EP1201731A1 - Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification - Google Patents

Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification Download PDF

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Publication number
EP1201731A1
EP1201731A1 EP00123186A EP00123186A EP1201731A1 EP 1201731 A1 EP1201731 A1 EP 1201731A1 EP 00123186 A EP00123186 A EP 00123186A EP 00123186 A EP00123186 A EP 00123186A EP 1201731 A1 EP1201731 A1 EP 1201731A1
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European Patent Office
Prior art keywords
zone
gasification
fluidized bed
post
dust
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Application number
EP00123186A
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German (de)
English (en)
Inventor
Bernd Prof. Dr. Meyer
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RWE Power AG
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RWE Rheinbraun AG
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Priority to EP00123186A priority Critical patent/EP1201731A1/fr
Publication of EP1201731A1 publication Critical patent/EP1201731A1/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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
    • 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
    • C10J2200/158—Screws
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Definitions

  • the invention relates to a method for gasifying solid, carbonaceous substances in a fluidized bed according to the Preamble of claim 1 and a carburetor according to the Preamble of claim 22.
  • the after-treatment in whatever way, is an additional process step that increases costs.
  • a thermal aftertreatment is either done in a separate Fluid bed steam generator or in a so-called Oxidator or sulfator performed.
  • the separation of gasification (Carbonizer) and post-oxidation of the C-containing gasification residues (Steam generator boiler) is also in the concepts the so-called second generation (see e.g. EP 707137, EP 544350 and EP 698726).
  • DE 19548324 C2 describes the supply of gasification material and gasifying agents to the fluidized bed such that a uniform radial flow profile and a constant or slightly increasing axial flow velocity adjust in fluidized bed (optimization of fluid dynamics and the reaction turnover of the gasification).
  • Another The proposal provides for those carried upwards from the fluidized bed C-containing dust-like solids in one Direction of flow of gas downstream of the fluidized bed Further gasification zone and gasification agent also to be introduced into the post-gasification zone (EP 0214417). at Applying these two suggestions can increase the rate of the C conversion to values between 90 and a maximum of 95% to reach. An additional oxidative aftertreatment of the gasification residues is also necessary here.
  • waste is gasified, it can be used instead of the post-gasification zone in a second gasification stage following the fluidized bed an entrained flow gasifier can be provided in which a complete gasification of the C-containing dust at temperatures takes place above the slag melting point (DE 4435349).
  • the goal is to decompose organic trace substances high temperatures and the non-elutable integration of Heavy metals in the slag.
  • the technical investment and experience the specific gasification agent consumption a sharp increase. Significant advantages of fluidized bed gasification against entrained-flow gasification are lost.
  • the invention has for its object the method and carburetor of the type described in the introduction so that a complete gasification of the feed materials and in If necessary, an oxidation of the mineral gasification residues at least to the extent that the Residue product without further ado, in particular without additional Treatment that can be deposited.
  • the predominant gasification of the feedstocks and the dust takes place with the first gasification agents, whereby ash granulation takes place at the same time, which, if necessary, takes place depending on the melting point of the ash of the solids used, using an additional gasification agent with a higher O 2 content.
  • the solid gasification residues that form in the fluidized bed zone are residual coke from the feed materials and the returned dust, as well as ash granulate and non-granulated ash.
  • the dust-containing raw gas is separated from the fluidized bed zone with raw gas dust loads of 1-10 kg / m 3 iN . Since the fluidized bed generally has no stationary upper boundary, a transition area will form between the fluidized bed and the splash zone, in which parts of the dust initially entrained with the gas fall back into the fluidized bed and another part of the dust is carried along by the gas, so that it comes to the aforementioned dust load with which the gas flows through the subsequent zones.
  • the above-described effect can be promoted in that the splash zone widens conically at least in its lower region, so that there, ie essentially in the aforementioned transition region, there is a reduction in the flow velocity of the gas.
  • first post-gasification zone under the fluidized bed zone finds a post-gasification of the fluidized bed down discharged residual coke instead of the residues of the input materials and the returned dust.
  • This Post-gasification takes place using second gasification agents, which is a loosening of that in the first post-gasification zone existing solid cause without however, a fluidized bed in the sense of complete fluidization sets, while at the same time the segregation of the Ash granules take place in such a way that it sinks downwards and accumulates in the second post-gasification zone.
  • the first post-gasification zone forming solid C-containing Gasification residues are residual coke from the bottom product of the Fluidized bed and non-granulated ash.
