heavy substances is known from the prior art.
  • Further crushing of the first light material is preferably carried out before being fed to the second density separation stage. In this way, a larger proportion of the first light goods can be transferred to the second light goods and the proportion of the medium goods is reduced.
  • the heavy goods processing includes the intermediate storage, homogenization and classification and the heavy goods fine fraction obtained in this way is removed from the heavy goods processing and at least partially mixed with the second light goods to the fine coal insert.
  • the heavy goods processing includes the intermediate storage, homogenization and classification and the heavy goods fine fraction obtained in this way is removed from the heavy goods processing and at least partially mixed with the second light goods to the fine coal insert.
  • the fixed-bed pressure gasifier is particularly preferably an FBDB-type gasifier, the feedstock and / or the ash resting on a rotating grate during operation of the gasifier.
  • a stable operation of an FBDB coal gasifier requires an ash bed that is stable enough to support the weight of the coal bed and allows an even and homogeneous distribution of the gas flow through the fixed bed. This is made possible by ash or clinker particles which form from the use of fine coal according to the invention under gasification conditions.
  • a further embodiment of the method according to the invention is characterized in that the middle goods obtained are further comminuted and at least partially returned to method step 1 (a). In this way, portions of the middle goods can be transferred to the light goods and / or the heavy goods and the waste fraction is reduced.
  • At least one, preferably both, density separation stages is designed as heavy turbidity separation devices and the respective cloud density corresponds to the first and / or second defined limit density.
  • Appropriate devices are provided by the trade.
  • the setting of the respective cloud density by using suitable heavy substances is known from the prior art.
  • the system further comprises a comminution device which is spatially and / or connected to the first and the second density separation stage in terms of the process sequence and is suitable for further comminuting the first light material before it is fed to the second density separation stage.
  • a comminution device which is spatially and / or connected to the first and the second density separation stage in terms of the process sequence and is suitable for further comminuting the first light material before it is fed to the second density separation stage.
  • the plant according to the invention is designed such that the heavy goods processing stage further comprises the following plant components: an intermediate store, a homogenization device, a classification device, means for discharging the heavy goods fine fraction obtained from the heavy goods processing stage, means for at least partially Mixing the heavy goods fine fraction with the second light goods to the fine coal insert.
  • the heavy goods processing stage further comprises the following plant components: an intermediate store, a homogenization device, a classification device, means for discharging the heavy goods fine fraction obtained from the heavy goods processing stage, means for at least partially Mixing the heavy goods fine fraction with the second light goods to the fine coal insert.
  • the term "line” is to be understood in a generalized manner and includes not only pipelines in the narrower sense, but also all other conveying methods and conveying devices known per se to those skilled in mechanical process engineering, such as conveyor belts, screw conveyors, trough chain conveyors, pneumatic conveying systems, etc .; they are not explained further here and are shown in detail. Depending on the nature of the material to be conveyed, the person skilled in the art will be able to select the most suitable funding method.
  • Fig. 1 schematically illustrated, preferred embodiment of the method according to the invention or the system according to the invention is introduced into system 1 for producing the fine coal insert for a fixed bed pressure gasifier of the FBDB type with rotating grate via line 2 comminuted raw coal.
  • the raw coal used here is associated with bedrock that includes different mineral types. These also include kaolinite, which is particularly intimately associated with the coal it contains and runs through it as fine passages or veins.
  • the raw coal reaches the first density separation stage 3 via line 2, which is equipped as a heavy turbidity separation device.
  • the cloud density is set to a first defined limit density between 1.8 and 2.1 g / cm 3 , preferably 1.9 g / cm 3 .
  • the mountains or the heavy material enriched in bedrock, i.e. the mineral or bedrock fraction, which contains only a small proportion of coal are separated from the remaining raw coal and discharged via line 11 from the first density separation stage.
  • the solid fraction with a density lower than the first defined limit density is discharged via line 4 as the first light material enriched in carbon from the first density separation stage and fed to the second density separation stage 5.
  • the cloud density is set to a second defined limit density between 1.4 and 1.8 g / cm 3 , preferably to 1.6 g / cm 3 .
  • this second density separation stage which in turn is designed as a heavy turbidity separation device, a solid fraction with a density lower than the second specified limit density as carbon-enriched second light material and a solid fraction with a density greater than the second specified limit density as medium value are discharged via line 6 which is discharged from the process via line 7 and discarded as waste.
  • the second light material is fed to a storage container 8 and temporarily stored therein.
  • the heavy material discharged via line 11 from the first density separation stage is fed to a homogenization and intermediate storage device 12. From this it is discharged via line 13 and fed to a classification device 14 equipped with a series of sieves of different mesh sizes.
  • the coarse fraction obtained during classification is discharged from the classification device via line 16 and discarded as waste.
  • the heavy material fine fraction obtained during the classification is discharged via line 15, to a homogenization device 10 and in this at least partially with the second light material, which comes via line 9 from the storage container 8 is discharged and also led to the homogenization device, mixed with the fine coal insert, which is discharged via line 17 from the plant 1 and can now be fed to a fixed-bed pressure gasification reactor.
  • the invention proposes a method and a system for producing a fine coal insert for a fixed-bed pressure gasifier from raw coal associated with bedrock, which forms an ash or clinker layer under gasification conditions, which has very good support and gasification properties.
  • the crushing and mixing action of the rotating grate from the fine coal insert obtained according to the invention results in an ash bed with gasification conditions obtained under gasification conditions, which is improved compared to ash beds which are obtained from fine coal inserts according to the prior art are.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Processing Of Solid Wastes (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Claims (13)

