EP0370201B1 - Process for operating a plant for the gasification of solid fuels, and suited operating plant - Google Patents

Process for operating a plant for the gasification of solid fuels, and suited operating plant Download PDF

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Publication number
EP0370201B1
EP0370201B1 EP89117731A EP89117731A EP0370201B1 EP 0370201 B1 EP0370201 B1 EP 0370201B1 EP 89117731 A EP89117731 A EP 89117731A EP 89117731 A EP89117731 A EP 89117731A EP 0370201 B1 EP0370201 B1 EP 0370201B1
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EP
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Prior art keywords
gasification
flue dust
fuel
process according
dust
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EP89117731A
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German (de)
French (fr)
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EP0370201A1 (en
Inventor
Karl-Heinz Dutz
Adolf Linke
Norbert Ullrich
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Krupp Koppers GmbH
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Krupp Koppers GmbH
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • 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 generally to the gasification of fine-grained to dust-like solid fuels.
  • Solid fuels refer in particular to hard coal, coke, petroleum coke and the like.
  • the gasification takes place with oxygen and / or air and possibly water vapor in the entrained flow and leads to a raw gas consisting mainly of carbon monoxide and hydrogen.
  • the raw gas carries with it dust that has a share of residual carbon.
  • the gasification is pressure gasification.
  • the invention relates to a method for operating a system for the gasification of fine-grained and dust-like solid fuels with a gasification reactor, which is equipped with gasification burners, device for the separation of dust from the raw gas, dust collection container and device for the recycling of dust into the gasification reactor, the gasification burner having a Burn the rotationally symmetrical fuel / reactant jet into the gasification reactor at the gasification burner outlet and a primary reaction zone of high temperature is formed by the fuel / reactant jets in the gasification reactor. It also relates to a system that is specially set up for operation in accordance with this method. - In the expression fuel / reactant jet, reactant denotes both the oxidizing agent and reaction products already formed and, if appropriate, also moderator gas and carrier gas.
  • the fly dust is mixed with the fresh fuel and fed to the gasification burners together with the fuel special treatment of the dust, namely extensive and complicated technical facilities with large safety precautions.
  • the pore space or gap space of the flue dust extracted from the raw gas is filled with the raw gas containing carbon monoxide and hydrogen, which has to be diluted or removed only below the hazard limit by repeated application and pumping with inert gas.
  • the treatment of the raw gas separated from the flying dust is also cumbersome and complex, since it often contains sulfur and, for reasons of environmental protection, cannot be flared, burned or released into the atmosphere. Incidentally, it disturbs that the fly dust added to the fresh fuel reduces the calorific value of the fuel, which influences the thermodynamics and the reaction kinetics of the gasification process.
  • the invention has for its object to carry out the method described in such a way that, without special treatment of the fly dust and without disturbing the thermodynamics or reaction kinetics of the gasification process, a sufficiently complete integration of the fly dust into the slag can be achieved, with simultaneous combustion of the Residual carbon.
  • the invention teaches that the fly dust with its raw gas and residual carbon content is introduced into the axis of at least one fuel / reactant jet by a conveying gas stream, introduced into the primary reaction zone and melted in the jet.