  • the second post-gasification zone which is the bottom discharge of the first post-gasification zone and the carburetor as a whole can be the most complete gasification possible of the C content of the residues and the oxidation of the ash with a third gasifier as well as cooling the as Bottom product of solid gasification residues to be discharged from the gasifier carried out.
  • the discharged soil product consists of largely C-free, oxidized ash and Ash granules.
  • the ash granulate is due to its The prevailing conditions are essentially free of calcium sulfide.
  • the first gasification agent which may also be blown into the fluidized bed from above, serves for the predominant gasification of the C-containing feedstocks in the fluidized bed zone. It consists of preheated air, air / steam or O 2 / steam mixtures with the typical compositions known for fluidized bed gasification, optionally with additions of other gases, for example N 2 and CO 2 .
  • the reaction of the C-containing feed with the gasification agents takes place in the fluidized bed zone at temperatures between 750 and 950 ° C, higher temperatures being able to occur locally in the areas in which O 2 -containing gasification agent is blown in, so that depending on Melting point of the ashes of the feedstock, the temperatures which occur at least locally when using the gasification agents containing O 2, exceed the ash melting point and thus cause granulation of at least a large part of the ash constituents.
  • These requirements can e.g. B. be present in the gasification of Rhenish lignite, the ash of which has a melting point of about 1250 ° C.
  • the solids forming the fluidized bed predominantly moving upward in the central region and downward in the vicinity of the circumference of the gasifier receiving the fluidized bed, it can be assumed that a large part of the solid particles are particularly affected by the in the peripheral areas of the fluidized bed, which represent areas of higher temperature, pass through, the C-containing constituents of these particles being converted as far as possible and the remaining ash constituents agglomerating into coarse-grained granules, the individual bodies of which have a diameter of several millimeters.
  • the conditions required with regard to the temperature can be present in the case of such an input material, for example, when the first gasification agents consisting of a mixture of O 2 and steam with a steam / O 2 ratio of 1 1 kg / m 3 iN are used.
  • additional gasifying agents When using C-containing solids with ashes, the melting point of which is noticeably higher, it may be necessary to inject additional gasifying agents to granulate the ashes in the fluidized bed zone. This can be the case, for example, when gasifying hard coal, the ash of which has a melting point of, for. B. 1450 - 1500 ° C.
  • the oxygen content of the additional gasifying agent will be ⁇ 21 vol.% In some areas of the fluidized bed in order to set the required higher temperature.
  • These additional gasifying agents can, for example, O 2 / steam mixtures with a steam / O 2 ratio in the range from 0.3-1 kg / m 3 iN and / or from air preheated to 400-600 ° C.
  • additional gasification agents can be mixed with other gases, for example NH 3 or purge gases or other gases to be disposed of, since the higher temperature which arises at the nozzle outlet in the fluidized bed in any case leads to a cleavage of higher molecular weight compounds, with gases being formed in the gas cleaning downstream of the carburetor can be removed without additional problems and / or additional expenditure being required.
  • gases for example NH 3 or purge gases or other gases to be disposed of, since the higher temperature which arises at the nozzle outlet in the fluidized bed in any case leads to a cleavage of higher molecular weight compounds, with gases being formed in the gas cleaning downstream of the carburetor can be removed without additional problems and / or additional expenditure being required.
  • the composition and / or temperature of the additional gasifying agent adjusted so that the Temperature in the flame, which is determined by the injection Gasification agent nozzles in the fluidized bed, sufficient is high at the given ash softening point melt granulation of the ashes in this flame cause.
  • Volatile alkalis, volatile metals and others inorganic trace substances are largely formed in the Ash granules incorporated so that they do not elute can be.
  • composition of the second gasification agents which are introduced into the first gasification zone for the purpose of post-gasification, is similar to that of the first gasification agents, the composition being able to be adapted by increasing the addition of further endothermic gasification agents such as CO 2 and water vapor, so that the temperature of each Place of the first post-gasification zone is limited to values below the ash softening.
  • the third gasification agents are used for the complete gasification of the remaining C components and for the oxidation of the ashes in the second post-gasification zone in the floor fume cupboard. They can be blown into the second post-gasification zone in several superimposed areas or levels. If necessary, there is the possibility of gasifying agents of different compositions in the individual levels, for example consisting of water, O 2 / steam, O 2 / CO 2 and O 2 / steam / CO 2 mixtures or of water, air, air / Blow in steam, air / CO 2 , air / steam / CO 2 mixtures.
