DE102009030542A1 - Fluidized bed reactor for producing gas product from carbon-containing materials through allothermal steam gasification, comprises combustion chamber with fluidized bed and reforming reactor with another fluidized bed and feeding device - Google Patents

Fluidized bed reactor for producing gas product from carbon-containing materials through allothermal steam gasification, comprises combustion chamber with fluidized bed and reforming reactor with another fluidized bed and feeding device Download PDF

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DE102009030542A1
DE102009030542A1 DE102009030542A DE102009030542A DE102009030542A1 DE 102009030542 A1 DE102009030542 A1 DE 102009030542A1 DE 102009030542 A DE102009030542 A DE 102009030542A DE 102009030542 A DE102009030542 A DE 102009030542A DE 102009030542 A1 DE102009030542 A1 DE 102009030542A1
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fluidized bed
reactor
reformer
reformer reactor
combustion chamber
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Markus Zankl
Georg Gallmetzer
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Highterm Research GmbH
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Highterm Research GmbH
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    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J8/1872—Details of the fluidised bed reactor
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    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
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    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
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    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/42—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles
    • C01B3/44—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles using the fluidised bed technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
    • C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
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    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/02—Multi-step carbonising or coking processes
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    • 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
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    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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    • 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
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    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
    • B01J2208/00221—Plates; Jackets; Cylinders comprising baffles for guiding the flow of the heat exchange medium
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    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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Abstract

A fluidized bed reactor comprises a combustion chamber (10) with a fluidized bed (12), where a reforming reactor (14) with another fluidized bed (16) and a feeding device (22) are also arranged on the combustion chamber. A heat transfer device (42) is designed in the latter fluidized bed for transporting heat from the former fluidized bed into the latter fluidized bed. A common reactor vessel (2) is provided with the former reforming reactor and the combustion chamber. The former reforming reactor is connected with a pyrolysis gas line with another reforming reactor (24).

Description

Die Erfindung betrifft einen Wirbelschichtreaktor zur Erzeugung von Produktgas aus kohlenstoffhaltigen Einsatzstoffen nach Anspruch 1.The The invention relates to a fluidized bed reactor for the production of Product gas from carbonaceous feedstocks according to claim 1.

Aus der EP 1 187 892 B1 ist ein sogenannter Heatpipe-Reformer zum Erzeugen von Brenngas aus kohlenstoffhaltigen Einsatzstoffen bekannt, bei dem mittels Wärmerohren in einer Brennkammer mit einer ersten Wirbelschicht erzeugte Wärme in einen über der Brennkammer angeordneten Reformer-Reaktor mit einer zweiten Wirbelschicht eingekoppelt wird. In dem Reformer-Reaktor wird durch allotherme Wasserdampfvergasung Produktgas aus den zu vergasenden Einsatzstoffen erzeugt wird. Der Prozess der allothermen Wasserdampfvergasung bzw. -Reformierung von kohlenstoffhaltigen Einsatzstoffen findet in drei Schritten statt: Trocknung, Pyrolyse und Reformierung. Im Heatpipe-Reformer treten alle drei Schritte zugleich im Reformer-Reaktor mit der zweiten Wirbelschicht auf. Allerdings wurde festgestellt, dass lediglich die Koksstaubschicht über der zweiten Wirbelschicht einen erhöhten Anteil an Reformierung aufweist, da Koks ähnlich wie Aktivkohle durch die hohe spezifische Oberfläche katalytische Eigenschaften besitzt. Insgesamt hat sich herausgestellt, dass die Reformierung nicht vollständig ist, so dass in dem Produktgas aus dem Reformer-Reaktor Teerverbindungen enthalten sind, die das Produktgas verunreinigen.From the EP 1 187 892 B1 a so-called heat pipe reformer for producing fuel gas from carbonaceous feedstocks is known in which heat generated by means of heat pipes in a combustion chamber with a first fluidized bed is coupled into a reformer reactor arranged above the combustion chamber with a second fluidized bed. In the reformer reactor, product gas is produced from the feedstocks to be gasified by allothermal steam gasification. The process of allothermal steam gasification or reforming of carbonaceous feedstocks takes place in three steps: drying, pyrolysis and reforming. In the heat pipe reformer, all three steps occur simultaneously in the reformer reactor with the second fluidized bed. However, it has been found that only the coke dust layer above the second fluidized bed has an increased amount of reforming since coke, like activated carbon, has catalytic properties due to the high specific surface area. Overall, it has been found that the reforming is not complete, so that in the product gas from the reformer reactor tar compounds are contained, which contaminate the product gas.

Es ist daher Aufgabe der vorliegenden Erfindung den aus der der EP 1 187 892 B1 bekannten Heatpipe-Reformer dahingehend zu verbessern, dass das darin erzeugte Produktgas einen geringeren Teeranteil aufweist.It is therefore an object of the present invention from the of EP 1 187 892 B1 known heat pipe reformer to the effect that the product gas produced therein has a lower tar content.

