DE102005048488B4 - Method and apparatus for high power airstream gasifier - Google Patents
Method and apparatus for high power airstream gasifier Download PDFInfo
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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
- C10J3/466—Entrained flow processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- 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
- C10J3/50—Fuel charging devices
- C10J3/506—Fuel charging devices for 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
- 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
- C10J3/845—Quench rings
-
- 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
- C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
-
- 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
- C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- 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
- C10J2300/1634—Ash vitrification
-
- 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
- C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
- Feeding And Controlling Fuel (AREA)
Abstract
Vorrichtung zur Vergasung von flüssigen und festen Brennstoffen im Flugstrom mit einem freien Sauerstoff enthaltenden Oxidationsmittel durch partielle Oxidation bei Drücken zwischen Umgebungsdruck und 8 MPa, Temperaturen zwischen 1.200 und 1.900°C sowie hohen Reaktorleistungen bei der
– ein Hochleistungsvergasungsreaktor (2) mehrere am Kopf angeordnete Vergasungsbrenner (2.1) sowie einen Zünd- und Pilotbrenner (2.2) aufweist,
dadurch gekennzeichnet, dass
– jedem Vergasungsbrenner (2.1) ein eigenes Brennstoff- Zuführungssystem zugeordnet ist,
– eine Anordnung am Vergasungsbrenner (2.1) zum Messen und Regeln der zufließenden Brennstoff- und Sauerstoffmengen gegeben ist und
– eine integrale Überwachung und Regelung der dem Vergasungsreaktor (2) insgesamt zufließenden Brennstoff- und Sauerstoffmenge gegeben ist.Device for the gasification of liquid and solid fuels in flight stream with a free oxygen-containing oxidant by partial oxidation at pressures between ambient pressure and 8 MPa, temperatures between 1,200 and 1,900 ° C and high reactor performance in the
A high-performance gasification reactor (2) has a plurality of gasification burners (2.1) arranged at the top and an ignition and pilot burner (2.2),
characterized in that
- each gasification burner (2.1) is assigned its own fuel supply system,
- An arrangement on the gasification burner (2.1) for measuring and regulating the inflowing fuel and oxygen levels is given and
- Is an integral monitoring and control of the gasification reactor (2) total inflowing fuel and oxygen is given.
Description
Die Erfindung betrifft eine Vorrichtung und ein Verfahren zur Flugstromvergasung sehr hoher Leistung, wie sie zur Synthesegasversorgung von Großsynthesen eingesetzt werden können. Die Erfindung erlaubt, zu Brennstaub aufbereitete Brennstoffe wie Braun- und Steinkohlen, Petrolkokse, feste mahlbare Rückstände aber auch Feststoff-Flüssig-Suspensionen, sogenannte Slurries in Synthesegas umzuwandeln. Dabei wird der Brennstoff bei Temperaturen zwischen 1.200 bis 1.900°C mit einem freien Sauerstoff enthaltenden Vergasungsmittel bei Drucken bis 8 MPa durch Partialoxidation in CO- und H2-haltige Gase umgesetzt. Dies geschieht in einem Vergasungsreaktor, der sich durch eine Mehrbrenneranordnung und durch einen gekühlten Vergasungsraum auszeichnet.The invention relates to a device and a method for entrained flow gasification very high performance, as they can be used for synthesis gas supply of large-scale synthesis. The invention allows converted into fuel dust fuels such as brown and hard coal, petroleum cokes, solid grindable residues but also solid-liquid suspensions, so-called slurries in synthesis gas. In this case, the fuel at temperatures between 1200 to 1900 ° C with a free oxygen-containing gasification agent at pressures up to 8 MPa by partial oxidation in CO and H 2 -containing gases. This is done in a gasification reactor, which is characterized by a multi-burner arrangement and by a cooled gasification chamber.
