EP0948583B1 - Method of gasifying solid fuels in a circulating fluidized bed - Google Patents

Method of gasifying solid fuels in a circulating fluidized bed Download PDF

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Publication number
EP0948583B1
EP0948583B1 EP97952838A EP97952838A EP0948583B1 EP 0948583 B1 EP0948583 B1 EP 0948583B1 EP 97952838 A EP97952838 A EP 97952838A EP 97952838 A EP97952838 A EP 97952838A EP 0948583 B1 EP0948583 B1 EP 0948583B1
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EP
European Patent Office
Prior art keywords
gas
solids
hydrocarbons
dust
separator
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Expired - Lifetime
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EP97952838A
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German (de)
French (fr)
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EP0948583A1 (en
Inventor
Johannes Albrecht
Johannes Loeffler
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MG Technologies AG
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Metallgesellschaft AG
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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
    • C10J3/58—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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • 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
    • C10J3/58—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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/008—Reducing the tar content by cracking
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas

Definitions

  • the invention relates to a process for gasifying solid fuels in the circulating fluidized bed, the fuels being gasified in a gasification reactor with the supply of oxygen-containing gas at temperatures in the range from 700 to 1000.degree. C., a gas-solid mixture from the upper area of the gasification reactor Separator feeds, from the separator dust and hydrocarbons including higher hydrocarbons with more than 6 carbon atoms in the molecule (C 6+ hydrocarbons) containing gas with a calorific value of 2000 to 8000 kJ / m 3 and separately separated solids and the solids leads at least partially back into the lower region of the gasification reactor.
  • the invention has for its object to modify the known methods so that the dust is removed dry and wet washing with the formation of waste water in the gas cleaning is eliminated. According to the invention, this is achieved in the process mentioned at the outset by passing the dust-containing gas from the separator through a cracking chamber, with the gas contained in the cracking chamber with the addition of gaseous oxygen in the temperature range from 800 to 1200 ° C.
  • Hydrocarbons largely splits and the content of the higher hydrocarbons (C 6+ hydrocarbons) in the gas is reduced to a maximum of 10% by weight of the content of these higher hydrocarbons in the gas coming from the separator by cooling the gas coming from the splitting chamber which conducts the cooled gas through a dedusting device and separates flue dust, that the cooled and dedusted gas is passed through at least one bed or a reactor with granular solids which binds pollutants and then dedusts the gas, and that at least part of the flue dust extracted from the dedusting device is removed s in a combustion chamber at temperatures in the range of 1000 to 1500 ° C with the addition of gas containing O 2 .
  • the solid fuels to be gasified can e.g. B. um municipal or industrial waste, biomass or coal act in different ways.
  • Municipal waste is gasified this is usually done before gasification pre-sorted, especially metal and glass parts be discarded.
  • the remaining waste is then still crushed, e.g. B. to piece sizes of at most 70 mm before it is gassed.
  • To increase the calorific value of the from the Gasification reactor coming gas can be the solid fuel dry before gasification.
  • the one from the bottom of the gasification reactor drawn ash is usually so inert that it z. B. still is usable for road construction, but at least the ashes are easy to deposit.
  • the one in the dust collector Air dust can be heavy metal and then disposed of in the usual way. You burn or gasifies at least part of the airborne dust in a combustion chamber at temperatures in the range of 1000 to 1500 ° C. It is recommended that in the combustion chamber formed gaseous products in the gasification reactor give.
  • the solid fuels to be gasified are fed in line (1) to a gasification reactor (2), where they come into contact with hot gases and particles in the state of the circulating fluidized bed.
  • Oxygen-containing fluidizing gas is introduced in line (3) and passed through a distribution chamber (4) with a grate (5) into the fluidized bed of the reactor (2).
  • the oxygen-containing gas in line (3) can be, for example, air or air enriched with O 2 .
  • the gasification in the reactor (2) takes place at temperatures of 700 to 1000 ° C and mostly at temperatures of at least 800 ° C.