Die Lösung dieser Aufgabe erfolgt durch einen Wirbelschichtreaktor gemäß den Merkmalen des Anspruchs 1.The This problem is solved by a fluidized bed reactor according to the features of claim 1.

Durch das Vorsehen eines zweiten Reformer-Reaktors mit einer dritten Wirbelschicht wird die allotherme Wasserdampfvergasung aufgeteilt in Trocknung und Pyrolyse im ersten Reformer-Reaktor und Reformierung im zweiten Reformer-Reaktor. Der zweite Reformer-Reaktor ist als Wirbelschicht-Wärmeübertrager ausgebildet, so dass durch Eintauchen des zweiten Reformer-Reaktors in die erste Wirbelschicht in der Brennkammer die für die Reformierung nötige Wärme aus der ersten Wirbelschicht in die dritte Wirbelschicht des zweiten Reformer-Reaktors übertragen wird. Das Pyrolysegas aus dem ersten Reformer-Reaktor führt Feststoffe, wie Koks und Bettmaterial aus der zweiten Wirbelschicht des ersten Reformer-Reaktors mit sich, die im zweiten Reformer-Reaktor als Bettmaterial für die dritte Wirbelschicht dienen und für den Wärmeübergang, vornehmlich durch Strahlung, von der ersten Wirbelschicht in der Brennkammer in dritte Wirbelschicht in dem zweiten Reformer-Reaktor sorgen. Die dritte Wirbelschicht in dem zweiten Reformer-Reaktor wird durch das Pyrolysegas aus dem ersten Reformer-Reaktor Blasen bildend fluidisiert und sorgt für eine gute Durchmischung von katalytisch wirkenden Koksteilchen und Pyrolysegas.By the provision of a second reformer reactor with a third fluidized bed the allothermal steam gasification is divided into drying and pyrolysis in the first reformer reactor and reforming in the second Reforming reactor. The second reformer reactor is a fluidized bed heat exchanger formed so that by immersion of the second reformer reactor in the first fluidized bed in the combustion chamber for the Reforming necessary heat from the first fluidized bed transferred to the third fluidized bed of the second reformer reactor becomes. The pyrolysis gas from the first reformer reactor leads Solids, such as coke and bed material from the second fluidized bed the first reformer reactor in the second reformer reactor serve as bed material for the third fluidized bed and for the heat transfer, mainly through Radiation, from the first fluidized bed in the combustion chamber into third Fluidized bed in the second reformer reactor provide. The third fluidized bed in the second reformer reactor is by the pyrolysis of the first reformer reactor forms bubbles forming fluidized and provides for a good mixing of catalytically active coke particles and pyrolysis gas.

Diese Aufteilung der Prozesse auf zwei Reaktoren ermöglicht, dass die Trocknung und Pyrolyse bei niedrigeren Temperaturen (< 850°C) und die Reformierung bei höheren Temperaturen (ca. 900°C) erfolgen kann. Teere werden im Temperaturbereich über 850°C und um 900°C in Anwesenheit von Koks als Katalysator und einem Überschuss an Wasserdampf gespalten und reformiert. Die durch das Koks katalytisch unterstützte Reformierung bei Temperaturen um 900°C ergibt ein nahezu teerfreies Produktgas mit hohem Wasserstoffanteil. Zusätzlich wird durch diese Aufteilung der Prozesse auf zwei Reformer-Reaktoren verhindert, dass Pyrolyseprodukte über Bypässe (z. b. Blaseneruption in der Wirbelschicht eines einzigen Reformer-Reaktors oder durch unzureichende Koksschicht in dem einzigen Reformer-Reaktor) den einzigen Reformer-Reaktor verlassen ohne eine Reformierung zu durchlaufen.These Allocation of processes to two reactors allows that the drying and pyrolysis at lower temperatures (<850 ° C) and reforming at higher temperatures (about 900 ° C) can be done. Tars are in the temperature range over 850 ° C and at 900 ° C in the presence of coke as catalyst and an excess of water vapor split and reformed. The catalyzed by the coke reforming at temperatures around 900 ° C results in a virtually tar-free Product gas with high hydrogen content. In addition, through this division of processes on two reformer reactors prevents pyrolysis products via bypasses (eg bubble eruption in the fluidized bed of a single reformer reactor or by insufficient coke layer in the single reformer reactor) leave a single reformer reactor without undergoing reforming.

Gemäß der vorteilhaften Ausgestaltung der Erfindung nach Anspruch 2 stellt einen bevorzugten Aufbau des Wirbelschichtreaktors dar.According to the advantageous embodiment of the invention according to claim 2 provides a preferred construction of the fluidized bed reactor.