  1. Procédé de fabrication d'un insert de fines de charbon à partir de charbon brut associé à des épontes en tant que matière première pour un gaséificateur sous pression à lit fixe, comprenant les étapes suivantes de :
    (a) fourniture de charbon brut broyé,
    (b) introduction du charbon brut broyé dans un premier étage de séparation de densité, adapté à la séparation de particules solides en fractions présentant des densités, qui sont inférieures et supérieures à une première densité limite fixée,
    (c) évacuation d'une fraction solide présentant une densité inférieure à la première densité limite fixée en tant que première matière légère enrichie en carbone et une fraction solide présentant une densité supérieure à la première densité limite fixée en tant que matière lourde enrichie en épontes,
    (d) introduction de la première matière légère dans un second étage de séparation de densité, adapté à la séparation de particules solides en fractions présentant des densités, qui sont inférieures et supérieures à une seconde densité limite fixée,
    (e) évacuation d'une fraction solide présentant une densité inférieure à la seconde densité limite fixée en tant que seconde matière légère enrichie en outre en carbone et une fraction solide présentant une densité supérieure à la seconde densité limite fixée en tant que matière moyenne,
    (f) introduction de la matière lourde dans un dispositif de transformation de matières lourdes, comprenant au moins une étape de traitement, choisie parmi le groupe : stockage intermédiaire, broyage, homogénéisation, calibrage ; évacuation d'une matière lourde traitée du dispositif de transformation de matières lourdes,
    (g) mélange d'au moins une partie de la matière lourde traitée avec la seconde matière légère dans l'insert de fines de charbon.
  2. Procédé selon la revendication 1, caractérisé en ce que le charbon brut est associé à des épontes, qui contiennent au moins deux types de minéraux différents, dans lequel le premier type de minéral fond ou se ramollit au moins partiellement dans les conditions de réaction de la gazéification sous pression à lit fixe et le second type de minéral reste solide dans les mêmes conditions de réaction et le second type de minéral adhère mieux au charbon ou est associé plus profondément à celui-ci.
  3. Procédé selon la revendication 2, caractérisé en ce que le second type de minéral est formé à partir de minéraux argileux, en particulier à partir de kaolinite.
  4. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la première densité limite fixée est comprise entre 1,8 et 2,1 g/cm3, de préférence est de 1,9 g/cm3.
  5. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la seconde densité fixée est comprise entre 1,4 et 1,8 g/cm3, de préférence est de 1,6 g/cm3.
  6. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'au moins un, de préférence les deux étages de séparation de densité sont conçus en tant que dispositifs de séparation par lame et la densité de la boue respective correspond à la première et/ou à la seconde densités limites fixées.
  7. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la première matière légère est broyée en outre avant l'introduction dans le second étage de séparation de densité.
  8. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le dispositif de transformation de matières lourdes comprend le stockage intermédiaire, l'homogénéisation et le calibrage et en ce que la partie fine des matières lourdes ainsi obtenue à partir du dispositif de transformation de matières lourdes est évacuée et au moins mélangée partiellement à la seconde matière légère dans l'insert de fines de charbon.
  9. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que pour le gaséificateur sous pression à lit fixe, il s'agit d'un gaséificateur de type FBDB et en ce que lors du fonctionnement du gaséificateur, la matière première et/ou les cendres reposent sur une grille tournante.
  10. Installation destinée à fabriquer un insert de fines de charbon à partir de charbon brut contenant des minéraux en tant que matière première pour un gaséificateur sous pression à lit fixe, comprenant les groupes de construction et les composants de l'installation suivants :
    (a) des moyens destinés à fournir le charbon brut broyé contenant des minéraux,
    (b) un premier étage de séparation de densité, adapté à la séparation de particules solides dans des fractions présentant des densités, qui sont inférieures et supérieures à une première densité limite fixée, des moyens destinés à introduire le charbon brut broyé contenant des minéraux dans le premier étage de séparation de densité,
    (c) des moyens destinés à évacuer une fraction solide présentant une densité inférieure à la première densité limite fixée en tant que première matière légère et des moyens destinés à évacuer une fraction solide présentant une densité supérieure à la première densité limite fixée en tant que matière lourde,
    (d) un second étage de séparation de densité, adapté à la séparation de particules solides en fractions présentant des densités, qui sont inférieures et supérieures à une seconde densité limite fixée, des moyens destinés à introduire la première matière légère dans le second étage de séparation de densité,
    (e) des moyens destinés à évacuer une fraction solide présentant une densité inférieure à la seconde densité limite fixée en tant que seconde matière légère et des moyens destinés à évacuer une fraction solide présentant une densité supérieure à la seconde densité limite fixée en tant que matière moyenne,
    (f) un étage de transformation des matières lourdes, comprenant au moins un dispositif, choisi parmi le groupe : stockage intermédiaire, dispositif de broyage, dispositif d'homogénéisation, dispositif de calibrage ; des moyens destinés à introduire la matière lourde dans l'étage de transformation des matières lourdes, des moyens destinés à évacuer une matière lourde traitée de l'étage de transformation des matières lourdes,
    (g)un dispositif de mélange destiné à mélanger au moins une partie de la matière lourde traitée à la seconde matière légère dans l'insert de fines de charbon.
  11. Installation selon la revendication 10,
    caractérisée en ce qu'au moins un, de préférence deux étages de séparation de densité sont conçus en tant que dispositifs de séparation par lame et la densité de la boue respective correspond à la première et/ou à la seconde densité limite fixée.
  12. Installation selon l'une quelconque des revendications précédentes, caractérisée en ce qu'en outre un dispositif de broyage est compris, qui est relié et adapté aux premier et second étages de séparation de densité, pour broyer en outre la première matière légère avant l'introduction dans le second étage de séparation de densité.
  13. Installation selon l'une quelconque des revendications précédentes, caractérisée en ce que l'étage de transformation des matières lourdes comprend en outre les composants de l'installation suivants : un stockage intermédiaire, un dispositif d'homogénéisation, un dispositif de calibrage, des moyens destinés à évacuer la partie fine des matières lourdes obtenue de l'étage de transformation de matières lourdes, des moyens destinés à mélanger au moins partiellement la partie fine des matières lourdes à la seconde matière légère dans l'insert de fines de charbon.
EP17400030.7A 2017-06-08 2017-06-08 Charge de fines de charbon pour un gazéificateur sous pression à lit fixe Active EP3412754B1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP17400030.7A EP3412754B1 (fr) 2017-06-08 2017-06-08 Charge de fines de charbon pour un gazéificateur sous pression à lit fixe
PCT/EP2018/025142 WO2018224186A1 (fr) 2017-06-08 2018-05-18 Charge d'alimentation en charbon fin pour gazéifieur à lit fixe sous pression
CN201810576476.8A CN109022039B (zh) 2017-06-08 2018-06-06 用于固定床加压气化器的粉煤进料
CN201820875258.XU CN209652248U (zh) 2017-06-08 2018-06-06 用于从原煤生产粉煤进料的设备