  • Ash is drawn off through line (6) and, if necessary, is deposited after removal of metal components or for further use, e.g. B. in road construction.
  • the dust-containing gas of line (10) contains condensable hydrocarbons and mostly carbon-containing fly dusts. It is important to at least largely eliminate the higher hydrocarbons (C 6+ ) and convert them into substances that do not condense at the given temperatures and partial pressures.
  • the gas is passed through a cracking chamber (12) through which line (13) O 2 -containing gas, for. B. air, oxygen-enriched air or technically pure oxygen. Temperatures in the range from 800 to 1200 ° C and mostly 900 to 1100 ° C are ensured in the gap chamber (12). It is important here that the temperature and the residence time in the cracking chamber (12) are chosen so that the formation of liquid slag is avoided and at the same time an adequate cracking of the C 6+ hydrocarbons is ensured.
  • the gas coming from the gap chamber (12) in line (15) contains various types of solids and ash particles, which are here be referred to as flying dust.
  • a waste heat boiler (16) cooling the gas to temperatures of about 150 to 300 ° C and then there is one through line (17) Dedusting device (18).
  • This can be, for. B. um act a tissue or electrostatic precipitator.
  • the accruing Airborne dust which usually contains heavy metals, is in the Line (19) withdrawn, part of it can be transported (20) to a combustion chamber (21). The rest Airborne dust is removed from the process through line (22) away.
  • oxygen-containing gas for. B. air, enriched with O 2 or technically pure oxygen and burns the supplied dust at temperatures in the range of 1000 to 1500 ° C.
  • the resulting solid or liquid and gaseous combustion products are put together in the upper area of the reactor (2), where they are taken up by the fluidized bed. 1, liquid slag can also be drawn off from the combustion chamber (21) in such a way that it does not get into the reactor (2), see FIG. 2.
  • a gas which still contains an interfering content Has pollutants.
  • pollutants are e.g. B. mercury, chlorine and sulfur compounds.
  • the cooled gas is led through the Line (27) for cleaning, whereby the formation of Avoids waste water.
  • the gas to be cleaned is in contact with granular adsorbents brought.
  • These adsorbents can e.g. B. in a fixed bed, Moving bed or fluidized bed can be arranged or you can get one Use entrained flow reactor.
  • Moving bed reactor (30) shown which one through the line (31) feeds granular adsorbent material in the reactor (30) forms a bed (33) which slowly moves downwards.
  • the fill is approximately in the horizontal direction from to flows through cleaning gas.
  • the gas leaves the reactor (30) through the line (35) and is dusted by the filter (36) performed, for. B. a tissue or Can act electrostatic precipitator.
  • Cleaned gas leaves the filter (36) in line (37). That coming from the reactor (30) loaded adsorbent is removed in line (38), with the solids in the line separated in the filter (36) (39) mixed and subtracted.
  • Adsorption materials are particularly the following Options: hydrated lime, activated carbon, stove coke or Zeolites.
  • the mercury removal using a Low-aluminum zeolites are described in EP patent 638 351.
  • FIG. 2 gives the pollutant gas line (27) one Spray absorber (40), to which one passes through the line (41) milk of lime and possibly other adsorbents.
  • Gas and Solids flow through line (42) to a filter (43), which is e.g. B. can be a fabric or electrostatic filter can.
  • Chloride-containing solids are drawn off in line (45).
  • In the combustion chamber (21) is pulled through the liquid slag Line (23) and leads the combustion gas through the line (32) into the reactor (2).
  • Residual municipal waste is fed to a process according to FIG. 2.
  • the following data are partially calculated.
  • the residual waste which is delivered in an amount of 7500 kg / h, contains 24.5% by weight moisture and 30% by weight ash.
  • This waste is first dried to 5% by weight of residual moisture and then gasified in the reactor (2) at 900 ° C. and with the supply of 6230 Nm 3 / h of air.
  • the residence time of the gas in the gap chamber (12) is 1.5 seconds, air is supplied through line (13) and an outlet temperature of 1000 ° C. is reached.
  • the content of C 6+ hydrocarbons in line (15) is only 0.1% by volume.
  • 400 kg / h of dust are fed through the line (20) into the combustion chamber (21), which is fed with 1860 Nm 3 / h of air and in which 1300 ° C. can be reached.
  • Lime milk is added to the spray absorber (40) and the outlet temperature is kept at 160 ° C.
  • the adsorber (46) contains a zeolite fixed bed for mercury removal.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Industrial Gases (AREA)
  • Treating Waste Gases (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Description