Durch die Ausgestaltung nach Anspruch 3 wird das nahezu teerfreie Produktgas aus dem oberen Bereich des zweiten Reformer-Reaktors abgezogen und durch den Boden des zweiten Reformerreaktors und den Boden des gemeinsamen Reaktorbehälters nach außen abgeführt.By The embodiment according to claim 3, the almost tar-free product gas withdrawn from the upper region of the second reformer reactor and through the bottom of the second reformer reactor and the bottom of the common Reactor tank discharged to the outside.

Die vorteilhafte Ausgestaltung der Erfindung nach Anspruch 4 stellte eine einfache konstruktive Möglichkeit dar, den zweiten Reformer-Reaktor als Wirbelschicht-Wärmeübertrager auszugestalten.The advantageous embodiment of the invention according to claim 4 a simple constructive possibility, the second Reformer reactor as a fluidized bed heat exchanger embody.

Die vorteilhafte Ausgestaltung der Erfindung nach Anspruch 5 stellte eine bevorzugte konstruktive Möglichkeit für die Ausgestaltung der Wärmetransporteinrichtung dar.The advantageous embodiment of the invention according to claim 5 provided a preferred constructive possibility for the Embodiment of the heat transport device.

Gemäß der vorteilhaften Ausgestaltung der Erfindung nach Anspruch 6 taucht der zweite Reformer-Reaktor zentral in die erste Wirbelschicht der Brennkammer ein. Der zweite Reformer-Reaktor sitzt damit quasi im Zentrum der Wärme erzeugenden ersten Wirbelschicht. Allerdings müssen hierbei thermische Wechselwirkungen zwischen den den zweiten Reformer-Reaktor umgebenden Heatpipes bzw. Wärmerohren berücksichtigt werden. Dies erübrigt sich bei der Ausgestaltung der Erfindung nach Anspruch 7.According to the advantageous embodiment of the invention according to claim 6 emerged the second reformer reactor centrally into the first fluidized bed of the combustion chamber one. The second reformer reactor is thus almost at the center of the Heat generating first fluidized bed. However, you have to this thermal interactions between the second reformer reactor considered surrounding heat pipes or heat pipes become. This is unnecessary in the embodiment of the invention according to claim 7.

Weitere Einzelheiten, Merkmale und Vorteile der Erfindung ergeben sich aus der nachfolgend beschriebenen beispielhaften Ausführungsform der Erfindung anhand der Zeichnungen.Further Details, features and advantages of the invention will become apparent the exemplary embodiment described below the invention with reference to the drawings.

Es zeigt:It shows:

1 eine Längsschnittdarstellung einer ersten Ausführungsform der Erfindung, 1 a longitudinal sectional view of a first embodiment of the invention,

2 einen Querschnitt durch den zweiten Reformer-Reaktor entlang der Eben A-A in 1, und 2 a cross section through the second reformer reactor along the plane AA in 1 , and

3 eine Längsschnittdarstellung einer zweiten Ausführungsform der Erfindung. 3 a longitudinal sectional view of a second embodiment of the invention.

1 zeigt einen Längsschnitt durch einen Heatpipe-Reformer mit einem kreiszylindrischen gemeinsamen Reaktorbehälter 2, der einen Reaktormantel 4, eine Bodenplatte 6 und eine Deckplatte 8 aufweist. Der Reaktorbehälter 2 besteht aus Stahl. In dem gemeinsamen Reaktorbehälter 2 ist ein topfförmiger Einsatz 9 angeordnet. Im unteren Teil des Reaktorbehälters 2, im Bodenbereich des topförmigen Einsatzes 9 ist eine Brennkammer 10 mit einer ersten Wirbelschicht 12 zur Erzeugung der für die allotherme Wasserdampfvergasung notwendigen Wärme angeordnet. Der Einsatz 9 besitzt eine Doppelfunktion und dient zum einen zum Vorwärmen des Fluidisierungsmittels Luft für die erste Wirbelschicht 12 und gleichzeitig zur Kühlung des gemeinsamen Reaktorbehälters 2. Der genaue Aufbau und die Funktion des Einsatzes 9 ist Gegenstand der deutschen Patentanmeldung 10 2008 051 161.7 . Insofern wird auf diese Anmeldung Bezug genommen. 1 shows a longitudinal section through a heat pipe reformer with a circular cylindrical common reactor vessel 2 , the one reactor jacket 4 , a floor plate 6 and a cover plate 8th having. The reactor vessel 2 is made of steel. In the common reactor vessel 2 is a pot-shaped use 9 arranged. In the lower part of the reactor vessel 2 , in the bottom area of the pot-shaped insert 9 is a combustion chamber 10 with a first fluidized bed 12 arranged to generate the heat necessary for the allothermal steam gasification. The use 9 has a dual function and serves on the one hand for preheating the fluidizing agent air for the first fluidized bed 12 and at the same time for cooling the common reactor vessel 2 , The exact structure and function of the insert 9 is the subject of German patent application 10 2008 051 161.7 , In this respect, reference is made to this application.