  • the use of different gasification agents at different heights in the second post-gasification zone can result from the fact that, on the one hand, the carbon-containing residues should be converted as far as possible and, if necessary, the ash or the granules should also be oxidized, but on the other hand the temperature is kept below and below the ash melting point End product is to be discharged from the second gasification zone, which has cooled so far that it can be handled with the usual means of transport, equipment, etc.
  • the composition and amount of the third gasification agent are therefore adjusted so that the C content of the soil product leaving the second post-gasification zone is reduced to the values required for landfilling.
  • the final residue which essentially consists of ash and ash granulate, should be cooled before it leaves the gasifier.
  • the oxygen content of the third gasifying agent will normally be ⁇ 21% by volume.
  • the speed at which at the end of the second gasification zone remaining solid residues z. B. by means of a Screw conveyor are discharged from the carburetor essentially determined by the residence time of the solids in the carburetor, given the conditions, especially the temperatures required to achieve the desired To achieve the degree of gasification of the carbon.
  • the first gasification agents are one or more Nozzle levels, each consisting of several gasifying agent nozzles, into the fluidized bed zone and possibly also via an additional one Nozzle level diagonally from above to the upper limit the fluidized bed zone.
  • This additional jet plane is at the transition between the fluidized bed zone and the Splashzone or be arranged slightly above, where, as already mentioned, generally not exactly defined upper limit of the fluidized bed zone is present, because of its upper range is usually several, for example 100 mm will move up and down.
  • the one about this additional Nozzle plane sloping down to the upper limit of the Fluidized bed blown first gasifier can too a certain equalization of the upper limit or serve the upper region of the fluidized bed and above also due to the downward, i.e.
  • directed flow component help that too much solid from the fluidized bed zone with the raw gas leaving the latter is discharged, since the top of the upper areas of the fluidized bed acting gas flows part of that from the fluidized bed zone escaping dust down again, i.e. into the fluidized bed zone back "press". This leads to a longer one Residence time of these solids in the fluidized bed, which The fact again the gasification efficiency of the whole System improved.
  • Gasifying agent nozzles which are also in at least one plane can be arranged in the gasifier blown gasifier are not intended to be essential in the splash zone additional reactions with that from the fluidized bed zone to cause discharged dust. Rather should they are at least predominantly in the upper range of the Implement the fluidized bed zone with the carbon present there.
  • additional gasification agent required for granulation the ashes are preferably over a nozzle plane or via several individual gasifying agent nozzles into the fluidized bed zone blown. Composition, quantity and preheating temperature of these additional gasifying agents are so set that the ash granulation to the desired extent takes place.
  • the ash is granulated at much lower ash softening temperatures than with gasification processes in which constantly part of the ash-containing solids from the gasification system is carried out. According to the eutectics being formed there is a lowering of the softening point of the total ash in general significantly more than 100 K compared to the Softening points of the individual ash fractions. This is a Advantage over z. B.
  • composition of the ash components ash granulation also causes a shift the particle size range of the solid inventory in the fluidized bed to larger grain diameters so that the gas flow rate if the same solids discharges are observed can be increased, increasing the specific carburetor output increases.
  • the dust-containing raw gas is cooled in the cooling zone and the heat dissipation by means of a heat exchanger which at a distance of 1 - 5 m above the upper limit arranged in the fluidized bed zone and preferably helical is designed as a bulkhead heating surface.
  • the heat exchanger cools the dusty raw gas to a temperature in the Range of 350 - 700 ° C and carries cooling heat in the form of saturated and / or heated steam.
  • a cooling of the Raw gas at temperatures below 350 ° C is generally inappropriate because then there is a risk that tar hydrocarbons and / or other condensable components on the Heat exchanger surfaces and the downstream filter for condense the dust separation.
  • the dust carried with the raw gas essentially consists of residual coke with a C content of ⁇ 20% by mass. From the experience gained with HTW gasification it is known that from a minimum C content of this size and a dust load of ⁇ 1 - 10 kg / m 3 iN no caking at the entrance z. B. form in the heat exchanger. Due to the high dust load of the gas, there is a self-cleaning effect on the heat exchanger surfaces.
  • the raw gas outlet from the Dedusting zone arranged in the cooling zone takes place as far as possible complete separation of the contained in the cooled raw gas Dust.