In der Technik der Gaserzeugung ist die autotherme Flugstromvergasung von festen, flüssigen und gasförmigen Brennstoffen langjährig bekannt. Das Verhältnis von Brennstoff zu sauerstoffhaltigen Vergasungsmitteln wird dabei so gewählt, dass aus Gründen der Synthesegasqualität höhere Kohlenstoffverbindungen zu Synthesegaskomponenten wie CO und H2 vollständig aufgespalten werden und die anorganischen Bestandteile als schmelzflüssige Schlacke ausgetragen werden, siehe J. Carl, P. Fritz, NOELL-KONVERSIONSVERFAHREN, EF-Verlag für Energie- und Umwelttechnik GmbH, 1996, S. 33 und S. 73.In The technique of gas production is autothermal entrained flow gasification from solid, liquid and gaseous Fuels for many years known. The relationship from fuel to oxygen-containing gasification agents is doing chosen so that for reasons the synthesis gas quality higher Carbon compounds to synthesis gas components such as CO and H2 Completely split and the inorganic components as molten slag J. Carl, P. Fritz, NOELL CONVERSION PROCEDURE, EF-Verlag for Energy and environmental technology GmbH, 1996, p. 33 and p. 73.
Nach
verschiedenen in der Technik eingeführten Systemen können dabei
Vergasungsgas und schmelzflüssige
Schlacke getrennt oder gemeinsam aus dem Reaktionsraum der Vergasungsvorrichtung ausgetragen
werden, wie
Von Ch. Higman und M. van der Burgt wird in „Gasification", Seite 124, Verlag Elsevier 2003, ein Verfahren vorgestellt, bei dem das heiße Vergasungsgas gemeinsam mit der flüssigen Schlacke den Vergaser verlässt und direkt in einen senkrecht darunter angeordneten Abhitzekessel eintritt, in dem das Rohgas und die Schlacke unter Nutzung derFrom Ch. Higman and M. van der Burgt is published in "Gasification", page 124, publisher Elsevier 2003, a method presented in which the hot gasification gas together with the liquid Slag leaves the carburetor and directly into a waste heat boiler arranged vertically underneath enters, in which the raw gas and the slag using the
Abwärme zur Dampferzeugung abgekühlt werden. Die Schlacke sammelt sich in einem Wasserbad, das gekühlte Rohgas verlässt den Abhitzekessel seitwärts. Dem Vorteil der Abhitzegewinnung nach diesem System steht eine Reihe von Nachteilen gegenüber. Genannt seien hier besonders die Bildung von Ablagerungen auf den Wärmetauscherrohren, die zur Behinderung des Wärmeüberganges sowie zur Korrosion und Erosion und damit zu mangelnder Verfügbarkeit führen.Waste heat to Steam production to be cooled. The slag collects in a water bath, the cooled raw gas leaves the waste heat boiler sideways. The advantage of waste heat recovery according to this system is a series of disadvantages. Mention may be made here especially of the formation of deposits on the Heat exchanger tubes, to prevent the heat transfer as well as to corrosion and erosion and thus lack of availability to lead.
Die Leistung der verschiedenen dargelegten Vergasungstechnologien ist auf ca. 500 MW begrenzt.The performance of the various outlined Gasification technologies is limited to approximately 500 MW.
Ausgehend von diesem Stand der Technik ist es Aufgabe der Erfindung, eine Vorrichtung zur Vergasung von flüssigen und festen Brennstoffen im Flugstrom sowie ein Verfahren zur Durchführung in dieser Vorrichtung zu schaffen, die bei einer zuverlässigen und sicheren Betriebsweise höchste Leistungen von 1.000 bis 1.500 MW erlauben.outgoing From this prior art, it is an object of the invention, a Device for the gasification of liquid and solid fuels in the tailings stream and a method of carrying them out in this stream To provide device in a reliable and safe operation highest Allow power from 1,000 to 1,500 MW.
Diese Aufgabe wird durch eine Vorrichtung zur Vergasung von flüssigen und festen Brennstoffen im Flugstrom nach Anspruch 1 sowie ein Verfahren zur Durchführung in dieser Vorrichtung nach Anspruch 13 gelöst. Unteransprüche geben vorteilhafte Ausführungen der Erfindung wieder.These The object is achieved by a device for the gasification of liquid and solid fuels in the flow stream according to claim 1 and a method for execution dissolved in this device according to claim 13. Subordinate claims advantageous embodiments the invention again.
Die Erfindung macht sich die Erkenntnis zu nutze, dass die Brennstoffzuführung zum Vergasungsreaktor einen Engpass für die Leistungsfähigkeit des Vergasungsreaktors bildet.The Invention makes use of the knowledge that the fuel supply to Gasification reactor a bottleneck for the efficiency of the gasification reactor forms.