Im oberen Teil des Reaktorbehälters 2 ist ein erster Reformer-Reaktor 14 mit einer zweiten Wirbelschicht 16 angeordnet. Der erste Reformer Reaktor 14 umfasst einen kreiszylindrischen Reformerdruckbehälter 18, der durch die Deckplatte 8 verschlossen wird. Im Inneren des Reformerdruckbehälters 18 ist ein oben offener topförmiger Wirbelschichtbehälter 20 angeordnet in der die zweite Wirbelschicht 14 ausgebildet ist. Der topfförmige, oben offene Wirbelschichtbehälter 20 ist konzentrisch zu und im Abstand von dem Reformerdruckbehälter 18 angeordnet, so dass zwischen dem Reformerdruckbehälter 18 und dem Wirbelschichtbehälter 20 ein Spaltraum 21 ausgebildet ist. Von oben durch die Deckplatte 8 führt eine Zuführungseinrichtung 22 in den Bodenbereich des Wirbelschichtbehälters 20. Durch die Zuführungseinrichtung 22 lassen sich kohlenstoffhaltige Einsatzstoffe in die zweite Wirbelschicht 16 einbringen.In the upper part of the reactor vessel 2 is a first reformer reactor 14 with a second fluidized bed 16 arranged. The first reformer reactor 14 includes a circular cylindrical reformer pressure vessel 18 passing through the cover plate 8th is closed. Inside the reformer pressure vessel 18 is an open-topped pot-shaped fluidized bed tank 20 arranged in the second fluidized bed 14 is trained. The pot-shaped, open-top fluidized bed tank 20 is concentric with and spaced from the reformer pressure vessel 18 arranged so that between the reformer pressure vessel 18 and the fluidized bed tank 20 a gap 21 is trained. From the top through the cover plate 8th guides a feeder 22 in the bottom area of the fluidized bed tank 20 , By the feeding device 22 Carbonaceous feedstocks can be in the second fluidized bed 16 contribute.

Unter dem ersten Reformer-Reaktor 14 ist ein zweiter Reformer-Reaktor 24 angeordnet, der säulenförmig ausgebildet ist, einen kreisringförmigen Querschnitt (siehe 2), einen Mantel 26, einen Deckenbereich 27 und einen Bodenbereich 28 aufweist. Der säulenförmige zweite Reformer-Reaktor taucht in die erste Wirbelschicht 12 der Brennkammer 10 ein. Der zweite Reformer-Reaktor 24 ist als Wirbelschicht-Wärmeübertrager ausgebildet und an seiner Außenseite zur Verbesserung des Wärmeübergangs mit Rippen 30 versehen. Zusätzlich oder alternativ kann auch die Innenseite des zweiten Reformer-Reaktor 24 mit Rippen 30 versehen sein.Under the first reformer reactor 14 is a second reformer reactor 24 arranged, which is column-shaped, an annular cross-section (see 2 ), a coat 26 , a ceiling area 27 and a floor area 28 having. The columnar second reformer reactor dips into the first fluidized bed 12 the combustion chamber 10 one. The second reformer reactor 24 is designed as a fluidized bed heat exchanger and on its outside to improve the heat transfer with ribs 30 Mistake. Additionally or alternatively, the inside of the second reformer reactor 24 with ribs 30 be provided.

Aus dem Bodenbereich des topfförmigen Wirbelschichtbehälters 20 mündet eine rohrförmige Pyrolysegasleitung 32, durchsetzt den Deckenbereich 27 des zweiten Reformer-Reaktors 24 und durchläuft das Innere des zweiten Reformer-Reaktors 24 und mündet bzw. endet im Bodenbereich 28 des zweiten Reformer-Reaktors 24. Eine Produktgasauslassleitung 34 beginnt im Deckenbereich 27 Inneren des zweiten Reformer-Reaktors 24, verläuft Im Inneren des zweiten Reformer-Reaktors 24, durchsetzt den Bodenbereich 28 und durchsetzt die Bodenplatte 6 des gemeinsamen Reaktorbehälters 2.From the bottom of the cup-shaped fluidized bed container 20 opens a tubular pyrolysis gas line 32 , intersperses the ceiling area 27 of the second reformer reactor 24 and passes through the interior of the second reformer reactor 24 and ends or ends in the floor area 28 of the second reformer reactor 24 , A product gas outlet line 34 starts in the ceiling area 27 Inside the second reformer reactor 24 , runs inside the second reformer reactor 24 , intersperses the floor area 28 and passes through the bottom plate 6 of the common reactor vessel 2 ,