Die Erfindung betrifft ein Verfahren zum Vergasen von Festbrennstoffen in der zirkulierenden Wirbelschicht, wobei man die Brennstoffe in einem Vergasungsreaktor unter Zufuhr von sauerstoffhaltigem Gas bei Temperaturen im Bereich von 700 bis 1000°C vergast, vom oberen Bereich des Vergasungsreaktors ein Gas-Feststoff-Gemisch einem Abscheider zuführt, aus dem Abscheider Staub und Kohlenwasserstoffe einschließlich höherer Kohlenwasserstoffe mit mehr als 6 C-Atomen im Molekül (C6+-Kohlenwasserstoffe) enthaltendes Gas mit einem Heizwert von 2000 bis 8000 kJ/m3 und getrennt davon abgeschiedene Feststoffe ableitet und die Feststoffe mindestens teilweise in den unteren Bereich des Vergasungsreaktors zurückführt.The invention relates to a process for gasifying solid fuels in the circulating fluidized bed, the fuels being gasified in a gasification reactor with the supply of oxygen-containing gas at temperatures in the range from 700 to 1000.degree. C., a gas-solid mixture from the upper area of the gasification reactor Separator feeds, from the separator dust and hydrocarbons including higher hydrocarbons with more than 6 carbon atoms in the molecule (C 6+ hydrocarbons) containing gas with a calorific value of 2000 to 8000 kJ / m 3 and separately separated solids and the solids leads at least partially back into the lower region of the gasification reactor.

Verfahren dieser Art sind aus DE-A-42 35 412 (hierzu korrespondiert US-A-5 425 317) und DE-A-44 12 004 bekannt. Bei den bekannten Verfahren wird das aus dem Abscheider kommende, brennbare Bestandteile enthaltende Gas unter Bildung flüssiger Schlacke vergast oder verbrannt, und die flüssige Schlacke wird aus dem Verfahren entfernt. Das bei der Verbrennung oder Vergasung entstehende Gas wird im Kontakt mit Waschflüssigkeit gereinigt. Dabei wird es notwendig, die gebrauchte Waschflüssigkeit aufzubereiten oder zu entsorgen. Beim aus DE-A-27 29 764 bekannten Verfahren wird die Asche aus der Vergasung nachverbrannt, und das aus dem Zyklon-Abscheider kommende heiße Gas wird sofort gekühlt, bevor es naß gereinigt wird. Methods of this type are described in DE-A-42 35 412 (see corresponds to US-A-5 425 317) and DE-A-44 12 004. At In the known processes, the Gas containing flammable constituents to form liquid Slag gasifies or burns, and the liquid slag is removed from the process. That with the combustion or Gasification generated gas is in contact with washing liquid cleaned. It becomes necessary to use the Process or dispose of washing liquid. When out DE-A-27 29 764 known method is the ashes from the Afterburning gasification, and that from the cyclone separator Coming hot gas is cooled immediately before being cleaned wet becomes.

Der Erfindung liegt die Aufgabe zugrunde, die bekannten Verfahren so abzuwandeln, daß der Flugstaub trocken entfernt wird und die Naßwäsche mit Bildung von Abwasser in der Gasreinigung entfällt. Erfindungsgemäß gelingt dies beim eingangs genannten Verfahren dadurch, daß man das staubhaltige Gas aus dem Abscheider durch eine Spaltkammer leitet, wobei man in der Spaltkammer unter Zufuhr von gasförmigem Sauerstoff im Temperaturbereich von 800 bis 1200°C und unter der Temperatur des Ascheschmelzpunktes die im Gas enthaltenen Kohlenwasserstoffe weitgehend spaltet und dabei den Gehalt an den höheren Kohlenwasserstoffen (C6+-Kohlenwasserstoffen) im Gas auf höchstens 10 Gew.-% des Gehalts an diesen höheren Kohlenwasserstoffen im aus dem Abscheider kommenden Gas verringert, daß man das aus der Spaltkammer kommende Gas kühlt, das gekühlte Gas durch eine Entstaubungseinrichtung leitet und Flugstaub abtrennt, daß man das gekühlte und entstaubte Gas durch mindestens ein Bett oder einen Reaktor mit Schadstoffe bindenden körnigen Feststoffen leitet und das Gas anschließend entstaubt, und daß man mindestens einen Teil des aus der Entstaubungseinrichtung abgezogenen Flugstaubs in einer Brennkammer bei Temperaturen im Berreich von 1000 bis 1500°C unter Zugabe von O2-haltigem Gas umsetzt. The invention has for its object to modify the known methods so that the dust is removed dry and wet washing with the formation of waste water in the gas cleaning is eliminated. According to the invention, this is achieved in the process mentioned at the outset by passing the dust-containing gas from the separator through a cracking chamber, with the gas contained in the cracking chamber with the addition of gaseous oxygen in the temperature range from 800 to 1200 ° C. and below the temperature of the ash melting point Hydrocarbons largely splits and the content of the higher hydrocarbons (C 6+ hydrocarbons) in the gas is reduced to a maximum of 10% by weight of the content of these higher hydrocarbons in the gas coming from the separator by cooling the gas coming from the splitting chamber which conducts the cooled gas through a dedusting device and separates flue dust, that the cooled and dedusted gas is passed through at least one bed or a reactor with granular solids which binds pollutants and then dedusts the gas, and that at least part of the flue dust extracted from the dedusting device is removed s in a combustion chamber at temperatures in the range of 1000 to 1500 ° C with the addition of gas containing O 2 .