Das Vergasungsverfahren zur Vergasung von festen aschehaltigen Brennstoffen bei sehr hohen Leistungen mit einem sauerstoffhaltigen Oxidationsmittel basiert auf einem Flugstromreaktor dessen Reaktionsraumkontur durch ein Kühlsystem begrenzt wird, wobei der Druck im Kühlsystem immer höher gehalten wird als der Druck im Reaktionsraum. Für die Vorbereitung des Brennstoffes und die Zuführung zu den Vergasungsbrennern wird wie folgt verfahren: Bei trockener pneumatischer Zuführung nach dem Prinzip der Dichtstromförderung wird der Brennstoff getrocknet, auf eine Körnung < 200 µm zerkleinert und über Betriebsbunker Druckschleusen aufgegeben, in denen durch Zuführung eines nicht kondensierenden Gases wie N2 oder CO2 der staubförmige Brennstoff auf den gewünschten Vergasungsdruck gebracht wird. Es können dabei gleichzeitig verschiedene Brennstoffe eingesetzt werden. Durch Anordnung mehrerer dieser Druckschleusen kann abwechselnd befüllt und mit Druck beaufschlagt werden. Anschließend gelangt der unter Druck gesetzte Staub in Dosiergefäße, in denen im unteren Teil durch Zuführung gleichfalls eines nicht kondensierenden Gases eine sehr dichte Wirbelschicht erzeugt wird, in die ein oder mehrere Förderrohre eintauchen und in den Brennern des Vergasungsreaktors münden. Jedem Hochleistungsbrenner ist dabei ein separates Zuführungs- und Dosiersystem zugeordnet. Durch Anlegen einer Druckdifferenz zwischen den Dosiergefäßen und den Brennern des Vergasungsreaktors fließt der fluidisierte Brennstaub den Brennern zu. Durch Mess- und Überwachungseinrichtungen wird die strömende Brennstaubmenge gemessen, geregelt und überwacht.The Gasification process for the gasification of solid ash-containing fuels at very high powers with an oxygen-containing oxidant is based on a flow reactor whose reaction space contour by a cooling system is limited, the pressure in the cooling system kept higher is called the pressure in the reaction space. For preparation of fuel and the feeder too The gasification burners are operated as follows: For dry pneumatic feed according to the principle of dense phase conveying The fuel is dried, crushed to a grain size <200 microns and operating bunker Pressure locks abandoned in which by supplying a non-condensing Gases like N2 or CO2 the dusty fuel to the desired Gasification pressure is brought. It can be different at the same time Fuels are used. By arranging several of these pressure locks can be filled alternately and be pressurized. Then comes under pressure put dust in dosing, in which in the lower part by feeder also a non-condensing gas a very dense fluidized bed is generated, in which one or more delivery pipes dip and in the burners of the gasification reactor open. Each high-performance burner is equipped with a separate supply and dosing system assigned. By applying a pressure difference between the dosing and the burners of the gasification reactor, the fluidized fuel dust flows to the burners too. By measuring and monitoring equipment is the streaming Fuel dust quantity measured, regulated and monitored.
Es besteht mit dem vorgeschlagenen Reaktor auch weiterhin die Möglichkeit, den ungetrockneten Brennstoff ebenfalls auf eine Körnung < 200 µm zu zerkleinern und den Brennstaub mit Wasser oder Öl zu vermischen und als Slurry den Brennern des Vergasungsreaktors zuzuführen. Das Verfahren zur Zuführung, welches an dieser Stelle nicht beschrieben ist, gestaltet der Fachmann nach den ihm bekannten Mitteln aus.It With the proposed reactor, there is still the possibility also to crush the undried fuel to a grain size <200 microns and mix the fuel dust with water or oil and as a slurry to supply to the burners of the gasification reactor. The method of delivery, which is not described at this point, designed by the expert the means known to him.