Über eine Brennstoffzuführung 36 wird Brennstoff in die Brennkammer 10 zugeführt. Das Rauchgas aus der Brennkammer 10 wird über einen Ringspalt 38 zwischen dem Einsatz 9 und dem Reformerdruckbehälter 18 einem Rauchgasabzug 40 zugeführt. Über den Rauchgasabzug 30 werden die Abgase aus der ersten Wirbelschicht 12 der Brennkammer 10 nach außen abgeführt. Die in der Brennkammer 10 erzeugte Wärme wird mittels einer Wärmerohranordnung aus einer Mehrzahl von Wärmerohren oder Heatpipes 42 in die zweite Wirbelschicht 16 in dem ersten Reformer-Reaktor 14 übertragen. Wie dies aus 2 zu ersehen ist, tauchen die einzelnen Wärmerohre 42 mit ihren Wärme aufnehmenden Enden 44 konzentrisch um den zweiten Reformer Reaktor 24 in die erste Wirbelschicht 12 ein, durchsetzen den Boden des Reformerdruckbehälters 18 und den Boden des topfförmigen Wirbelschichtbehälters 20 und enden mit ihren Wärme abgebenden Enden 46 in der zweiten Wirbelschicht 16 des ersten Reformer-Reaktors 14.About a fuel supply 36 fuel gets into the combustion chamber 10 fed. The flue gas from the combustion chamber 10 is through an annular gap 38 between the use 9 and the reformer pressure vessel 18 a flue gas outlet 40 fed. About the flue gas outlet 30 the exhaust gases from the first fluidized bed 12 the combustion chamber 10 discharged to the outside. The ones in the combustion chamber 10 Heat generated by means of a heat pipe arrangement of a plurality of heat pipes or heat pipes 42 in the second fluidized bed 16 in the first reformer reactor 14 transfer. Like this 2 can be seen, the individual heat pipes dip 42 with their heat receiving ends 44 concentric around the second reformer reactor 24 in the first fluidized bed 12 a, enforce the bottom of the reformer pressure vessel 18 and the bottom of the cup-shaped fluidized bed container 20 and end with their heat-emitting ends 46 in the second fluidized bed 16 of the first reformer reactor 14 ,

Während des Betriebes des Heatpipe-Reformers wird in der Brennkammer 10 in der ersten Wirbelschicht 12 erzeugte Wärme mit den Wärmerohren 42 in die zweite Wirbelschicht 16 in dem ersten Reformer-Reaktor 14 transportiert. In der zweiten Wirbelschicht 16 durchlaufen die über die Zuführeinrichtung 22 zugeführten kohlenstoffhaltigen Einsatzstoffe bei einer Temperatur um 800°C eine Trocknung und anschließend eine Pyrolyse. Das dabei entstehende heiße Pyrolysegas entweicht zusammen Koks- und Staubpartikeln nach oben aus dem topfförmigen, oben offenen Wirbelschichtbehälter 20 und strömt in dem Spaltraum 21 in die Pyrolysegasleitung 32. Die Pyrolysegasleitung 32 mündet im Bodenbereich 28 des zweiten Reformer-Reaktors, der in die erste Wirbelschicht 12 in der Brennkammer 10 eingetaucht ist. Das Pyrolysegas bildet in dem zweiten Reformer-Reaktor 24 mit den mitgeführten Koks- und Staubpartikeln als Bettmaterial eine dritte Wirbelschicht 48 aus, in der der Reformierungsprozess erfolgt. Durch das Eintauchen des zweiten Reformer-Reaktors 24 in die erste Wirbelschicht 12 der Brennkammer 10 wird die dritte Wirbelschicht 48 und damit das Pyrolysegas mit den mitgeführten Koks- und Staubpartikeln auf ca. 900°C aufgeheizt, so dass durch Reformierung in dem Pyrolysegas enthaltene Teerverbindungen in Anwesenheit von Koks als Katalysator und einem Überschuss an Wasserdampf in kürzere Kohlenwasserstoffe oder in Wasserstoff und Kohlenmonoxid aufgespalten werden. Über die Produktgasleitung 34 verlässt daher nahezu teerfreies Produktgas mit einem hohen Wasserstoffanteil den Heatpipe-Reformer.During operation of the heat pipe reformer is in the combustion chamber 10 in the first fluidized bed 12 generated heat with the heat pipes 42 in the second fluidized bed 16 in the first reformer reactor 14 transported. In the second fluidized bed 16 go through the over the feeder 22 supplied carbonaceous feeds at a temperature around 800 ° C drying and then pyrolysis. The resulting hot pyrolysis escapes coke and dust particles upwards from the pot-shaped, open-top fluidized bed tank 20 and flows in the gap space 21 in the pyrolysis gas line 32 , The pyrolysis gas 32 flows into the ground area 28 of the second reformer reactor operating in the first fluidized bed 12 in the combustion chamber 10 is immersed. The pyrolysis gas forms in the second reformer reactor 24 with the entrained coke and dust particles as bedding a third fluidized bed 48 in which the reforming process is taking place. By immersing the second reformer reactor 24 in the first fluidized bed 12 the combustion chamber 10 becomes the third fluidized bed 48 and thus the pyrolysis gas with the entrained coke and dust particles heated to about 900 ° C, so that by reforming contained in the pyrolysis tar compounds are split in the presence of coke as a catalyst and an excess of water vapor into shorter hydrocarbons or hydrogen and carbon monoxide. About the product gas line 34 Therefore, almost tar-free product gas with a high hydrogen content leaves the heat pipe reformer.