  • the flying dust is introduced through the axis of the respective gasification burner.
  • the gasification reaction already begins in the fuel-reactant stream and is not disturbed by the flying dust here or in the primary reaction zone, which contributes to the fact that its residual carbon is also gasified.
  • the volume flow of airborne dust must not be chosen too large.
  • the usual high temperatures of, for example, 2000 ° C. and more arise in the primary reaction zone, which are required for the melting of the flying dust.
  • the fly dust is scarcely discharged from the primary reaction zone more than usual and without the fly dust recirculation described. The fly dust does not accumulate in the untreated raw gas, so that the described cycle management is possible.
  • gasification burners which have a feed channel for primary oxygen which is coaxial with the gasification burner axis and a surrounding ring channel for have the fuel supply and an annular channel surrounding it indirectly or directly for the supply of secondary oxygen.
  • the invention recommends feeding the fly dust in the axis of the feed channel for the primary oxygen through a special feed channel.
  • the primary oxygen flow can be divided into two concentric partial flows.
  • the gasification burners are set up for supplying a flow of flue dust that is smaller by a factor of 0.01 to 0.15 than the fuel flow. This applies practically proportionally to other designs of the gasification burner.
  • the invention also relates to a plant which is particularly suitable for carrying out the method. It is explained in more detail below with the aid of a drawing. - The only drawing shows the diagram of a system according to the invention.
  • the basic structure of the plant shown in the figure consists of a gasification reactor 1, which is equipped with gasification burners 2, a device 3 for separating the dust from the raw gas, a dust collecting container 4 with a device for returning the dust into the gasification reactor 1.
  • the gasification burners 2 burn with a fuel / reactant jet 5 which is rotationally symmetrical at the gasification burner outlet into the gasification reactor 1 into it and create a primary reaction zone 6 of high temperature.
  • the gasification burners 2 have a central feed duct 7 for the flying dust. This is surrounded by an annular channel 8 for the supply of primary oxygen.
  • the arrangement is also such that the central feed channels 7 are connected to the dust collector 4 via a metering device 9. - It goes without saying that the gasification burner 2 can otherwise be set up as usual in the gasification of solid fuels.
  • the raw gas loaded with the dust comes through the line 10 into the device 3 for the dust separation, which is designed as a separating cyclone.
  • the dust is separated here.
  • the separated fly dust which still contains raw gas in its pore space or gap space, falls through line 11 into the fly dust collection container 4.
  • the dosing device 9 is operated from this fly dust collection container 4. It includes two allotment containers 12. Periodically, the two allotment containers 12 are filled via lines 13 from the dust collection container 4 by free fall.
  • the feed container 12, which is filled with fly dust is pressurized through a line 14 with purified raw gas or inert gas, which is only slightly above the pressure in the gasification reactor 1.
  • the airborne dust is introduced through the lines 15 under sufficient pressure via the line 16 into the lines which open into the gasification burners 2. They open into the central feed channel 7 for the fly dust, which is surrounded by the ring channel 8 for the feed of primary oxygen.
  • the lines 17 are expansion lines for the respective empty emptying containers 12 and lead into the line 18 outgoing from the device 3 for the dust collection for the cleaned raw gas.