  • One can preferably be used as a blind separator trained pre-separator may be provided, of which the partially dedusted, cooled raw gas is fed into an absolute filter which is directly instead of the usual cyclone connects to the carburetor.
  • the absolute filter in which the Raw gas is almost completely dust-free preferably from a candle filter with ceramic or metallic Filter elements.
  • the absolute filter together with the dust become volatile Alkalis and heavy metals as well as volatile organic and organic trace and pollutants separated.
  • a temperature optimum the dust separation in the absolute filter is approx 500 - 700 ° C. At these temperatures there is a practical complete alkali separation and a sufficiently high one Trace substance adsorption with adequate heat extraction in the heat exchanger.
  • the one in the dedusting zone is separated cooled dust by means of gravity via feedback systems, in the simplest case consisting of one of internals free return line, completely into the fluidized bed zone and thus preferably returned to the lower part.
  • feedback systems in the simplest case consisting of one of internals free return line, completely into the fluidized bed zone and thus preferably returned to the lower part.
  • the pressure difference between the entry point in the fluidized bed and the absolute filter is low, so that gas barriers or transportation aids in the return zone can be.
  • the first post-gasification zone In the first post-gasification zone, the first stage of the Post-gasification of the residual coke from the fluidized bed zone and the Segregation of the ash granules formed in the fluidized bed zone.
  • the second gasification agent is over preferably blown in a nozzle plane.
  • the C content of the solids leaving the first post-gasification zone - these are due to the input materials and the returned dust Residual coke as well as ash and ash granulate - is thereby Lowered values ⁇ 20% by mass.
  • the third gasification agent in the Countercurrent to that formed in the second post-gasification zone Moving bed preferably over several nozzles or Nozzle planes arranged at vertical distances from each other can be blown into the second post-gasification zone.
  • the third gasification agent can also use so-called open nozzle bottoms, i.e. from below.
  • the third gasification agents are distributed in such a way that in preferably two or three at different heights arranged nozzles gasifying agent of different composition be fed.
  • a gasifier in the lower Quench water As a gasifier in the lower Quench water is injected, which evaporates and as steam in the gasification zones above flows in which it acts as an endothermic gasifying agent.
  • the cooling of the lowest area of the solid residues located in the second post-gasification zone causes.
  • the endothermic end of the quench water Gasifying agents are in a first and possibly also in one second area above it contains oxygen-containing gasifying agents admixed so that in the third post-gasification zone in those above the supply of quench water Areas of the C content of the solids to an allowable maximum salary, e.g. B.
  • the specified speed ranges take into account the wide range of material properties of the C-containing feedstocks.
  • the process according to the invention in which the gasification agents are introduced into the fluidized bed zone and the two post-gasification zones, makes it possible to introduce gasification agents into the zone located above the fluidized bed, which is referred to as "post-gasification zone" in gasification processes according to the prior art , to renounce.
  • This post-gasification zone of known gasifiers has the disadvantage of a low specific reaction conversion of the endothermic gasification reactions and consequently a correspondingly large specific reactor volume and exergetic losses as a result of the indispensable water quench at the outlet of the post-gasification zone above the fluidized bed.
  • the formation of ash and slag mixtures due to incompletely avoidable, local and temporary excess temperatures in the raw gas represents a further disadvantage.
  • the ash granulation in the fluidized bed gasification reactor in a centrally located vertical combustion jet over which the entire gasification air or amount of gasification oxygen supplied without subdivision becomes. There is no complete gasification or Oxidation of the C-containing soil product. A thermal aftertreatment is required in any case.
  • the application of the invention becomes essential procedural and plant simplifications achieved, for example the elimination of thermal aftertreatment the gasification residues and noticeable simplifications in raw gas cooling and cleaning.
  • cooling and return of the dust to the fluidized bed zone as completely as possible there is separation, recirculation, decomposition and / or incorporation of a variety of volatile organic and inorganic compounds and pollutants.
  • Which resulting positive effects on the subsequent Gas cleaning process can be used depending on the C-containing substances and the process control different his.
  • the sulfur inclusion in the own ash and / or basic additives used for in-situ desulfurization be admitted improved.
  • the C content of the feedstocks practically completely thermally and materially used can be, which leads to a noticeable increase in thermal Efficiency of the gasification as well as the overall process leads.
