DE102005042640A1 - Process and apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels with partial quenching and waste heat recovery - Google Patents
Process and apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels with partial quenching and waste heat recovery 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
- C10J3/48—Apparatus; Plants
- C10J3/52—Ash-removing devices
- C10J3/526—Ash-removing 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
- 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
- C10J3/86—Other features combined with waste-heat boilers
-
- 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
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
-
- 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
- C10J2300/0973—Water
-
- 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
- C10J2300/0983—Additives
-
- 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
Abstract
Die Erfindung betrifft ein Verfahren und eine Vorrichtung zur Vergasung von festen Brennstoffen wie Steinkohlen und Kokse wie solche aus Steinkohlen, Braunkohlen und Biomasse sowie Petrolkokse, die fein aufgemahlen und gemeinsam mit Wasser oder Öl zu Brennstoff-Flüsig-Suspensionen, so genannten Slurries, vermischt werden und ihre Vergasung gemeinsam mit einem freien Sauerstoff enthaltenden Oxidationsmittel durch partielle Oxidation bei Drücken zwischen Umgebungsdruck und 100 bar sowie Temperaturen zwischen 1200 bis 1900 DEG C in einem Flugstromreaktor, bestehend aus den Verfahrensschritten Slurryherstellung und -zuführung zum Reaktor, Vergasung in einem Flugstromreaktor mit gekühlter Reaktionsraumkontur, Teilquenchung, Abhitzegewinnung sowie nasse oder trockene Staubabscheidung, wobei das Rohgas so vorbehandelt ist, dass es weiteren technologischen Stufen wie einer Rohgaskonvertierung oder Entschwefelung zugeleitet werden kann.The invention relates to a method and an apparatus for the gasification of solid fuels such as hard coal and coke such as those made from hard coal, lignite and biomass and petroleum coke, which are finely ground and mixed together with water or oil to form fuel-liquid suspensions, so-called slurries and their gasification together with a free oxygen-containing oxidizing agent by partial oxidation at pressures between ambient pressure and 100 bar and temperatures between 1200 and 1900 ° C in an entrained-flow reactor, consisting of the process steps of slurry production and supply to the reactor, gasification in an entrained-flow reactor with a cooled reaction chamber contour , Partial quenching, waste heat recovery and wet or dry dust separation, the raw gas being pretreated in such a way that it can be fed to further technological stages such as raw gas conversion or desulfurization.
Description
Die Erfindung betrifft ein Vergasungsverfahren entsprechend dem Oberbegriff des ersten Patentanspruches und eine Vorrichtung zur Durchführung des Verfahrens.The The invention relates to a gasification process according to the preamble of the first claim and a device for carrying out the Process.
Das Verfahren besteht aus den Verfahrensschritten Slurryherstellung, Brennstoffzuführung, Vergasungsreaktion, Teilquenchung, Gaswäsche und Teilkondensation, wobei Gaswäsche und Teilkondensation durch eine mechanische Staubabscheidung ersetzt werden können, zur Erzeugung CO- und H2-haltiger Gase durch Partialoxidation staubförmiger, aschehaltiger Brennstoffe mit einem freien Sauerstoff enthaltenden Vergasungsmittel bei hohen Temperaturen und erhöhtem Druck.The process consists of the process steps slurry preparation, fuel supply, gasification reaction, partial quenching, gas scrubbing and partial condensation, gas scrubbing and partial condensation can be replaced by a mechanical dust separation, to produce CO and H 2 -containing gases by partial oxidation of dusty, ash-containing fuels with a free oxygen containing gasification agent at high temperatures and elevated pressure.
Um lange Betriebszeiten zu erreichen muß der Druckmantel des Vergasungsreaktors zuverlässig gegen die Einwirkung von Rohgas und gegen die hohen Vergasungstemperaturen von 1.200-1.900°C geschützt sein. Dies geschieht durch Begrenzung des Reaktions- bzw. Vergasungsraumes durch einen gekühlten Rohrschirm, der in den Druckmantel eingehangen ist. Der Ringspalt zwischen Rohrschirm und Druckmantel wird gespült.Around To reach long operating times must the pressure jacket of the gasification reactor reliable against the action of raw gas and against the high gasification temperatures protected from 1,200-1,900 ° C. This is done by limiting the reaction or gasification space through a chilled Pipe screen, which is mounted in the pressure jacket. The annular gap between pipe screen and pressure jacket is rinsed.