Description

Die Erfindung bezieht sich allgemein auf die Vergasung von feinkörnigen bis staubförmigen festen Brennstoffen. Feste Brennstoffe bezeichnet insbesondere Steinkohle, Koks, Petrolkoks und dergleichen. Die Vergasung geschieht mit Sauerstoff und/oder Luft und gegebenenfalls Wasserdampf im Flugstrom und führt zu einem Rohgas aus hauptsächlich Kohlenmonoxid und Wasserstoff. Das Rohgas führt Flugstaub mit, der einen Anteil an Restkohlenstoff aufweist. Die Vergasung ist eine Druckvergasung.The invention relates generally to the gasification of fine-grained to dust-like solid fuels. Solid fuels refer in particular to hard coal, coke, petroleum coke and the like. The gasification takes place with oxygen and / or air and possibly water vapor in the entrained flow and leads to a raw gas consisting mainly of carbon monoxide and hydrogen. The raw gas carries with it dust that has a share of residual carbon. The gasification is pressure gasification.

Die Erfindung betrifft konkret ein Verfahren zum Betrieb einer Anlage für die Vergasung feinkörniger und staubförmiger fester Brennstoffe mit Vergasungsreaktor, der mit Vergasungsbrennern ausgerüstet ist, Einrichtung für die Flugstaubabscheidung aus dem Rohgas, Flugstaubsammelbehälter und Einrichtung für die Flugstaubrückführung in den Vergasungsreaktor, wobei die Vergasungsbrenner mit einem am Vergasungsbrenneraustritt rotationssymmetrischen Brennstoff/Reaktionsmittel-Strahl in den Vergasungsreaktor hineinbrennen und von den Brennstoff/Reaktionsmittel-Strahlen in dem Vergasungsreaktor eine Primärreaktionszone hoher Temperatur gebildet wird. Sie betrifft fernerhin eine Anlage, die für den Betrieb entsprechend diesem Verfahren besonders eingerichtet ist. - Im dem Ausdruck Brennstoff/Reaktionsmittel-Strahl bezeichnet Reaktionsmittel sowohl die Oxidationsmittel als auch bereits gebildete Reaktionsprodukte und gegebenenfalls auch Moderatorgas sowie Trägergas.Specifically, the invention relates to a method for operating a system for the gasification of fine-grained and dust-like solid fuels with a gasification reactor, which is equipped with gasification burners, device for the separation of dust from the raw gas, dust collection container and device for the recycling of dust into the gasification reactor, the gasification burner having a Burn the rotationally symmetrical fuel / reactant jet into the gasification reactor at the gasification burner outlet and a primary reaction zone of high temperature is formed by the fuel / reactant jets in the gasification reactor. It also relates to a system that is specially set up for operation in accordance with this method. - In the expression fuel / reactant jet, reactant denotes both the oxidizing agent and reaction products already formed and, if appropriate, also moderator gas and carrier gas.

Im Rahmen der bekannten Maßnahmen, von denen die Erfindung ausgeht (EP 0 072 457 B1, EP 0 109 109 B1) wird der Flugstaub dem frischen Brennstoff beigemischt und zusammen mit dem Brennstoff den Vergasungsbrennern zugeführt .Das ist aufwendig und erfordert eine besondere Aufbereitung des Flugstaubes, nämlich umfangreiche und komplizierte technische Einrichtungen mit großen Sicherheitsvorkehrungen. Der Porenraum oder Lückenraum des aus dem Rohgas abgezogenen Flugstaubes ist mit dem Kohlenmonoxid und Wasserstoff enthaltenden Rohgas gefüllt, welches erst durch mehrmaliges Beaufschlagen und Umpumpen mit Inertgas bis unter die Gefahrengrenze verdünnt oder entfernt werden muß. Auch die Behandlung des aus dem Flugstaub abgetrennten Rohgases ist umständlich und aufwendig, da es häufig schwefelhaltig ist und aus Gründen des Umweltschutzes weder abgefackelt noch sonstwie verbrannt oder an die Atmosphäre abgegeben werden kann. Im übrigen stört, daß der dem frischen Brennstoff beigemischte Flugstaub den Heizwert des Brennstoffes reduziert, was die Thermodynamik und die Reaktionskinetik des Vergasungsprozesses beeinflußt.As part of the known measures, from which the invention is based (EP 0 072 457 B1, EP 0 109 109 B1), the fly dust is mixed with the fresh fuel and fed to the gasification burners together with the fuel special treatment of the dust, namely extensive and complicated technical facilities with large safety precautions. The pore space or gap space of the flue dust extracted from the raw gas is filled with the raw gas containing carbon monoxide and hydrogen, which has to be diluted or removed only below the hazard limit by repeated application and pumping with inert gas. The treatment of the raw gas separated from the flying dust is also cumbersome and complex, since it often contains sulfur and, for reasons of environmental protection, cannot be flared, burned or released into the atmosphere. Incidentally, it disturbs that the fly dust added to the fresh fuel reduces the calorific value of the fuel, which influences the thermodynamics and the reaction kinetics of the gasification process.