  • the insert coal 2 is introduced into the fluidized bed zone 4 of the fluidized bed gasifier 1 via one or more feed devices 3, which use, for example, a screw conveyor.
  • the first gasification agent 5 is blown into the fluidized bed zone 4 by means of four nozzle planes 6 to 9 arranged one above the other.
  • the gasification agent 5 consists of compressed, 350 ° C hot air with the addition of 0.18 kg of water vapor per m 3 iN air.
  • Each of the nozzle levels 6 to 9 has a plurality of gasifying agent nozzles 10, which are each distributed uniformly over the circumference of the fluidized bed gasifier 1 in one level.
  • the arrangement of the gasification agent nozzles in each case in one plane is advantageous not least because of the uniformity of the gasification agent entry into the fluidized bed and the resulting easier calculation of the flow conditions in the fluidized bed.
  • an arrangement is also conceivable in which not several nozzles are arranged in one plane each.
  • Gasification agent 11 is blown in through the nozzles 10 of the nozzle plane 12. The latter is located between the two nozzle levels 7 and 8 for the first gasifying agent 5.
  • the additional Gasifying agent 11 consists of oxygen enriched Air with an oxygen content of 30% by volume. It has a Temperature of 350 ° C. The oxygen content is sufficient high to melt granulation in the brown coal used the ash above the ash softening temperature of e.g. B. 1200 ° C and the formation of ash granules. In the ash granules become the volatile alkalis and heavy metals not integrated elutable.
  • the one with the extra Amount of oxygen supplied to gasifying agent 11 about 45% of those supplied with the first gasifying agent 5 Amount of oxygen.
  • the dust load of the raw gas 14 emerging upward from the fluidized bed is reduced to a value of approximately 1 kg / m 3 iN until it enters the cooling zone 15 arranged downstream of the splash zone 13 in the flow direction of the raw gas ,
  • the C content of the dust is about 40% by mass.
  • the nozzles 10 of the other gasification agent levels 6 - 8 and 12 are in the direction of flow of the gasifying agents passing through them diagonally upward so as to fluidize the to promote solids in the fluidized bed zone.
  • the dust-containing raw gas 14 When passing through the cooling zone 15, the dust-containing raw gas 14 becomes cooled to 600 ° C.
  • the heat exchanger consisting of one Evaporator 16 with a superheater 17 connected downstream is helical executed as a bulkhead heating surface.
  • the dusty, cooled raw gas 18 leaves the cooling zone 15 via the raw gas outlet 19 and arrives in the dedusting zone 20. It flows through first one designed as a blind separator Pre-separator 21 that separates most of the dust that gets into the dust collecting chamber 22 of the candle filter 23.
  • the Dusty, cooled raw gas 18 is then completely dedusted in the candle filter 23. It leaves this as dust-free, chilled raw gas 24.
  • the total separated dust 25 is constituted by gravity via the return zone 26 from a return line 38 free of internals, into which lower part of the fluidized bed zone 4 returned.
  • the dust free Raw gas 24 meets the requirements of the gas turbine the low dust content and the permissible content of volatile alkalis.
  • a second gasification agent 28 is blown in via the nozzles 10 arranged in the plane 29.
  • the second gasification agent 28 consists of compressed, 350 ° C hot air with the addition of 0.33 kg of water vapor / m 3 iN .
  • the amount of oxygen supplied with the gasifying agent 28 is approximately 15% of the amount of oxygen supplied with the first gasifying agent 5.
  • a temperature of 800-850 ° C. is established in the first post-gasification zone 27.
  • the distance to the ash softening temperature is sufficiently high to avoid caking.
  • the C content of the solids passing from the first post-gasification zone into the second post-gasification zone located below it is reduced to about 10% by mass by the post-gasification in the post-gasification zone 27.
  • the first is enough Post-gasification zone loosening, which leads to the fact that the heavier ash agglomerates that are in the fluidized bed zone 4 formed in the manner already described have to sink down faster than the smaller residual coke particles, that still contain C components and therefore longer in stay in the first post-gasification zone 27, in order also in This first post-gasification zone still has a noticeable C conversion to allow for a correspondingly lower C content of the residual coke, which leads to the first post-gasification zone 27 leaves below and into the second post-gasification zone 30 arrives, which results in the discharge area 31 of the carburetor 1 represents from which the solid residues of the gasification process are discharged from the carburetor.
  • the solids in the second post-gasification zone 30 form a moving bed moving from top to bottom, into which third gasifying agent 32 are introduced, without a substantial loosening of the moving bed occurring.