Den Brennern wird gleichzeitig ein freien Sauerstoff enthaltendes Oxidationsmittel aufgegeben und das Slurry durch partielle Oxidation in ein Rohsynthesegas überführt. Die Vergasung findet bei Temperaturen zwischen 1.200 und 1.900°C bei Drucken bis zu 80 bar statt. Der Reaktor besitzt eine gekühlte Reaktionsraumkontur, die durch einen Kühlschirm gebildet wird. Dieser besteht aus einem gasdicht verschweißten Rohrschirm, der bestiftet und mit einem gut temperaturleitfähigen Material belegt ist.The Burners simultaneously become a free oxygen-containing oxidant abandoned and the slurry converted by partial oxidation in a Rohsynthesegas. The gasification takes place at temperatures between 1,200 and 1,900 ° C at pressures up to 80 bar instead of. The reactor has a cooled reaction space contour, the through a cooling screen is formed. This consists of a gastight welded pipe screen, which is donated and covered with a good temperature conductive material.
Das im Vergasungsreaktor erzeugte Rohgas verlässt gemeinsam mit der aus der Brennstoffasche gebildeten flüssigen Schlacke den Vergasungsreaktor und gelangt in einen senkrecht darunter angeordneten Raum, in dem durch Einspritzen von Wasser eine Abkühlung des heißen Rohgases und der flüssigen Schlacke erfolgt. Die Abkühlung kann vollständig bis zum Taupunkt des Gases durch Einspritzen von Wasser im Überschuss erfolgen. In Abhängigkeit vom Druck liegt die Temperatur danach zwischen 180 und 240°C. Es ist jedoch auch möglich, nur eine begrenzte Kühlwassermenge zuzuführen und Rohgas und Schlacke durch eine Teilkühlung auf beispielsweise 700 bis 1.100°C abzukühlen, um anschließend in einem Abhitzekessel die fühlbare Wärme des Rohgases zur Dampferzeugung zu nutzen. Durch die Teilquenchung bzw. Teilkühlung wird die Gefahr des Anbackens von Schlacke an die Rohre des Abhitzekessels verhindert oder stark begrenzt. Das für die vollständige oder Teilkühlung erforderliche Wasser oder rückgeführte Gaskondensat wird über Düsen zugeführt, die sich direkt am Mantel des Kühlraumes befinden. Die abgekühlte Schlacke wird in einem Wasserbad gesammelt und aus dem Verfahren ausgeschleust. Das auf Temperaturen zwischen 200 bis 300°C abgekühlte Rohgas gelangt anschließend in eine Rohgaswäsche, die zweckmäßiger Weise als Venturiwäsche ausgebildet ist.The in the gasification reactor produced raw gas leaves together with the from the Fuel ash formed liquid Slag the gasification reactor and get into a vertical underneath arranged space in which by injection of water a cooling of the be called Raw gas and the liquid Slag takes place. The cooling can completely up to the dew point of the gas by injecting excess water respectively. Depending on Pressure then the temperature is between 180 and 240 ° C. It is but also possible only a limited amount of cooling water supply and raw gas and slag by partial cooling to, for example, 700 up to 1,100 ° C cool, then in a waste heat boiler the tangible Heat of the Use raw gas for steam generation. By partial quenching or part cooling the risk of caking of slag on the pipes of the waste heat boiler prevented or severely limited. That for the full or part cooling required water or recycled gas condensate will over Supplied to nozzles are located directly on the jacket of the cold room. The cooled Slag is collected in a water bath and removed from the process discharged. The cooled to temperatures between 200 to 300 ° C raw gas then arrives in a raw gas wash, the appropriate way as Venturi wash is trained.
Hierbei wird der mitgeführte Staub bis zu einer Korngröße von ca. 20 μm entfernt. Dieser Reinheitsgrad reicht noch nicht aus, um anschließend katalytische Prozesse wie beispielsweise eine Rohgaskonvertierung durchzuführen. Dabei ist weiter zu bedenken, dass zusätzlich Salznebel im Rohgas mitgeführt werden, die während der Vergasung aus dem Brennstaub entbunden und mit dem Rohgas abgeführt werden. Um sowohl den Feinststaub < 20 μm als auch die Salznebel zu entfernen wird das gewaschene Rohgas einer Kondensationsstufe zugeführt, in der das Rohgas indirekt um 5 bis 10°C abgekühlt wird. Dabei wird aus dem wasserdampfgesättigten Rohgas Wasser kondensiert, das die beschriebenen feinen Staub- und Salzpartikel aufnimmt. In einem anschließenden Abscheider wird das die Staub- und Salzpartikel enthaltene kondensierte Wasser aus dem Rohgas entfernt. Das so gereinigte Rohgas kann danach direkt beispielsweise einer Entschwefelungsanlage zugeführt werden.Here, the entrained dust is removed up to a particle size of about 20 microns. This degree of purity is still insufficient to subsequently carry out catalytic processes such as a crude gas conversion. It should further be considered that in addition salt mist are carried in the raw gas, which are released during the gasification of the fuel dust and discharged with the raw gas. In order to remove both the ultrafine dust <20 microns and the salt mist, the scrubbed crude gas is fed to a condensation stage in which the crude gas is indirectly cooled by 5 to 10 ° C. becomes. In this case, water is condensed from the water vapor-saturated crude gas, which absorbs the fine dust and salt particles described. In a subsequent separator, the condensed water containing the dust and salt particles is removed from the raw gas. The thus purified crude gas can then be fed directly, for example, a desulfurization.