Der Brennstoff wird als Slurry durch Pumpenförderung auf Vergasungsdruck gebracht und am Kopf des Reaktors über Brenner zugeführt. Es können gleichzeitig ein oder mehrere Brennstoffe oder Kohlesorten vergast werden. Das Rohgas verlässt den Vergasungsraum gemeinsam mit der verflüssigten Schlacke am unteren Ende des Reaktors und wird anschließend durch Einspritzen von Wasser auf 700 °C bis 1100 °C teilgekühlt und nach der Abhitzegewinnung von mitgeführtem Feinstaub befreit. Nachfolgend wird das gewaschene Rohgas weiteren Behandlungsstufen zugeführt.Of the Fuel is produced as slurry by pumping to gasification pressure brought and fed at the top of the reactor via burner. It can simultaneously gasified one or more fuels or coals become. The raw gas leaves the Gasification room together with the liquefied slag at the bottom End of the reactor and is then injected by injecting Water at 700 ° C up to 1100 ° C partially cooled and freed of entrained particulate matter after waste heat recovery. following the scrubbed raw gas is fed to further treatment stages.
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 technology of gas generation, the autothermal entrained flow gasification of solid, liquid and gaseous fuels has been known for many years. The ratio of fuel to oxygen-containing gasification agents is chosen so that due to the synthesis gas quality higher carbon compounds to synthesis gas components such as CO and H 2 are completely split and the inorganic components are discharged as molten slag, see J. Carl, P. Fritz, NOELL- CONVERSION PROCESS, 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 der 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.By Ch. Higman and M. van der Burgt in "Gasification", page 124, published by Elsevier 2003, a process is presented in which the hot gasification gas leaves the gasifier together with the liquid slag and enters directly into a waste heat boiler arranged vertically underneath, in which the raw gas and the slag are cooled by using the waste heat for steam generation Slag accumulates in a water bath, the cooled raw gas leaves the waste heat boiler sideways. The advantage of waste heat recovery according to this system faces a number of disadvantages. Mention may be particularly the formation of deposits on the heat exchanger tubes, which lead to the obstruction of heat transfer and corrosion and erosion and thus lack of availability.
CN 200 4200 200 7.1 beschreibt einen „Solid Pulverized Fuel Gasifier", bei dem der Kohlenstaub pneumatisch zugeführt wird und Vergasungsgas und verflüssigte Schlacke über ein zentrales Rohr zur weiteren Abkühlung in ein Wasserbad eingeleitet werden. Diese zentrale Abführung im genannten Zentralrohr ist anfällig gegen Verstopfungen, die den Gesamtbetrieb stören und die Verfügbarkeit der Gesamtanlage mindern.CN 200 4200 200 7.1 describes a "Solid Pulverized Fuel Gasifier" in which the coal dust is pneumatically supplied is and gasification gas and liquefied Slag over a central tube is introduced into a water bath for further cooling. This central exhaustion in said central tube is vulnerable against blockages that disrupt the overall operation and availability reduce the overall investment.
Ausgehend von diesem Stand der Technik ist es Aufgabe der Erfindung, eine Möglichkeit zu schaffen, die bei einer zuverlässigen Betriebsweise den unterschiedlichen Aschegehalten der Brennstoffe Rechnung trägt und eine hohe Verfügbarkeit aufweist.outgoing From this prior art, it is an object of the invention, a possibility which, given a reliable mode of operation, provides the different Ash content of the fuels takes into account and high availability having.
Diese Aufgabe wird durch ein Vergasungsverfahren nach den Merkmalen des ersten Patentanspruches und eine Vorrichtung nach Anspruch 13 gelöst. Unteransprüche geben vorteilhafte Ausführungen der Erfindung wieder.These Task is performed by a gasification process according to the characteristics of first claim and a device according to claim 13 solved. Subordinate claims advantageous embodiments the invention again.