  • different gasification agents are introduced in the two levels 35 and 36.
  • quench water 33 is introduced, by means of which the bottom product 37 leaving the second post-gasification zone 30 below is cooled to 450 ° C. under evaporative cooling.
  • compressed air 350 at 350 ° C. is located in level 36 above level 35 with an addition of 0.17 kg steam / m 3 in air blown.
  • the amount of oxygen supplied with this second post-gasification agent is approximately 2.5% of the amount of oxygen which is blown into the fluidized bed zone with the first gasification agent.
  • a temperature is established in the second post-gasification zone of a maximum of 850 ° C.
  • the distance to the ash softening temperature is big enough to avoid caking.
  • the level of the upper nozzle level 36 is sufficient for the solids Contact with the free oxygen-containing gas atmosphere, so that the oxidation of calcium sulfide-containing ash takes place.
  • the nozzles 10 of the nozzle planes 29 and 36 in the first and second post-gasification zone are analogous to the nozzles 10 of the nozzle planes 6 - 8 and 12 also obliquely in the direction of flow arranged at the top.
  • the nozzles 10 in the Level 35 in which the quench water is supplied, for example analogous to the nozzle level 9 directed downwards so that the discharge to support the gasification residues from the carburetor.
  • a small amount of nitrogen is used as sealing gas 39 from below to prevent water vapor from penetrating into the one below existing facilities for discharging the soil product (not shown) entered.
  • a fluidized bed gasifier 1 for a thermal output of 1100 MW th has a clear diameter of 1.1 m in the second post-gasification zone 30.
  • the clear diameter of the cooling zone is 3.7 m.
  • a cooling heat of 156 MW th is dissipated in the cooling zone 15 in the form of superheated steam. 600,000 m 3 iN / h of raw gas (raw gas calorific value H u 5.02 MJ / m 3 iN ), corresponding to a raw gas calorific value flow of 837 MW th , are generated.

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  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
EP00123186A 2000-10-26 2000-10-26 Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification Withdrawn EP1201731A1 (fr)

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Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10343582A1 (de) * 2003-09-18 2005-05-19 Rwe Power Ag Verfahren und Vorrichtung zur Wirbelschichtvergasung mit Flüssigschlackeabzug
WO2007090585A1 (fr) * 2006-02-06 2007-08-16 Rwe Power Aktiengesellschaft Procede et reacteur de gazeification avec extraction du laitier liquide
DE102007006980A1 (de) 2007-02-07 2008-08-14 Technische Universität Bergakademie Freiberg Verfahren zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DE102007006982A1 (de) 2007-02-07 2008-08-14 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DE102008009132A1 (de) 2007-02-07 2008-08-21 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zum Verbrennen fester Brennstoffe
WO2012110236A1 (fr) * 2011-02-17 2012-08-23 European Charcoal Ag Production de carbone et de gaz combustibles à partir de lignite
WO2014093308A1 (fr) 2012-12-10 2014-06-19 Southern Company Gazéifieur de second étage dans une gazéification étagée
DE102013101945A1 (de) * 2013-02-27 2014-08-28 Thyssenkrupp Uhde Gmbh Verfahren zur Weiterverwertung von Nebenprodukten aus Vergasungsanlagen
DE102013107311A1 (de) * 2013-07-10 2015-01-15 Thyssenkrupp Industrial Solutions Ag Verfahren und Vorrichtung zur Nachbehandlung des bei der Vergasung anfallenden C-haltigen Bodenproduktes
EP2862914A1 (fr) * 2013-10-16 2015-04-22 Syncraft Engineering GmbH Procédé de réglage destiné au fonctionnement d'un gazéificateur à lit mobile et d'un réacteur à lit mobile