Der Erfindung liegt die Aufgabe zugrunde, das eingangs beschriebene Verfahren so zu führen, daß ohne besondere Aufbereitung des Flugstaubes sowie ohne störende Beeinflussung der Thermodynamik oder Reaktionskinetik des Vergasungsprozesses eine ausreichend vollständige Einbindung des Flugstaubes in die Schlacke erreicht werden kann, und zwar bei gleichzeitigter Verbrennung des Restkohlenstoffes.The invention has for its object to carry out the method described in such a way that, without special treatment of the fly dust and without disturbing the thermodynamics or reaction kinetics of the gasification process, a sufficiently complete integration of the fly dust into the slag can be achieved, with simultaneous combustion of the Residual carbon.

Zur Lösung dieser Aufgabe lehrt die Erfindung, daß der Flugstaub mit seinem Gehalt an Rohgas und seinem Restkohlenstoff durch einen Fördergasstrom in die Achse von zumindest einem Brennstoff/Reaktionsmittel-Strahl eingeführt, von diesem in die Primärreaktionszone eingebracht und in dieser eingeschmolzen wird. Nach bevorzugter Ausführungsform der Erfindung wird der Flugstaub durch die Achse des jeweiligen Vergasungsbrenners eingeführt. - Die Erfindung nutzt die Tatsache, daß bei Vergasung mit rotationssymmetrischen Brennstoff/Reaktionsmittel-Strahlen, die zur Vergasung fester Brennstoffe eingesetzt werden, die Brennstoff/Reaktionsmittel-Strahlen in gasdynamischer Hinsicht sehr stabil sind und einen Flugstaubmengenstrom in die Primärreaktionszone hineintragen können. Die Vergasungsreaktion beginnt bekanntlich bereits in dem Brennstoff-Reaktionsmittel-Strom und wird hier sowie in der Primärreaktionszone durch den Flugstaub nicht gestört, wozu beiträgt, daß auch deren Restkohlenstoff vergast wird. Der Mengenstrom an Flugstaub darf allerdings nicht zu groß gewählt werden. In der Primärreaktionszone entstehen die üblichen hohen Temperaturen, von beispielsweise 2000°C und mehr, die für das Einschmelzen des Flugstaubes erforderlich sind. Überraschenderweise wird trotz der erfindungsgemäßen Flugstaubrückführung aus der Primärreaktionszone der Flugstaub kaum stärker ausgetragen als üblich und ohne die beschriebene Rückführung von Flugstaub. Im ungereinigten Rohgas reichert sich der Flugstaub nicht störend an, so daß die beschriebene Kreislaufführung möglich ist. - Grundsätzlich ist es bekannt, Flugstaub in einen Vergasungsreaktor zurückzuführen (DE 24 09 008 C2), und zwar über besondere, von den Vergasungsbrennern getrennte Zuführungsdüsen. Das beeinträchtigt die Vergasungsreaktion und hat in die Praxis kaum Eingang gefunden. In der Praxis ist es eher üblich (DE-AS 23 25 204), den Flugstaub in einem Reaktor auf die Schlacke aufzublasen, wobei im allgemeinen auch der mitgeführte Restkohlenstoff in die Schlacke geht.To achieve this object, the invention teaches that the fly dust with its raw gas and residual carbon content is introduced into the axis of at least one fuel / reactant jet by a conveying gas stream, introduced into the primary reaction zone and melted in the jet. According to a preferred embodiment of the invention, the flying dust is introduced through the axis of the respective gasification burner. - The invention uses the The fact that in gasification with rotationally symmetrical fuel / reactant jets, which are used for the gasification of solid fuels, the fuel / reactant jets are very stable in terms of gas dynamics and can carry a flow of flue dust into the primary reaction zone. As is known, the gasification reaction already begins in the fuel-reactant stream and is not disturbed by the flying dust here or in the primary reaction zone, which contributes to the fact that its residual carbon is also gasified. However, the volume flow of airborne dust must not be chosen too large. The usual high temperatures of, for example, 2000 ° C. and more arise in the primary reaction zone, which are required for the melting of the flying dust. Surprisingly, in spite of the fly dust recirculation according to the invention, the fly dust is scarcely discharged from the primary reaction zone more than usual and without the fly dust recirculation described. The fly dust does not accumulate in the untreated raw gas, so that the described cycle management is possible. - Basically, it is known to recycle fly dust into a gasification reactor (DE 24 09 008 C2), specifically via feed nozzles that are separate from the gasification burners. This affects the gasification reaction and has hardly found its way into practice. In practice, it is rather common (DE-AS 23 25 204) to blow up the flying dust in a reactor onto the slag, the residual carbon carried in general also going into the slag.