3 zeigt eine alternative, zweite Ausführungsform der Erfindung, die sich von der ersten Ausführungsform durch den Aufbau des ersten und zweiten Reformer-Reaktors 14, 24 und durch die Anordnung der beiden Reformer-Reaktoren 14, 24 zueinander unterscheidet. Der zweite Reformer-Reaktor 24 ist nicht mittig und konzentrisch zu den Wärmerohren 42, sondern außerhalb, seitlich versetzt zu den konzentrisch angeordneten Wärmerohre 42 in die erste Wirbelschicht 12 der Brennkammer 10 eintaucht. Durch diese versetzte Anordnung des zweiten Reformer-Reaktors 24 muss aus thermischer Hinsicht bei der Anordnung der Wärmerohre 42 weniger Rücksicht auf die Lage und Anordnung des zweiten Reformer-Reaktors 24 genommen werden. Der erste Reformer-Reaktor 14 weist keinen Wirbelschichtbehälter auf, vielmehr ist die zweite Wirbelschicht 16 im unteren Bereich des Reformerdruckbehälters 18 ausgebildet. Die Pyrolysegasleitung führt seitlich aus dem oberen Bereich des Reformerdruckbehälters 18 heraus, wird senkrecht nach unten geführt und mündet in den Bodenbereich 28 in den zweiten Reformer-Reaktor 24. Die Produktgasleitung 34 wird aus dem Deckenbereich 27 des zweiten Reformer-Reaktors 24 heraus geführt, durchläuft neben dem zweiten Reformer-Reaktor 24 die erste Wirbelschicht 12 und durchsetzt den Einsatz 9 und die Bodenplatte 9 des gemeinsamen Reaktorbehälters 2. 3 shows an alternative, second embodiment of the invention, which differs from the first embodiment by the construction of the first and second reformer reactor 14 . 24 and by the arrangement of the two reformer reactors 14 . 24 different from each other. The second reformer reactor 24 is not centered and concentric to the heat pipes 42 but outside, laterally offset to the concentrically arranged heat pipes 42 in the first fluidized bed 12 the combustion chamber 10 dips. By this staggered arrangement of the second reformer reactor 24 must from a thermal point of view when arranging the heat pipes 42 less consideration for the location and arrangement of the second reformer reactor 24 be taken. The first reformer reactor 14 has no fluidized bed container, but rather the second fluidized bed 16 in the lower part of the reformer pressure vessel 18 educated. The pyrolysis gas line leads laterally from the upper region of the reformer pressure vessel 18 out, is guided vertically downwards and opens into the bottom area 28 in the second reformer reactor 24 , The product gas line 34 gets out of the ceiling area 27 of the second reformer reactor 24 led out, passes through the second reformer reactor 24 the first fluidized bed 12 and enforces the mission 9 and the bottom plate 9 of the common reactor vessel 2 ,

Es ist auch möglich mehrere zweite Reformer-Reaktoren 24 vorzusehen, die entlang der Innenseite des Einsatzes 9 angeordnet werden. Es ist auch möglich außerhalb und innerhalb der Wärmerohre 42 zweite Reformer-Reaktoren anzuordnen. Bei der zweiten Ausführungsform der Erfindung kann die Produktgasleitung 34 auch seitlich durch den Einsatz 9 oder über dem Einsatz 9 durch den Reaktormantel 4 nach außen geführt werden.It is also possible to have several second reformer reactors 24 Provide along the inside of the insert 9 to be ordered. It is also possible outside and inside the heat pipes 42 to arrange second reformer reactors. In the second embodiment of the invention, the product gas line 34 also laterally through the insert 9 or over the insert 9 through the reactor jacket 4 be led to the outside.