Das
Vergasungsverfahren zur Vergasung von festen aschehaltigen Brennstoffen
mit einem sauerstoffhaltigen Oxidationsmittel in einem als Flugstromreaktor
ausgebildeten Vergasungsraum bei Drücken zwischen Umgebungsdruck
und 100 bar, bei dem die Reaktionsraumkontur durch ein Kühlsystem
begrenzt wird, wobei der Druck im Kühlsystem immer höher gehalten
wird als der Druck im Reaktionsraum, zeichnet sich durch folgende
Merkmale aus:
Der Brennstoff, z. B. Steinkohlen, Stein- und
Braunkohlenkokse sowie Biomassekokse und/oder Petrolkokse bzw. ihre
Mischungen, werden auf eine Körnung < 500 μm, vorzugsweise < 200 μm, zerkleinert und
unter Zugabe von Flüssigkeiten
wie Wasser oder Öl
zu einer Brennstoff-Wasser- oder Brennstoff-Öl-Suspension, einen sogenannten
Slurry, vermischt. Bei Verwendung von Wasser als Trägermedium
erreicht man unter Zusatz von Tensiden stabile Feststoffkonzentrationen
bis 70 Ma%. Diese werden mittels geeigneter Pumpen auf den gewünschten Vergasungsdruck
bis maximal 100 bar gebracht und über geeignete Brenner, die
am Kopf des Vergasungsreaktors angebracht sind, der Vergasungsreaktion
zugeführt.
Durch Mess-, Regel- und Überwachungseinrichtungen
wird die Brennstoffkonzentration im Slurry sowie die strömende Slurrymenge überwacht,
gemessen und geregelt. Dem Brenner wird gleichzeitig ein freien
Sauerstoff enthaltendes Oxidationsmittel zugeführt und der Brennstoffslurry
durch partielle Oxidation in ein Rohsynthesegas überführt. Die Vergasung findet bei
Temperaturen zwischen 1.200 und 1.900°C bei Drücken bis 100 bar statt. Der Reaktor
ist mit einem Kühlschirm
ausgestattet, der aus gasdicht verschweißten und wassergekühlten Rohren
besteht.The gasification process for the gasification of solid ash-containing fuels with an oxygen-containing oxidant in a trained as a fly-reactor gasification at pressures between ambient pressure and 100 bar, wherein the reaction space contour is limited by a cooling system, the pressure in the cooling system is always kept higher than the pressure in the reaction chamber , characterized by the following features:
The fuel, z. As hard coal, lignite and lignite coke and biomass coke and / or petroleum coke or their mixtures are crushed to a grain size <500 microns, preferably <200 microns and with the addition of liquids such as water or oil to a fuel-water or fuel Oil suspension, a so-called slurry, mixed. When using water as the carrier medium is achieved with the addition of surfactants stable solids concentrations up to 70 Ma%. These are brought by suitable pumps to the desired gasification pressure up to a maximum of 100 bar and fed via suitable burners, which are attached to the head of the gasification reactor, the gasification reaction. The fuel concentration in the slurry as well as the flowing amount of slurry are monitored, measured and controlled by measuring, regulating and monitoring devices. The burner is simultaneously fed to a free oxygen-containing oxidant and the fuel slurry is converted by partial oxidation in a Rohsynthesegas. The gasification takes place at temperatures between 1,200 and 1,900 ° C at pressures up to 100 bar. The reactor is equipped with a cooling screen consisting of gas-tight welded and water-cooled pipes.
Das heiße Rohsynthesegas 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 oder durch Zuführung eines kühlen Gases eine Teilquenchung, also eine Abkühlung auf Temperaturen zwischen 700 °C und 1.100°C erfolgt. Bei dieser Temperatur ist die mitgeführte flüssige Schlacke soweit abgekühlt, dass sie nicht mehr an den metallischen Oberflächen haften kann. Das auf die Temperaturen von 700 °C und 1.100° abgekühlte Rohgas gelangt hiernach gemeinsam mit der gleichfalls gekühlten festen Schlacke in einen Abhitzekessel zur Nutzung der fühlbaren Wärme zur Dampferzeugung. Durch diese vorangehende Teilquenchung oder Teilkühlung wird die Gefahr des Anbackens von Schlacke an die Abhitzekühlrohre verhindert oder stark begrenzt. Das für die Teilquenchung erforderliche Wasser oder rückgeführtes Gaskondensat wird über Düsen zugeführt, die sich direkt am Mantel befinden. Die abgekühlte Schlacke sammelt sich in einem Wasserbad, das am unteren Ende des Abhitzekessels angeordnet ist. Das auf ca. 200 °C-300 °C abgekühlte Rohgas verlässt seitlich den Abhitzekessel und gelangt in eine Rohgaswäsche, die zweckmäßiger Weise als Venturiwäsche ausgebildet ist. 