Durch die Bedingungen in der Spaltkammer und den Bedingungen in der Gasreinigung unterbleibt die Kondensation und Sublimation der höheren Kohlenwasserstoffe (C6+) in den nachgeschalteten Gasreinigungseinrichtungen.Due to the conditions in the cracking chamber and the conditions in the gas cleaning, the condensation and sublimation of the higher hydrocarbons (C 6+ ) does not take place in the downstream gas cleaning devices.

Bei den zu vergasenden Festbrennstoffen kann es sich z. B. um kommunalen oder industriellen Müll, Biomassen oder Kohlen verschiedener Art handeln. Bei der Vergasung von kommunalem Müll wird dieser üblicherweise vor der Vergasung zunächst vorsortiert, wobei insbesondere Metall- und Glasteile ausgesondert werden. Der verbleibende Restmüll wird dann noch zerkleinert, z. B. auf Stückgrößen von höchstens 70 mm, bevor er vergast wird. Zur Erhöhung des Heizwertes des aus dem Vergasungsreaktor kommenden Gases kann man die Festbrennstoffe vor der Vergasung trocknen.In the solid fuels to be gasified, it can e.g. B. um municipal or industrial waste, biomass or coal act in different ways. When municipal waste is gasified this is usually done before gasification pre-sorted, especially metal and glass parts be discarded. The remaining waste is then still crushed, e.g. B. to piece sizes of at most 70 mm before it is gassed. To increase the calorific value of the from the Gasification reactor coming gas can be the solid fuel dry before gasification.

Beim erfindungsgemäßen Verfahren fallen keine flüssigen Reststoffe an. Die vom unteren Bereich des Vergasungsreaktors abgezogene Asche ist üblicherweise so inert, daß sie z. B. noch für den Straßenbau verwertbar ist, zumindest aber ist die Asche leicht deponierbar. Der in der Entstaubungseinrichtung anfallende Flugstaub kann schwermetallhaltig sein und wird dann in üblicher Weise entsorgt. Man verbrennt oder vergast mindestens einen Teil des anfallenden Flugstaubes in einer Brennkammer bei Temperaturen im Bereich von 1000 bis 1500°C. Dabei empfiehlt es sich, die in der Brennkammer gebildeten gasförmigen Produkte in den Vergasungsreaktor zu geben.In the method according to the invention, no liquid falls Residues. The one from the bottom of the gasification reactor drawn ash is usually so inert that it z. B. still is usable for road construction, but at least the ashes are easy to deposit. The one in the dust collector Air dust can be heavy metal and then disposed of in the usual way. You burn or gasifies at least part of the airborne dust in a combustion chamber at temperatures in the range of 1000 to 1500 ° C. It is recommended that in the combustion chamber formed gaseous products in the gasification reactor give.

Ausgestaltungsmöglichkeiten des Verfahrens werden mit Hilfe der Zeichnung erläutert. Es zeigt

  • Fig. 1 das Fließschema einer ersten Verfahrensvariante und
  • Fig. 2 das Fließschema einer zweiten Verfahrensvariante.
    • Design options of the method are explained with the aid of the drawing. It shows
  • Fig. 1 shows the flow diagram of a first process variant and
  • Fig. 2 shows the flow diagram of a second process variant.