CN107312575A (zh) * 2017-08-01 2017-11-03 中国科学院工程热物理研究所 分级配风的循环流化床气化装置以及气化方法
DE102016210348A1 (de) * 2016-06-10 2017-12-14 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Nachoxidation von kohlenstoffhaltigen Vergasungsprodukten
DE102016210350A1 (de) 2016-06-10 2017-12-14 Technische Universität Bergakademie Freiberg Vergasungsreaktor zur Erzeugung von Synthesegasen aus festen Vergasungsstoffen mit Hilfe sauerstoffhaltiger Vergasungsmittel
DE102016214242A1 (de) * 2016-08-02 2018-02-08 Thyssenkrupp Ag Anlage und Verfahren zur Umwandlung kohlenstoffhaltiger Brennstoffe in Synthesegas
DE102016223318A1 (de) * 2016-11-24 2018-05-24 Thyssenkrupp Ag Verfahren und Anlage zur Kohlenstoff-Reduzierung im Bodenprodukt eines Wirbelschichtvergasers
CN108219846A (zh) * 2018-03-28 2018-06-29 程石 一种利用城市废弃物、生物质制燃气的装置
WO2018228946A1 (fr) 2017-06-14 2018-12-20 Thyssenkrupp Industrial Solutions Ag Système de post-traitement et procédé pour réaliser le post-traitement d'au moins des gaz en aval d'une gazéification en lit fluidisé ainsi qu'unité logique et utilisation
DE102017219783A1 (de) * 2017-11-07 2019-05-09 Thyssenkrupp Ag Vorrichtung und Verfahren zum Vergasen von Einsatzstoffen und zum Bereitstellen von Synthesegas sowie Verwendung

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EP0214417A2 (fr) * 1985-09-02 1987-03-18 Rheinische Braunkohlenwerke AG. Procédé de production de gaz de synthèse à partir de combustibles solides
DE4340459C1 (de) * 1993-11-27 1995-05-18 Rheinische Braunkohlenw Ag Verfahren zum Betreiben eines Wirbelschichtreaktors zum Vergasen von kohlenstoffhaltigen Einsatzstoffen
DE4413923A1 (de) * 1994-04-21 1995-10-26 Rheinische Braunkohlenw Ag Verfahren zum Erzeugen von Synthesegas in der Wirbelschicht

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Publication number Priority date Publication date Assignee Title
EP0214417A2 (fr) * 1985-09-02 1987-03-18 Rheinische Braunkohlenwerke AG. Procédé de production de gaz de synthèse à partir de combustibles solides
DE4340459C1 (de) * 1993-11-27 1995-05-18 Rheinische Braunkohlenw Ag Verfahren zum Betreiben eines Wirbelschichtreaktors zum Vergasen von kohlenstoffhaltigen Einsatzstoffen
DE4413923A1 (de) * 1994-04-21 1995-10-26 Rheinische Braunkohlenw Ag Verfahren zum Erzeugen von Synthesegas in der Wirbelschicht

Cited By (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10343582A1 (de) * 2003-09-18 2005-05-19 Rwe Power Ag Verfahren und Vorrichtung zur Wirbelschichtvergasung mit Flüssigschlackeabzug
DE10343582B4 (de) * 2003-09-18 2006-01-12 Rwe Power Ag Verfahren und Vorrichtung zur Wirbelschichtvergasung fester, Kohlenstoffhaltiger Materialien mit Flüssigschlackeabzug
WO2007090585A1 (fr) * 2006-02-06 2007-08-16 Rwe Power Aktiengesellschaft Procede et reacteur de gazeification avec extraction du laitier liquide
DE102007006980A1 (de) 2007-02-07 2008-08-14 Technische Universität Bergakademie Freiberg Verfahren zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DE102007006982A1 (de) 2007-02-07 2008-08-14 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DE102008009132A1 (de) 2007-02-07 2008-08-21 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zum Verbrennen fester Brennstoffe
DE102007006980B4 (de) * 2007-02-07 2009-03-19 Technische Universität Bergakademie Freiberg Verfahren zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DE102007006982B4 (de) * 2007-02-07 2009-03-19 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DE102008009132B4 (de) * 2007-02-07 2011-01-27 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zum Verbrennen fester Brennstoffe
WO2012110236A1 (fr) * 2011-02-17 2012-08-23 European Charcoal Ag Production de carbone et de gaz combustibles à partir de lignite
EP2928590A4 (fr) * 2012-12-10 2016-09-21 Southern Co Gazéifieur de second étage dans une gazéification étagée