Im einzelnen bestehen mehrere Möglichkeiten der weiteren Ausbildung des erfindungsgemäßen Verfahrens. Vorteilhaft wird mit Vergasungsbrennern gearbeitet, die einen zur Vergasungsbrennerachse koaxialen Zuführungskanal für Primärsauerstoff, einen umgebenden Ringkanal für die Brennstoffzuführung und einen diesen mittelbar oder unmittelbar umgebenden Ringkanal für die Zuführung von Sekundärsauerstoff aufweisen. Hier empfiehlt die Erfindung, den Flugstaub in der Achse des Zuführungskanals für den Primärsauerstoff durch einen besonderen Zuführungskanal zuzuführen. Der Primärsauerstoffstrom kann in zwei konzentrische Teilströme aufgeteilt werden. Um die Vergasungsreaktion nicht zu beeinträchtigen, empfiehlt es sich, so vorzugehen, daß die Vergasungsbrenner für die Zuführung eines Flugstaubmengenstromes eingerichtet sind, der um einen Faktor von 0,01 bis 0,15 kleiner ist als der Brennstoffmengenstrom. Das gilt praktisch proportional für andere Auslegungen des Vergasungsbrenners. Diese Abstimmung läßt sich bei üblichen Vergasungsreaktoren des eingangs beschriebenen Aufbaus ohne Schwierigkeiten dann verwirklichen, wenn der Flugstaub über alle Vergasungsbrenner zugeführt wird. Zusätzliche Maßnahmen für die Sauerstoffzuführung und die Regelung der Sauerstoffzuführung sind nicht erforderlich. Vielmehr genügt es, daß die Menge des Primärsauerstoffes und/oder des Sekundärsauerstoffes nach Maßgabe des Restkohlenstoffgehaltes im Flugstaub erhöht wird.There are several options for further developing the method according to the invention. It is advantageous to work with gasification burners which have a feed channel for primary oxygen which is coaxial with the gasification burner axis and a surrounding ring channel for have the fuel supply and an annular channel surrounding it indirectly or directly for the supply of secondary oxygen. Here, the invention recommends feeding the fly dust in the axis of the feed channel for the primary oxygen through a special feed channel. The primary oxygen flow can be divided into two concentric partial flows. In order not to interfere with the gasification reaction, it is advisable to proceed in such a way that the gasification burners are set up for supplying a flow of flue dust that is smaller by a factor of 0.01 to 0.15 than the fuel flow. This applies practically proportionally to other designs of the gasification burner. In conventional gasification reactors of the construction described in the introduction, this adjustment can be achieved without difficulty if the flying dust is supplied via all gasification burners. Additional measures for the oxygen supply and the regulation of the oxygen supply are not necessary. Rather, it is sufficient that the amount of the primary oxygen and / or the secondary oxygen is increased in accordance with the residual carbon content in the fly dust.

Gegenstand der Erfindung ist auch eine Anlage die für die Durchführung des Verfahrens besonders geeignet ist. Sie wird im folgenden anhand einer Zeichnung näher erläutert. - Die einzige Zeichnung zeigt das Schema einer erfindungsgemäßen Anlage.The invention also relates to a plant which is particularly suitable for carrying out the method. It is explained in more detail below with the aid of a drawing. - The only drawing shows the diagram of a system according to the invention.