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP17400030.7A EP3412754B1 (fr) 2017-06-08 2017-06-08 Charge de fines de charbon pour un gazéificateur sous pression à lit fixe

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EP3412754A1 EP3412754A1 (fr) 2018-12-12
EP3412754B1 true EP3412754B1 (fr) 2020-08-05

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CN112076885A (zh) * 2020-08-17 2020-12-15 天地（唐山）矿业科技有限公司 一种煤矸石中煤系高岭土的富集工艺
CN112474033B (zh) * 2020-11-05 2022-04-29 阜新工大矿物加工利用科技有限公司 煤泥预先脱泥分选工艺
CN113609793B (zh) * 2021-07-01 2023-05-23 华电电力科学研究院有限公司 一种用于制粉系统实现煤粉均匀分配的节流元件调控方法
CN114712895B (zh) * 2022-03-08 2023-04-28 江南大学 提高模拟移动床产率的带额外色谱柱的双部分丢弃方法

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CA1091622A (fr) * 1976-08-16 1980-12-16 James D. Deimler No translation available
IT1139273B (it) * 1981-10-22 1986-09-24 Prominco Srl Procedimento per la separazione dinamica a mezzo denso di miscele di materiali,quali ad esempio minerali,a diverso peso specifico,ed impianto per attuarlo
HUT53560A (en) * 1987-10-06 1990-11-28 Haldex Vallalat Method for separating the granules of coal and dead from aqueous suspension in two-stage hydrocyclone system
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CN209652248U (zh) 2019-11-19
CN109022039B (zh) 2021-07-02
WO2018224186A1 (fr) 2018-12-13
EP3412754A1 (fr) 2018-12-12
CN109022039A (zh) 2018-12-18

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