KR20150093783A (ko) * 2012-12-10 2015-08-18 서던 컴퍼니 단계식 가스화에서의 제 2 단 가스화기
JP2016505666A (ja) * 2012-12-10 2016-02-25 サザン カンパニー 段階的ガス化における第２段ガス化装置
WO2014093308A1 (fr) 2012-12-10 2014-06-19 Southern Company Gazéifieur de second étage dans une gazéification étagée
DE102013101945A1 (de) * 2013-02-27 2014-08-28 Thyssenkrupp Uhde Gmbh Verfahren zur Weiterverwertung von Nebenprodukten aus Vergasungsanlagen
DE102013107311A1 (de) * 2013-07-10 2015-01-15 Thyssenkrupp Industrial Solutions Ag Verfahren und Vorrichtung zur Nachbehandlung des bei der Vergasung anfallenden C-haltigen Bodenproduktes
EP2862914A1 (fr) * 2013-10-16 2015-04-22 Syncraft Engineering GmbH Procédé de réglage destiné au fonctionnement d'un gazéificateur à lit mobile et d'un réacteur à lit mobile
DE102016210350B4 (de) * 2016-06-10 2018-01-18 Technische Universität Bergakademie Freiberg Vergasungsreaktor zur Erzeugung von Synthesegasen aus festen Vergasungsstoffen mit Hilfe sauerstoffhaltiger Vergasungsmittel
DE102016210348A1 (de) * 2016-06-10 2017-12-14 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Nachoxidation von kohlenstoffhaltigen Vergasungsprodukten
DE102016210350A1 (de) 2016-06-10 2017-12-14 Technische Universität Bergakademie Freiberg Vergasungsreaktor zur Erzeugung von Synthesegasen aus festen Vergasungsstoffen mit Hilfe sauerstoffhaltiger Vergasungsmittel
WO2017211940A1 (fr) 2016-06-10 2017-12-14 Technische Universität Bergakademie Freiberg Réacteur de gazéification pour produire des gaz de synthèse à partir de matières solides à gazéifier, au moyen d'agents de gazéification contenant de l'oxygène
DE102016214242B4 (de) 2016-08-02 2023-03-02 Gidara Energy B.V. Anlage und Verfahren zur Umwandlung kohlenstoffhaltiger Brennstoffe in Synthesegas
DE102016214242A1 (de) * 2016-08-02 2018-02-08 Thyssenkrupp Ag Anlage und Verfahren zur Umwandlung kohlenstoffhaltiger Brennstoffe in Synthesegas
WO2018024404A1 (fr) 2016-08-02 2018-02-08 Thyssenkrupp Industrial Solutions Ag Installation et procédé de conversion de combustibles contenant du carbone en gaz de synthèse
DE102016223318A1 (de) * 2016-11-24 2018-05-24 Thyssenkrupp Ag Verfahren und Anlage zur Kohlenstoff-Reduzierung im Bodenprodukt eines Wirbelschichtvergasers
WO2018095781A1 (fr) 2016-11-24 2018-05-31 Thyssenkrupp Industrial Solutions Ag Procédé et système pour la réduction du carbone dans la fraction de queue d'un gazéificateur à lit fluidisé
RU2769442C2 (ru) * 2017-06-14 2022-03-31 ГИДАРА Энержи Б.В. Устройство дополнительной обработки и способ дополнительной обработки по меньшей мере газов после процесса газификации в псевдоожиженном слое, а также логический блок и его применение
WO2018228946A1 (fr) 2017-06-14 2018-12-20 Thyssenkrupp Industrial Solutions Ag Système de post-traitement et procédé pour réaliser le post-traitement d'au moins des gaz en aval d'une gazéification en lit fluidisé ainsi qu'unité logique et utilisation
DE102017210044A1 (de) 2017-06-14 2018-12-20 Thyssenkrupp Ag Nachbehandlungsanordnung und Verfahren zum Nachbehandeln von zumindest Gasen stromab einer Wirbelschichtvergasung sowie Logikeinheit und Verwendung
US11401476B2 (en) 2017-06-14 2022-08-02 Gidara Energy B.V. Aftertreatment arrangement and method for the aftertreatment of at least gases downstream of a fluid bed gasification system, and logic unit and use
CN107312575A (zh) * 2017-08-01 2017-11-03 中国科学院工程热物理研究所 分级配风的循环流化床气化装置以及气化方法
CN107312575B (zh) * 2017-08-01 2023-07-18 中国科学院工程热物理研究所 分级配风的循环流化床气化装置以及气化方法
DE102017219783A1 (de) * 2017-11-07 2019-05-09 Thyssenkrupp Ag Vorrichtung und Verfahren zum Vergasen von Einsatzstoffen und zum Bereitstellen von Synthesegas sowie Verwendung
CN108219846A (zh) * 2018-03-28 2018-06-29 程石 一种利用城市废弃物、生物质制燃气的装置

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