Im Folgenden wird die Erfindung an 5 Figuren und zwei Ausführungsbeispielen näher erläutert. Die Figuren zeigen:in the Below, the invention of 5 figures and two embodiments explained in more detail. The Figures show:
Die
Die
Die
Die
Die
An
einem ersten Beispiel soll die Funktion anhand von Stoffströmen und
verfahrenstechnischen Vorgängen
erläutert
werden:
Einem Vergasungsreaktor mit einer Bruttoleistung von
1500 MW wird eine Kohlenstaubmenge von 240 Mg/h zugeführt. Dieser
durch Trocknung und Mahlung aus Rohsteinkohle hergestellte Brennstaub
besitzt einen Feuchtigkeitsgehalt von 5,8%, einen Aschegehalt von
13 Ma% und einen Heizwert von 24.700 kJ/kg. Die Vergasung findet
bei 1.550°C
statt, die benötigte
Sauerstoffmenge beträgt
208.000 m3 i. N./h. Die Rohkohle wird zunächst einer
dem Stand der Technik entsprechende Trocknungs- und Mahlanlage zugeführt, in
der der Wassergehalt auf 1,8 Ma% reduziert wird. Das nach der Mahlung
vorhandene Körnungsband
des aus der Rohkohle hergestellten Brennstaubes liegt zwischen 0
und 200 μm. Danach
wird der gemahlene Brennstaub (
A pulverized coal amount of 240 Mg / h is fed to a gasification reactor with a gross capacity of 1500 MW. This dust produced by drying and grinding of raw coal has a moisture content of 5.8%, an ash content of 13% by mass and a calorific value of 24,700 kJ / kg. The gasification takes place at 1,550 ° C, the required amount of oxygen is 208,000 m 3 i. N./h. The raw coal is first fed to a state of the art drying and grinding plant, in which the water content is reduced to 1.8 Ma%. The existing after grinding graining band of the produced from the raw coal fuel dust is between 0 and 200 microns. Thereafter, the ground fuel dust (
Das
1.550°C
heiße
Rohgas verlässt
gemeinsam mit der flüssigen
Schlacke den Vergasungsraum
Nach
einem Beispiel 2 soll der Vorgang der Brennstaubzuführung nach
- 11
- Pneumatische Dosiersysteme für Brennstaubpneumatic Dosing systems for pulverized fuel
- 1.11.1
- Bunkerbunker
- 1.21.2
- Druckschleusepressure lock
- 1.31.3
- Dosiergefäßmetering
- 1.41.4
- Förderleitungdelivery line
- 1.51.5
- Leitung für Wirbelgasmanagement for fluidizing gas
- 1.61.6
-
Leitung
für Inertgas
in
1.2 Line for inert gas in1.2 - 1.71.7
-
Entspannungsleitung
aus
1.2 Relaxation line off1.2 - 22
- Vergasungsreaktor mit gekühlter Reaktionsraumstrukturgasification reactor with chilled Reaction chamber structure
- 2.12.1
- Staubbrenner mit Sauerstoffzuführungdust burner with oxygen supply
- 2.22.2
- Zünd- und PilotbrennerIgnition and ignition pilot burner
- 2.32.3
- Vergasungsraumgasification chamber
- 2.42.4
- Kühlschirmcooling screen
- 2.52.5
- Austrittsöffnungoutlet opening
- 33
- Quenchkühlerquench
- 3.13.1
- Quenchraumquench
- 3.23.2
- Quenchdüsenquench nozzles
- 3.33.3
- Quenchdüsenquench nozzles
- 3.43.4
- Rohgasabgangcrude gas
- 3.53.5
- Wasserbad mit Schlackewater bath with slag
- 3.63.6
-
Unterer
Abgang von
3 Lower Departure from3 - 3.73.7
- Auskleidunglining
- 44
- Rohgaswäscheraw gas scrubbing
- 4.14.1
- Abhitzekesselwaste heat boiler
- 55
- Kondensation, TeilkondensationCondensation, partial condensation
Claims (21)