    • Gemäß Fig. 1 werden die zu vergasenden Festbrennstoffe in der Leitung (1) einem Vergasungsreaktor (2) zugeführt, wo sie mit heißen Gasen und Partikeln im Zustand der zirkulierenden Wirbelschicht in Kontakt kommen. Sauerstoffhaltiges Fluidisierungsgas wird in der Leitung (3) herangeführt und durch eine Verteilkammer (4) mit einem Rost (5) in die Wirbelschicht des Reaktors (2) geleitet. Beim sauerstoffhaltigen Gas der Leitung (3) kann es sich zum Beispiel um Luft oder mit O2 angereicherte Luft handeln. Die Vergasung im Reaktor (2) erfolgt bei Temperaturen von 700 bis 1000°C und zumeist bei Temperaturen von mindestens 800°C. Asche wird durch die Leitung (6) abgezogen und wird, falls nötig, nach Entfernung von Metallbestandteilen deponiert oder einer weiteren Verwendung, z. B. im Straßenbau, zugeführt.According to FIG. 1, the solid fuels to be gasified are fed in line (1) to a gasification reactor (2), where they come into contact with hot gases and particles in the state of the circulating fluidized bed. Oxygen-containing fluidizing gas is introduced in line (3) and passed through a distribution chamber (4) with a grate (5) into the fluidized bed of the reactor (2). The oxygen-containing gas in line (3) can be, for example, air or air enriched with O 2 . The gasification in the reactor (2) takes place at temperatures of 700 to 1000 ° C and mostly at temperatures of at least 800 ° C. Ash is drawn off through line (6) and, if necessary, is deposited after removal of metal components or for further use, e.g. B. in road construction.

    Am oberen Ende des Reaktors (2) verläßt ein Gas-Feststoff-Gemisch den Reaktor durch den Kanal (8) und strömt in einen Zyklon-Abscheider (9), aus welchem durch die Leitung (10) staubhaltiges Brenngas abgezogen wird. Im Abscheider (9) anfallende Feststoffe werden durch die Leitung (11) zurück in den unteren Bereich des Reaktors (2) geführt.Leaves at the top of the reactor (2) Gas-solid mixture the reactor through the channel (8) and flows in a cyclone separator (9), from which through the line (10) dust-containing fuel gas is withdrawn. In the separator (9) resulting solids are fed back through line (11) led the lower region of the reactor (2).

    Das staubhaltige Gas der Leitung (10) enthält kondensierbare Kohlenwasserstoffe und zumeist kohlenstoffhaltige Flugstäube. Wichtig ist, die höheren Kohlenwasserstoffe (C6+) zumindest weitgehend zu beseitigen und sie in Substanzen zu überführen, die bei den gegebenen Temperaturen und Partialdrücken nicht kondensieren. Zu diesem Zweck führt man das Gas durch eine Spaltkammer (12), der man durch die Leitung (13) O2-haltiges Gas, z. B. Luft, mit Sauerstoff angereicherte Luft oder technisch reinen Sauerstoff zuführt. In der Spaltkammer (12) sorgt man für Temperaturen im Bereich von 800 bis 1200°C und zumeist 900 bis 1100°C. Wichtig ist hierbei, daß man die Temperatur und die Verweilzeit in der Spaltkammer (12) so wählt, daß die Bildung flüssiger Schlacke vermieden wird und gleichzeitig eine ausreichende Spaltung der C6+-Kohlenwasserstoffe gewährleistet ist.The dust-containing gas of line (10) contains condensable hydrocarbons and mostly carbon-containing fly dusts. It is important to at least largely eliminate the higher hydrocarbons (C 6+ ) and convert them into substances that do not condense at the given temperatures and partial pressures. For this purpose, the gas is passed through a cracking chamber (12) through which line (13) O 2 -containing gas, for. B. air, oxygen-enriched air or technically pure oxygen. Temperatures in the range from 800 to 1200 ° C and mostly 900 to 1100 ° C are ensured in the gap chamber (12). It is important here that the temperature and the residence time in the cracking chamber (12) are chosen so that the formation of liquid slag is avoided and at the same time an adequate cracking of the C 6+ hydrocarbons is ensured.