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 °C 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 abgeschieden. Das so gereinigte Rohgas kann danach direkt, beispielsweise einer Rohgaskonvertierung oder Entschwefelungsanlage, zugeführt werden.The name is Raw synthesis gas leaves together with the formed from the fuel ash liquid slag the gasification reactor and enters a space arranged vertically below, in which by injecting water or by supplying a cool gas a partial quenching, ie a cooling to temperatures between 700 ° C and 1100 ° C he follows. At this temperature, the entrained liquid slag is cooled so far that they can no longer adhere to the metallic surfaces. That on the Temperatures of 700 ° C and 1,100 ° cooled raw gas thereafter comes together with the equally cooled solid Slag in a waste heat boiler to use the tangible Heat to Steam production. By this previous partial quenching or partial cooling is prevents the risk of caking of slag to the waste heat cooling pipes or severely limited. That for the Teilquenchung required water or recycled gas condensate is supplied via nozzles, the are located directly on the jacket. The cooled slag collects in a water bath placed at the bottom of the waste heat boiler is. The cooled to about 200 ° C-300 ° C raw gas leaves laterally the waste heat boiler and enters a raw gas scrubbing, the expedient manner as Venturi wash is trained. Here, the entrained dust is up to a particle size of approx. 20 μm away. This degree of purity is not enough, then catalytic Processes such as a raw gas conversion perform. there is further to consider that in addition Salt mist in the raw gas entrained be that while the gasification of the fuel dust be released and removed with the raw gas. To both the fine dust <20 microns and removing the salt mist, the scrubbed raw gas is a condensation stage fed in the raw gas indirectly by 5 ° C up to 10 ° C chilled becomes. In this case, water is condensed from the water vapor-saturated crude gas, which absorbs the described fine dust and salt particles. In a subsequent Separator is the condensed the dust and salt particles contained Water separated. The purified crude gas can then be directly, for example, a raw gas conversion or desulphurisation plant, supplied become.
An Stelle der Wasch- und Kondensationsstufe kann eine bei 200 °C bis 300 °C arbeitende mechanische Staubabscheidung vorgesehen werden, wobei Fliehkraftabscheider oder Filtersysteme eingesetzt werden können.Instead of washing and Kondensststu Fe can be provided at 200 ° C to 300 ° C working mechanical dust separation, with centrifugal or filter systems can be used.
Im Folgenden wird die Erfindung an 3 Figuren und einem Ausführungsbeispiel näher erläutert. Die Figuren zeigen:in the Below, the invention of 3 figures and an embodiment explained in more detail. The Figures show:
Eine
Steinkohlenmenge von 320 t/h mit einer Zusammensetzung von
Der
Vergasungsreaktor ist in den
Der
Vergasungsraum
Die gereinigte feuchte Rohgasmenge beträgt 775.000 Nm3/h. Sie kann direkt einer Rohgaskonvertierung oder anderen Behandlungsstufen zugeführt werden.The purified wet raw gas quantity is 775,000 Nm 3 / h. It can be fed directly to a crude gas conversion or other treatment stages.
- 11
- Slurryherstellung und -zuführungslurry preparation and feeding
- 1.11.1
- SlurryleitungSlurryleitung
- 22
- Reaktorreactor
- 2.12.1
- Leitung für Sauerstoffmanagement for oxygen
- 2.22.2
- Brennerburner
- 2.32.3
- Vergasungsraumgasification chamber
- 2.42.4
- Kühlschirmcooling screen
- 2.52.5
- Austrittsöffnungoutlet opening
- 33
- Quenchkühlerquench
- 3.13.1
- Quenchraumquench
- 3.23.2
-
Düsen in
3 Nozzles in3 - 3.43.4
-
Transferleitung
von
3 zu4 Transfer line from3 to4 - 44
- Abhitzekesselwaste heat boiler
- 4.14.1
-
Kühlrohre
im Abhitzekessel
4 Cooling tubes in the waste heat boiler4 - 4.24.2
-
Wasserbad
mit Schlacke in
4 Water bath with slag in4 - 4.34.3
-
Schlackeabzug
aus
4 Slag vent off4 - 4.44.4
-
Öffnung aus
4 zum Rohgaswäscher5 Opening off4 to the crude gas scrubber5 - 4.54.5
-
Wasserbad
mit Schlacke
4 Water bath with slag4 - 4.64.6
-
Schlackeabzug
aus
4 Slag vent off4 - 55
- RohgaswäscherRohgaswäscher
- 66
- Teilkondensatorpartial condenser
Claims (21)