Die in der Figur dargestellte Anlage besteht in ihrem grundsätzlichen Aufbau aus einem Vergasungsreaktor 1, der mit Vergasungsbrennern 2 ausgerüstet ist, einer Einrichtung 3 für die Flugstaubabscheidung aus dem Rohgas, einem Flugstaubsammelbehälter 4 mit Einrichtung für die Flugstaubrückführung in den Vergasungsreaktor 1. Die Vergasungsbrenner 2 brennen mit am Vergasungsbrenneraustritt rotationssymmetrischen Brennstoff/Reaktionsmittel-Strahl 5 in den Vergasungsreaktor 1 hinein und erzeugen in diesem eine Primärreaktionszone 6 hoher Temperatur. Wie sich aus dem vergrößerten Ausschnitt A ergibt, besitzen die Vergasungsbrenner 2 einen zentralen Zuführungskanal 7 für den Flugstaub. Dieser ist von einem Ringkanal 8 für die Zuführung von Primärsauerstoff umgeben. Die Anordnung ist fernerhin so getroffen, daß die zentralen Zuführungskanäle 7 über eine Dosiereinrichtung 9 an den Flugstaubsammelbehälter 4 angeschlossen sind. - Es versteht sich, daß die Vergasungsbrenner 2 im übrigen wie bei der Vergasung von festen Brennstoffen üblich eingerichtet sein können.The basic structure of the plant shown in the figure consists of a gasification reactor 1, which is equipped with gasification burners 2, a device 3 for separating the dust from the raw gas, a dust collecting container 4 with a device for returning the dust into the gasification reactor 1. The gasification burners 2 burn with a fuel / reactant jet 5 which is rotationally symmetrical at the gasification burner outlet into the gasification reactor 1 into it and create a primary reaction zone 6 of high temperature. As can be seen from the enlarged section A, the gasification burners 2 have a central feed duct 7 for the flying dust. This is surrounded by an annular channel 8 for the supply of primary oxygen. The arrangement is also such that the central feed channels 7 are connected to the dust collector 4 via a metering device 9. - It goes without saying that the gasification burner 2 can otherwise be set up as usual in the gasification of solid fuels.

Aus dem Vergasungsreaktor 1 gelangt das mit Flugstaub beladene Rohgas durch die Leitung 10 in die Einrichtung 3 für die Flugstaubabscheidung, die als Abscheidezyklon ausgeführt ist. Hier wird der Flugstaub abgetrennt. Der abgetrennte Flugstaub, der in seinem Porenraum oder Lückenraum noch Rohgas enthält, fällt durch die Leitung 11 in den Flugstaubsammelbehälter 4.Aus diesem Flugstaubsammelbehälter 4 wird die Dosiereinrichtung 9 bedient. Zu ihr gehören zwei Zuteilbehälter 12. Periodisch werden aus dem Flugstaubsammelbehälter 4 durch freien Fall die beiden Zuteilbehälter 12 über Leitungen 13 gefüllt. Der jeweils mit Flugstaub gefüllte Zuteilbehälter 12 wird durch eine Leitung 14 mit gereinigtem Rohgas oder Inertgas unter einen Druck gesetzt, der nur unwesentlich über dem Druck im Vergasungsreaktor 1 liegt. Durch die Leitungen 15 wird der Flugstaub unter ausreichenden Druck über die Leitung 16 in die Leitungen eingeführt, die in den Vergasungsbrennern 2 münden. Sie münden in den zentralen Zuführungskanal 7 für den Flugstaub, der von dem Ringkanal 8 für die Zuführung von Primärsauerstoff umgeben ist. Die Leitungen 17 sind Entspannungsleitungen für die jeweils geleerten Zuteilbehälter 12 und führen in die aus der Einrichtung 3 für die Flugstaubabscheidung abgehende Leitung 18 für das gereinigte Rohgas. - Es versteht sich, daß das Verfahren von den Hilfsmitteln der modernen Verfahrenstechnik begleitet werden muß. Dazu werden die üblichen Meß- und Regelorgane eingebaut und werden die erforderlichen Regel- und Steuerungsmaßnahmen rechnergestützt durchgeführt. (Vgl. P 38 13 357.1)