22
gemeinsamer Reaktorbehältercommon reactor vessel
44
Reaktormantel,Reactor shell,
66
Bodenplattebaseplate
88th
Deckplattecover plate
99
Einsatzcommitment
1010
Brennkammercombustion chamber
1212
erste Wirbelschichtfirst fluidized bed
1414
erster Reformer-Reaktorfirst Reforming reactor
1616
zweite Wirbelschichtsecond fluidized bed
1818
ReformerdruckbehälterReformer pressure vessel
2020
WirbelschichtbehälterFluidized-bed tank
2121
Spaltraumgap
2222
Zuführungseinrichtung für kohlenstoffhaltige Einsatzstoffefeeder for carbonaceous feedstocks
2424
zweiter Reformer-Reaktorsecond Reforming reactor
2626
Mantel von 24 Coat of 24
2727
Deckenbereiche von 24 Ceiling areas of 24
2828
Bodenbereich von 24 Ground area of 24
3030
Rippen an 24 Ribs on 24
3232
Pyrolysegasleitungpyrolysis gas
3434
ProduktgasleitungProduct gas line
3636
Brennstoffzuführungfuel supply
3838
Ringspaltannular gap
4040
RauchgasabzugFlue gas exhaust
4242
Wärmerohreheat pipes
4444
Wärme aufnehmendes Ende von 42 Heat absorbing end of 42
4646
Wärme abgebendes Ende von 42 Heat releasing end of 42
4848
dritte Wirbelschichtthird fluidized bed

ZITATE ENTHALTEN IN DER BESCHREIBUNGQUOTES INCLUDE IN THE DESCRIPTION

Diese Liste der vom Anmelder aufgeführten Dokumente wurde automatisiert erzeugt und ist ausschließlich zur besseren Information des Lesers aufgenommen. Die Liste ist nicht Bestandteil der deutschen Patent- bzw. Gebrauchsmusteranmeldung. Das DPMA übernimmt keinerlei Haftung für etwaige Fehler oder Auslassungen.This list The documents listed by the applicant have been automated generated and is solely for better information recorded by the reader. The list is not part of the German Patent or utility model application. The DPMA takes over no liability for any errors or omissions.

Zitierte PatentliteraturCited patent literature

  • - EP 1187892 B1 [0002, 0003] - EP 1187892 B1 [0002, 0003]
  • - DE 102008051161 [0017] - DE 102008051161 [0017]

Claims (7)

Wirbelschichtreaktor zur Erzeugung von Produktgas aus kohlenstoffhaltigen Einsatzstoffen durch allotherme Wasserdampfvergasung, mit einer Brennkammer (10) mit einer ersten Wirbelschicht (12), einem über der Brennkammer (10) angeordneten ersten Reformer-Reaktor (14) mit einer zweiten Wirbelschicht (16) und einer Zuführeinrichtung (22) zur Aufgabe der zu vergasenden Einsatzstoffe, einer Wärmetransporteinrichtung (42), die Wärme aus der ersten Wirbelschicht (12) in die zweite Wirbelschicht (16) transportiert, einem gemeinsamen Reaktorbehälter (2), in dem der erste Reformer-Reaktor (14) und die Brennkammer (10) angeordnet sind, und einer aus dem gemeinsamen Reaktorbehälter (2) heraus führenden Produktgasleitung, dadurch gekennzeichnet, dass in die erste Wirbelschicht (12) in der Brennkammer (10) wenigstens ein zweiter Reformer-Reaktor (24) mit einer dritten Wirbelschicht (48) eingetaucht ist, der als Wirbelschicht-Wärmeübertrager ausgebildet ist, dass der erste Reformer-Reaktor (14) über eine Pyrolysegasleitung mit dem zweiten Reformer-Reaktor (24) verbunden ist, und dass der zweite Reformer-Reaktor (24) mit der Produktgasleitung verbunden ist.Fluidized bed reactor for producing product gas from carbonaceous feedstocks by allothermic steam gasification, with a combustion chamber ( 10 ) with a first fluidized bed ( 12 ), one above the combustion chamber ( 10 ) arranged first reformer reactor ( 14 ) with a second fluidized bed ( 16 ) and a feeder ( 22 ) for the task of gasifying feedstocks, a heat transport device ( 42 ), the heat from the first fluidized bed ( 12 ) into the second fluidized bed ( 16 ), a common reactor vessel ( 2 ), in which the first reformer reactor ( 14 ) and the combustion chamber ( 10 ), and one from the common reactor vessel ( 2 ) leading out product gas line, characterized in that in the first fluidized bed ( 12 ) in the combustion chamber ( 10 ) at least one second reformer reactor ( 24 ) with a third fluidized bed ( 48 immersed, which is designed as a fluidized bed heat exchanger, that the first reformer reactor ( 14 ) via a pyrolysis gas line to the second reformer reactor ( 24 ) and that the second reformer reactor ( 24 ) is connected to the product gas line. Wirbelschichtreaktor nach Anspruch 1, dadurch gekennzeichnet, dass der zweite Reformer-Reaktor (24) einen säulenförmigen Behälter (26) mit einem Decken- (27) und einem Bodenbereich (28) umfasst, dass die Pyrolysegasleitung teilweise in dem zweiten Reformer-Reaktor (24) angeordnet ist und im Bodenbereich des zweiten Reformer-Reaktors (24) eine Austrittsöffnung aufweist, und dass aus dem Deckenbereich (27) des zweiten Reformer-Reaktors die Produktgasleitung (34) heraus führt.Fluidised bed reactor according to claim 1, characterized in that the second reformer reactor ( 24 ) a columnar container ( 26 ) with a ceiling ( 27 ) and a floor area ( 28 ), that the pyrolysis gas line is partly in the second reformer reactor ( 24 ) and in the bottom region of the second reformer reactor ( 24 ) has an outlet opening, and that from the ceiling area ( 27 ) of the second reformer reactor, the product gas line ( 34 ) leads out. Wirbelschichtreaktor nach Anspruch 2, dadurch gekennzeichnet, dass die Produktgasleitung den zweiten Reformer-Reaktor (24) durchsetzt und im Bodenbereich (28) nach außen geführt ist.Fluidized bed reactor according to claim 2, characterized in that the product gas line, the second reformer reactor ( 24 ) and in the ground area ( 28 ) is led to the outside. Wirbelschichtreaktor nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der Mantel (26) des zweiten Reformer-Reaktors (24) berippt (30) ist.Fluidised bed reactor according to one of the preceding claims, characterized in that the jacket ( 26 ) of the second reformer reactor ( 24 ) ribbed ( 30 ). Wirbelschichtreaktor nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass die Wärmetransporteinrichtung eine Wärmerohranordnung mit einer Mehrzahl von Wärmerohren (42) umfasst.Fluidized bed reactor according to one of the preceding claims, characterized in that the heat transport device comprises a heat pipe arrangement with a plurality of heat pipes ( 42 ). Wirbelschichtreaktor nach Anspruch 5, dadurch gekennzeichnet, dass die einzelnen Wärmerohre (42) um den wenigstens einen zweiten Reformer-Reaktor (24) herum angeordnet sind.Fluidized bed reactor according to claim 5, characterized in that the individual heat pipes ( 42 ) around the at least one second reformer reactor ( 24 ) are arranged around. Wirbelschichtreaktor nach Anspruch 5, dadurch gekennzeichnet, dass der wenigstens eine zweite Reformer-Reaktor (24) seitlich versetzt, neben den einzelnen Wärmerohre (42) angeordnet ist.Fluidized bed reactor according to claim 5, characterized in that the at least one second reformer reactor ( 24 ) laterally offset, next to the individual heat pipes ( 42 ) is arranged.
DE102009030542A 2009-06-25 2009-06-25 Fluidized bed reactor for producing gas product from carbon-containing materials through allothermal steam gasification, comprises combustion chamber with fluidized bed and reforming reactor with another fluidized bed and feeding device Withdrawn DE102009030542A1 (en)