    Das in der Leitung (15) aus der Spaltkammer (12) kommende Gas enthält verschiedenartige Feststoffe und Aschepartikel, die hier als Flugstaub bezeichnet werden. In einem Abhitzekessel (16) kühlt man das Gas auf Temperaturen von etwa 150 bis 300°C und gibt es dann durch die Leitung (17) einer Entstaubungseinrichtung (18) auf. Hierbei kann es sich z. B. um ein Gewebe- oder Elektrofilter handeln. Der anfallende Flugstaub, der üblicherweise schwermetallhaltig ist, wird in der Leitung (19) abgezogen, ein Teil davon kann auf dem Transportweg (20) zu einer Brennkammer (21) geführt werden. Der restliche Flugstaub wird durch die Leitung (22) aus dem Verfahren entfernt.The gas coming from the gap chamber (12) in line (15) contains various types of solids and ash particles, which are here be referred to as flying dust. In a waste heat boiler (16) cooling the gas to temperatures of about 150 to 300 ° C and then there is one through line (17) Dedusting device (18). This can be, for. B. um act a tissue or electrostatic precipitator. The accruing Airborne dust, which usually contains heavy metals, is in the Line (19) withdrawn, part of it can be transported (20) to a combustion chamber (21). The rest Airborne dust is removed from the process through line (22) away.

    Man führt der Brennkammer (21) durch die Leitung (24) sauerstoffhaltiges Gas, z. B. Luft, mit O2 angereicherte Luft oder technisch reinen Sauerstoff zu und verbrennt den zugeführten Flugstaub bei Temperaturen im Bereich von 1000 bis 1500°C. Die dabei entstehenden festen oder flüssigen und gasförmigen Verbrennungsprodukte gibt man gemeinsam in den oberen Bereich des Reaktors (2), wo sie vom Wirbelbett aufgenommen werden. Abweichend von Fig. 1 kann flüssige Schlacke aus der Brennkammer (21) auch so abgezogen werden, daß sie nicht in den Reaktor (2) gelangt, vergleiche Fig. 2.One leads the combustion chamber (21) through the line (24) oxygen-containing gas, for. B. air, enriched with O 2 or technically pure oxygen and burns the supplied dust at temperatures in the range of 1000 to 1500 ° C. The resulting solid or liquid and gaseous combustion products are put together in the upper area of the reactor (2), where they are taken up by the fluidized bed. 1, liquid slag can also be drawn off from the combustion chamber (21) in such a way that it does not get into the reactor (2), see FIG. 2.

    Aus der Entstaubungseinrichtung (18) zieht man in der Leitung (25) ein Gas ab, welches noch einen störenden Gehalt an Schadstoffen aufweist. Bei diesen Schadstoffen handelt es sich z. B. um Quecksilber-, Chlor- und Schwefel-Verbindungen. Um diese Schadstoffe weitgehend zu entfernen, führt man das Gas zunächst durch einen indirekten Kühler (26) und stellt die für die nachfolgende Behandlung günstige Temperatur z. B. im Bereich von 100 bis 150°C ein. Das gekühlte Gas führt man durch die Leitung (27) einer Reinigung zu, wobei man die Bildung von Abwasser vermeidet. In einem oder mehreren Betten oder Reaktoren wird das zu reinigende Gas mit körnigen Adsorbentien in Kontakt gebracht. Diese Adsorbentien können z. B. im Festbett, Wanderbett oder Wirbelbett angeordnet werden oder man kann einen Flugstromreaktor einsetzen.From the dedusting device (18), one pulls in the line (25) a gas, which still contains an interfering content Has pollutants. These pollutants are e.g. B. mercury, chlorine and sulfur compounds. Around To remove most of these pollutants, you run the gas first by an indirect cooler (26) and provides the for the subsequent treatment favorable temperature z. B. in the area from 100 to 150 ° C. The cooled gas is led through the Line (27) for cleaning, whereby the formation of Avoids waste water. In one or more beds or reactors the gas to be cleaned is in contact with granular adsorbents brought. These adsorbents can e.g. B. in a fixed bed, Moving bed or fluidized bed can be arranged or you can get one Use entrained flow reactor.