Figure imgb0001
From the gasification reactor 1, the raw gas loaded with the dust comes through the line 10 into the device 3 for the dust separation, which is designed as a separating cyclone. The dust is separated here. The separated fly dust, which still contains raw gas in its pore space or gap space, falls through line 11 into the fly dust collection container 4. The dosing device 9 is operated from this fly dust collection container 4. It includes two allotment containers 12. Periodically, the two allotment containers 12 are filled via lines 13 from the dust collection container 4 by free fall. The feed container 12, which is filled with fly dust, is pressurized through a line 14 with purified raw gas or inert gas, which is only slightly above the pressure in the gasification reactor 1. The airborne dust is introduced through the lines 15 under sufficient pressure via the line 16 into the lines which open into the gasification burners 2. They open into the central feed channel 7 for the fly dust, which is surrounded by the ring channel 8 for the feed of primary oxygen. The lines 17 are expansion lines for the respective empty emptying containers 12 and lead into the line 18 outgoing from the device 3 for the dust collection for the cleaned raw gas. - It goes without saying that the process must be accompanied by the aids of modern process engineering. For this purpose, the usual measuring and regulating elements are installed and the necessary regulating and control measures are carried out with the aid of a computer. (See P 38 13 357.1)
Figure imgb0001

Diese Mengenrelationen ergeben sich aus folgenden Gründen:
80% der in den Vergasungsreaktor mit dem Brennstoff eingesetzten Asche werden als Schlacke ausgetragen, 20 % der Achse plus unvergaster Kohlenstaub werden mit dem Gas ausgetragen. 80 % der im Gas enthaltenen Feststoffe (Flugstaub) werden in dem Flugstaubabscheider abgeschieden und unter den beschriebenen Bedingungen in die Vergasungsbrenner zurückgeführt.These quantity relations result for the following reasons:
80% of the ashes placed in the gasification reactor with the fuel are discharged as slag, 20% of the axis plus ungasified coal dust are discharged with the gas. 80% of the solids (airborne dust) contained in the gas are separated in the airborne dust separator and returned to the gasification burner under the conditions described.

Claims (7)

1. Process for the operation of a plant for the gasification of fine-grained to powdered solid fuels, having a
   gasification reactor which is equipped with gasification burners,
   device for the separation of flue dust from the crude gas,
   flue dust collection tank, and device for the return of flue dust to the gasification reactor,
in which the gasification burners burn into the gasification reactor with a rotationally symmetrical fuel/reaction medium jet at the gasification burner outlet, and a primary reaction zone of high temperature is formed by the fuel/reaction medium jets in the gasification reactor, characterized in that the flue dust with its crude gas content and its carbon residue is introduced by a carrier gas stream into the axis of at least one fuel/ reaction medium jet, and is introduced into the primary reaction zone by the fuel/reaction medium jet and melted down therein.
2. Process according to Claim 1, characterized in that the flue dust is introduced through the axis of the gasification burner in question.
3. Process according to one of Claims 1 or 2, in which gasification burners which have a supply channel for primary oxygen which is coaxial with the axis of the gasification burner, a surrounding annular channel for the fuel supply, and an annular channel surrounding the latter for the supply of secondary oxygen are used, characterized in that the flue dust in the axis of the supply channel for the primary oxygen is fed in by a special supply channel.
4. Process according to one of Claims 1 to 3, characterized in that the gasification burners are designed for the infeed of a flue dust mass flow which. is a factor of 0.01 to 0.15 smaller than the fuel mass flow.
5. Process according to one of Claims 1 to 4, characterized in that the quantity of primary oxygen and/or of secondary oxygen is increased according to the carbon residue content in the flue dust.
6. Process according to one of Claims 1 to 5, characterized in that the flue dust is fed in via all gasification burners.
7. Plant for carrying out the process according to one of Claims 1 to 5, which has the basic layout indicated in Claim 1, characterized in that the gasification burners (2) have a central supply channel (7) for the flue dust which is surrounded by an annular channel (8) for the infeed of primary oxygen, and in that the central supply channels (7) are connected to the flue dust collection tank (4) by means of a metering device (9).
EP89117731A 1988-11-05 1989-09-26 Process for operating a plant for the gasification of solid fuels, and suited operating plant Expired - Lifetime EP0370201B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3837587A DE3837587C1 (en) 1988-11-05 1988-11-05
DE3837587 1988-11-05