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102005042640A DE102005042640A1 (en) | 2005-09-07 | 2005-09-07 | Process and apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels with partial quenching and waste heat recovery |
DE202005021662U DE202005021662U1 (en) | 2005-09-07 | 2005-09-07 | Apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels with partial quenching and waste heat recovery |
CNA2005101141525A CN1928028A (en) | 2005-09-07 | 2005-10-26 | Method and device for producing synthesis gases by partial oxidation of slurries |
US11/349,883 US20070051043A1 (en) | 2005-09-07 | 2006-02-08 | Method and device for producing synthesis by partial oxidation of slurries made from fuels containing ash with partial quenching and waste heat recovery |
CA002537787A CA2537787A1 (en) | 2005-09-07 | 2006-02-27 | Method and device for producing synthesis gases by partial oxidation of slurries made from fuels containing ash with partial quenching and waste heat recovery |
AU2006201144A AU2006201144A1 (en) | 2005-09-07 | 2006-03-20 | Method and device for producing synthesis gases by partial oxidation of slurries made from fuels containing ash with partial quenching and waste heat recovery |
ZA2006/07265A ZA200607265B (en) | 2005-09-07 | 2006-08-31 | Method and device for producing synthesis gases by partial oxidation of slurries made from fuels containing ash with partial quenching and waste heat recovery |
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DE102005042640A DE102005042640A1 (en) | 2005-09-07 | 2005-09-07 | Process and apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels with partial quenching and waste heat recovery |
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DE202005021662U Expired - Lifetime DE202005021662U1 (en) | 2005-09-07 | 2005-09-07 | Apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels with partial quenching and waste heat recovery |
DE102005042640A Withdrawn DE102005042640A1 (en) | 2005-09-07 | 2005-09-07 | Process and apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels with partial quenching and waste heat recovery |
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US (1) | US20070051043A1 (en) |
CN (1) | CN1928028A (en) |
AU (1) | AU2006201144A1 (en) |
CA (1) | CA2537787A1 (en) |
DE (2) | DE202005021662U1 (en) |
ZA (1) | ZA200607265B (en) |
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2005
- 2005-09-07 DE DE202005021662U patent/DE202005021662U1/en not_active Expired - Lifetime
- 2005-09-07 DE DE102005042640A patent/DE102005042640A1/en not_active Withdrawn
- 2005-10-26 CN CNA2005101141525A patent/CN1928028A/en active Pending
-
2006
- 2006-02-08 US US11/349,883 patent/US20070051043A1/en not_active Abandoned
- 2006-02-27 CA CA002537787A patent/CA2537787A1/en not_active Abandoned
- 2006-03-20 AU AU2006201144A patent/AU2006201144A1/en not_active Abandoned
- 2006-08-31 ZA ZA2006/07265A patent/ZA200607265B/en unknown
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DE112009000341B4 (en) | 2008-02-21 | 2024-02-01 | Air Products And Chemicals, Inc. | Methods and systems for integrated boiler feed water heating |
DE102009019966A1 (en) * | 2009-04-27 | 2010-11-04 | Siemens Aktiengesellschaft | Suspended particle gasifier has partial quenching chamber above quench tank, with gas outlet geometry separating entrained particles ahead of waste heat recovery boiler |
DE102010045482A1 (en) | 2010-09-16 | 2012-03-22 | Choren Industries Gmbh | Slag treatment device for coal gasifier plant, has dip tube with inner and outer pipes between which annular gap is formed and connected with annular coolant chamber, and coolant feed pipe connected at lower portion of dip tube |
WO2012034700A2 (en) | 2010-09-16 | 2012-03-22 | Choren Industries Gmbh | Device and method for treating a hot gas flow containing slag |
US8945286B2 (en) | 2010-09-16 | 2015-02-03 | Ccg Energy Technology Company Ltd. | Device and method for treating a hot gas flow containing slag |
DE102013003413A1 (en) | 2013-02-28 | 2014-09-11 | Linde Aktiengesellschaft | Method and device for separating liquid slag particles |
Also Published As
Publication number | Publication date |
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US20070051043A1 (en) | 2007-03-08 |
ZA200607265B (en) | 2008-01-08 |
AU2006201144A1 (en) | 2007-03-22 |
CA2537787A1 (en) | 2007-03-07 |
DE202005021662U1 (en) | 2009-03-05 |
CN1928028A (en) | 2007-03-14 |
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