    In der Zeichnung ist in schematischer Darstellung ein Wanderbettreaktor (30) dargestellt, dem man durch die Leitung (31) körniges Adsorptionsmaterial zuführt, das im Reaktor (30) eine Schüttung (33) bildet, die sich langsam nach unten bewegt. Dabei wird die Schüttung etwa in horizontaler Richtung vom zu reinigenden Gas durchströmt. Das Gas verläßt den Reaktor (30) durch die Leitung (35) und wird zum Entstauben durch das Filter (36) geführt, bei dem es sich z. B. um ein Gewebe- oder Elektrofilter handeln kann. Gereinigtes Gas verläßt das Filter (36) in der Leitung (37). Das aus dem Reaktor (30) kommende beladene Adsorptionsmittel wird in der Leitung (38) abgeführt, mit den im Filter (36) abgeschiedenen Feststoffen in der Leitung (39) gemischt und abgezogen. In the drawing is a schematic representation Moving bed reactor (30) shown, which one through the line (31) feeds granular adsorbent material in the reactor (30) forms a bed (33) which slowly moves downwards. The fill is approximately in the horizontal direction from to flows through cleaning gas. The gas leaves the reactor (30) through the line (35) and is dusted by the filter (36) performed, for. B. a tissue or Can act electrostatic precipitator. Cleaned gas leaves the filter (36) in line (37). That coming from the reactor (30) loaded adsorbent is removed in line (38), with the solids in the line separated in the filter (36) (39) mixed and subtracted.

    Bei der Auswahl und der Anwendung geeigneter, an sich bekannter Adsorptionsmaterialien gibt es insbesondere folgende Möglichkeiten: Kalkhydrat, Aktivkohle, Herdofenkoks oder Zeolithe. Die Quecksilber-Entfernung mit Hilfe eines aluminiumarmen Zeolithen ist im EP-Patent 638 351 beschrieben.When selecting and using suitable, more well-known Adsorption materials are particularly the following Options: hydrated lime, activated carbon, stove coke or Zeolites. The mercury removal using a Low-aluminum zeolites are described in EP patent 638 351.

    Im Fließschema der Fig. 2 haben die bereits zusammen mit Fig. 1 erwähnten Bezugsziffern die dort erläuterte Bedeutung. Gemäß Fig. 2 gibt man das schadstoffhaltige Gas der Leitung (27) einem Sprühabsorber (40) auf, dem man durch die Leitung (41) Kalkmilch und möglicherweise noch andere Adsorbentien zuführt. Gas und Feststoffe strömen durch die Leitung (42) zu einem Filter (43), bei dem es sich z. B. um ein Gewebe- oder Elektrofilter handeln kann. Gereinigtes Gas gelangt in der Leitung (44) zu einem Adsorber (46) zur Abscheidung von Quecksilber, z. B. in einem Zeolith-Festbett, wie im EP-Patent 638 351 beschrieben. Chloridhaltige Feststoffe zieht man in der Leitung (45) ab. In der Brennkammer (21) zieht man flüssige Schlacke durch die Leitung (23) ab und leitet das Verbrennungsgas durch die Leitung (32) in den Reaktor (2).In the flow diagram of FIG. 2, they already have together with FIG. 1 mentioned reference numbers the meaning explained there. According to Fig. 2 gives the pollutant gas line (27) one Spray absorber (40), to which one passes through the line (41) milk of lime and possibly other adsorbents. Gas and Solids flow through line (42) to a filter (43), which is e.g. B. can be a fabric or electrostatic filter can. Cleaned gas arrives in line (44) Adsorber (46) for the separation of mercury, e.g. B. in one Zeolite fixed bed, as described in EP patent 638 351. Chloride-containing solids are drawn off in line (45). In the combustion chamber (21) is pulled through the liquid slag Line (23) and leads the combustion gas through the line (32) into the reactor (2).

    Beispiel:Example:

    Einer Verfahrensführung gemäß Fig. 2 wird kommunaler Restmüll zugeführt. Die nachfolgenden Daten sind teilweise berechnet. Der Restmüll, der in einer Menge von 7500 kg/h angeliefert wird, enthält 24,5 Gew.-% Feuchte und 30 Gew.-% Asche. Dieser Müll wird zunächst auf 5 Gew.-% Restfeuchte getrocknet und dann im Reaktor (2) bei 900°C und unter Zufuhr von 6230 Nm3/h Luft vergast. Pro Stunde strömen 13000 Nm3 Gas durch die Leitung (-10), das Gas enthält 48 g/Nm3 Staub und 1 Vol.-% C6+-Kohlenwasserstoffe. In der Spaltkammer (12) beträgt die Verweilzeit des Gases 1,5 Sekunden, Luft wird durch die Leitung (13) zugeführt, und es wird eine Austrittstemperatur von 1000°C erreicht. Der Gehalt an C6+-Kohlenwasserstoffen in der Leitung (15) beträgt nur noch 0,1 Vol.-%. Durch die Leitung (20) gibt man 400 kg/h Staub in die Brennkammer (21), die mit 1860 Nm3/h Luft gespeist wird und in der 1300°C erreicht werden. Dem Sprühabsorber (40) führt man Kalkmilch zu und hält die Auslaßtemperatur auf 160°C. Der Adsorber (46) enthält ein Zeolith-Festbett zur Hg-Entfernung.Residual municipal waste is fed to a process according to FIG. 2. The following data are partially calculated. The residual waste, which is delivered in an amount of 7500 kg / h, contains 24.5% by weight moisture and 30% by weight ash. This waste is first dried to 5% by weight of residual moisture and then gasified in the reactor (2) at 900 ° C. and with the supply of 6230 Nm 3 / h of air. 13,000 Nm 3 of gas flow through line (-10) per hour, the gas contains 48 g / Nm 3 of dust and 1% by volume of C 6+ hydrocarbons. The residence time of the gas in the gap chamber (12) is 1.5 seconds, air is supplied through line (13) and an outlet temperature of 1000 ° C. is reached. The content of C 6+ hydrocarbons in line (15) is only 0.1% by volume. 400 kg / h of dust are fed through the line (20) into the combustion chamber (21), which is fed with 1860 Nm 3 / h of air and in which 1300 ° C. can be reached. Lime milk is added to the spray absorber (40) and the outlet temperature is kept at 160 ° C. The adsorber (46) contains a zeolite fixed bed for mercury removal.

    Claims (2)

    1. A process of gasifying solid fuels in the circulating fluidized bed, wherein the fuels are gasified in a gasification reactor (2) by supplying oxygen-containing gas at temperatures in the range from 700 to 1000°C, from the upper portion of the gasification reactor a gas-solids mixture is supplied to a separator (9), gas containing dust and hydrocarbons including higher hydrocarbons with more than 6 C atoms in the molecule, which gas has a calorific value of 2000 to 8000 kJ/m3, and separated solids are separately discharged from the separator, and the solids are at least partly recirculated into the lower portion of the gasification reactor, characterized in that the dust-laden gas from the separator (9) is passed through a separation chamber (12), the hydrocarbons contained in the gas being largely broken down in the separation chamber by supplying gaseous oxygen at a temperature in the range from 800 to 1200°C and below the temperature of the ash melting point, whereby the content of higher hydrocarbons (C6+ hydrocarbons) in the gas is reduced to not more than 10 wt-% of the content of these higher hydrocarbons in the gas coming from the separator, that the gas coming from the separation chamber is cooled, the cooled gas is passed through a dedusting means (18) and entrained dust is separated, that the cooled and dedusted gas is passed through at least one bed or one reactor (40) with granular solids binding noxious substances and the gas is then dedusted, and that at least part of the entrained dust withdrawn from the dedusting means (18) is reacted in a combustion chamber (21) at temperatures in the range from 1000 to 1500°C by adding O2-containing gas.
    2. The process as claimed in claim 1, characterized in that the gaseous products formed in the combustion chamber (21) are admixed to the solids-containing gas formed in the gasification reactor (2).
    EP97952838A 1996-12-18 1997-12-01 Method of gasifying solid fuels in a circulating fluidized bed Expired - Lifetime EP0948583B1 (en)

    Applications Claiming Priority (3)

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    DE19652770A DE19652770A1 (en) 1996-12-18 1996-12-18 Process for gasifying solid fuels in the circulating fluidized bed
    DE19652770 1996-12-18
    PCT/EP1997/006716 WO1998027182A1 (en) 1996-12-18 1997-12-01 Method of gasifying solid fuels in a circulating fluidized bed

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    EP0948583B1 true EP0948583B1 (en) 2001-01-24

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    NZ573217A (en) 2006-05-05 2011-11-25 Plascoenergy Ip Holdings S L Bilbao Schaffhausen Branch A facility for conversion of carbonaceous feedstock into a reformulated syngas containing CO and H2
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    EP0948583A1 (en) 1999-10-13
    DE59702967D1 (en) 2001-03-01
    JP2001506288A (en) 2001-05-15
    WO1998027182A1 (en) 1998-06-25
    AU5657598A (en) 1998-07-15
    DE19652770A1 (en) 1998-06-25
    AU722068B2 (en) 2000-07-20
    ES2155270T3 (en) 2001-05-01
    BR9714421A (en) 2000-05-02

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