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EP0370201A1 EP0370201A1 (en) 1990-05-30
EP0370201B1 true EP0370201B1 (en) 1992-06-17

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EP89117731A Expired - Lifetime EP0370201B1 (en) 1988-11-05 1989-09-26 Process for operating a plant for the gasification of solid fuels, and suited operating plant

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EP (1) EP0370201B1 (en)
CN (1) CN1025867C (en)
DD (1) DD285990A5 (en)
DE (3) DE3837587C1 (en)
DK (1) DK548489A (en)
ES (1) ES2033504T3 (en)
PL (1) PL161778B1 (en)
ZA (1) ZA897381B (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4132770A1 (en) * 1991-10-02 1993-04-08 Kurt Kugler Treatment of incinerator airborne ash and dust - comprises sepg. into coarse and fine fractions and removing heavy metals
DE4407651C1 (en) * 1994-03-08 1995-10-26 Rheinische Braunkohlenw Ag Prodn. of synthesis gas from by-prods., by steam-oxygen@ gasification,
US7540891B2 (en) 2003-10-31 2009-06-02 Shell Oil Company System and method for stripping toxigas from a powder
PL224212B1 (en) 2012-10-12 2016-11-30 Sarre Piotr Method for gasification of coal-bearing raw materials, and coal char and layout of equipment for performing this process

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL171691C (en) * 1973-02-26 1983-05-02 Shell Int Research PROCESS FOR THE PREPARATION OF HYDROGEN AND / OR CARBON MONOXIDE-CONTAINING GASES BY INCOMPLETE BURNING OF FUELS AND SEPARATION OF THE SOLID PARTICLES THEREFORE.
US3929429A (en) * 1974-09-26 1975-12-30 Texaco Inc Fuel gas from solid carbonaceous fuels
US4168956A (en) * 1977-08-18 1979-09-25 Combustion Engineering, Inc. Method of operating a coal gasifier
DE2947222A1 (en) * 1979-11-23 1981-05-27 Carbon Gas Technologie GmbH, 4030 Ratingen METHOD FOR GASIFYING SOLID, DUST-MADE TO PIECE-LIKE CARBONATED MATERIAL
DE3132506A1 (en) * 1981-08-18 1983-03-03 Hoechst Ag, 6000 Frankfurt METHOD AND DEVICE FOR PRODUCING SYNTHESIS GAS
DE3372867D1 (en) * 1982-11-11 1987-09-10 Shell Int Research Process for the partial combustion of solid fuel with fly ash recycle
US4480559A (en) * 1983-01-07 1984-11-06 Combustion Engineering, Inc. Coal and char burner

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PL161778B1 (en) 1993-07-30
ES2033504T3 (en) 1993-03-16
EP0370201A1 (en) 1990-05-30
DE58901693D1 (en) 1992-07-23
ZA897381B (en) 1990-07-25
DK548489A (en) 1990-05-06
DD285990A5 (en) 1991-01-10
DE3941816A1 (en) 1991-06-20
CN1025867C (en) 1994-09-07
DK548489D0 (en) 1989-11-03
DE3837587C1 (en) 1990-05-23
CN1042560A (en) 1990-05-30

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