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ITFI20110133A1 (en) * 2011-07-05 2013-01-06 Rewood S R L GASIFICATION PROCESS.
WO2013098525A1 (en) * 2011-12-29 2013-07-04 Cogebio Method and apparatus for fixed bed gasification
DE102014204672A1 (en) * 2014-03-13 2015-09-17 Linde Aktiengesellschaft Gasification process and gasification reactor
JP2022030460A (en) * 2020-08-07 2022-02-18 株式会社堤水素研究所 Hydrogen production device
WO2024083755A1 (en) * 2022-10-17 2024-04-25 Synthec Fuels GmbH A device for gasification of feedstock

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EP1187892B1 (en) 1999-06-09 2004-12-29 Technische Universität München Lehrstuhl für Thermische Kraftanlagen Device for the gasification of carbonaceous feedstock
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EP1187892B1 (en) 1999-06-09 2004-12-29 Technische Universität München Lehrstuhl für Thermische Kraftanlagen Device for the gasification of carbonaceous feedstock
DE102008051161A1 (en) 2008-10-10 2010-04-22 Highterm Research Gmbh Fluidized bed reactor and use for such a fluidized bed reactor

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITFI20110133A1 (en) * 2011-07-05 2013-01-06 Rewood S R L GASIFICATION PROCESS.
WO2013005239A1 (en) * 2011-07-05 2013-01-10 Rewood S.R.L. Gasification process
WO2013098525A1 (en) * 2011-12-29 2013-07-04 Cogebio Method and apparatus for fixed bed gasification
US9255231B2 (en) 2011-12-29 2016-02-09 Cogebio Method and apparatus for fixed bed gasification
DE102014204672A1 (en) * 2014-03-13 2015-09-17 Linde Aktiengesellschaft Gasification process and gasification reactor
JP2022030460A (en) * 2020-08-07 2022-02-18 株式会社堤水素研究所 Hydrogen production device
JP7118341B2 (en) 2020-08-07 2022-08-16 株式会社堤水素研究所 Hydrogen production equipment
WO2024083755A1 (en) * 2022-10-17 2024-04-25 Synthec Fuels GmbH A device for gasification of feedstock

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