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE202005021659U DE202005021659U1 (en) | 2005-10-07 | 2005-10-07 | Device for high-flow entrainment gasifier |
DE102005048488.3A DE102005048488C5 (en) | 2005-10-07 | 2005-10-07 | Method and device for high power entrained flow gasifiers |
CN2005101272860A CN1944593B (en) | 2005-10-07 | 2005-12-05 | Method and device for high-capacity entrained flow gasifier |
CA002534407A CA2534407A1 (en) | 2005-10-07 | 2006-01-26 | Method and device for high-capacity entrained flow gasifier |
US11/359,608 US20070079554A1 (en) | 2005-10-07 | 2006-02-22 | Method and device for high-capacity entrained flow gasifier |
AU2006201142A AU2006201142B2 (en) | 2005-10-07 | 2006-03-20 | Method and device for high-capacity entrained flow gasifier |
DE102006029595.1A DE102006029595B4 (en) | 2005-10-07 | 2006-06-26 | Method for high current jet carburettor |
ZA2006/07404A ZA200607404B (en) | 2005-10-07 | 2006-09-05 | Method and device for high-capacity entrained flow gasifier |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102005048488.3A DE102005048488C5 (en) | 2005-10-07 | 2005-10-07 | Method and device for high power entrained flow gasifiers |
Publications (3)
Publication Number | Publication Date |
---|---|
DE102005048488A1 DE102005048488A1 (en) | 2007-05-03 |
DE102005048488B4 true DE102005048488B4 (en) | 2009-07-23 |
DE102005048488C5 DE102005048488C5 (en) | 2020-07-02 |
Family
ID=37909963
Family Applications (3)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DE202005021659U Expired - Lifetime DE202005021659U1 (en) | 2005-10-07 | 2005-10-07 | Device for high-flow entrainment gasifier |
DE102005048488.3A Expired - Fee Related DE102005048488C5 (en) | 2005-10-07 | 2005-10-07 | Method and device for high power entrained flow gasifiers |
DE102006029595.1A Expired - Fee Related DE102006029595B4 (en) | 2005-10-07 | 2006-06-26 | Method for high current jet carburettor |
Family Applications Before (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DE202005021659U Expired - Lifetime DE202005021659U1 (en) | 2005-10-07 | 2005-10-07 | Device for high-flow entrainment gasifier |
Family Applications After (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DE102006029595.1A Expired - Fee Related DE102006029595B4 (en) | 2005-10-07 | 2006-06-26 | Method for high current jet carburettor |
Country Status (6)
Country | Link |
---|---|
US (1) | US20070079554A1 (en) |
CN (1) | CN1944593B (en) |
AU (1) | AU2006201142B2 (en) |
CA (1) | CA2534407A1 (en) |
DE (3) | DE202005021659U1 (en) |
ZA (1) | ZA200607404B (en) |
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Also Published As
Publication number | Publication date |
---|---|
US20070079554A1 (en) | 2007-04-12 |
CN1944593A (en) | 2007-04-11 |
CN1944593B (en) | 2011-11-23 |
CA2534407A1 (en) | 2007-04-07 |
DE102005048488A1 (en) | 2007-05-03 |
AU2006201142A1 (en) | 2007-04-26 |
DE102006029595B4 (en) | 2018-04-19 |
ZA200607404B (en) | 2008-01-08 |
DE202005021659U1 (en) | 2010-01-14 |
DE102005048488C5 (en) | 2020-07-02 |
AU2006201142B2 (en) | 2011-07-21 |
DE102006029595A1 (en) | 2007-12-27 |
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