EP0776961B1 - Process for the treatment of the exhaust gas form the gasification of carbonaceous material - Google Patents
Process for the treatment of the exhaust gas form the gasification of carbonaceous material Download PDFInfo
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- EP0776961B1 EP0776961B1 EP96116298A EP96116298A EP0776961B1 EP 0776961 B1 EP0776961 B1 EP 0776961B1 EP 96116298 A EP96116298 A EP 96116298A EP 96116298 A EP96116298 A EP 96116298A EP 0776961 B1 EP0776961 B1 EP 0776961B1
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- gas
- exhaust gas
- solids
- temperatures
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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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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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
- C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
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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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
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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
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
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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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
- C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas
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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
- 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 method for treating exhaust gas the gasification of carbonaceous material, the Gasification with the addition of gas containing free oxygen at temperatures in the range of 700 to 1100 ° C and thereby a solid-containing exhaust gas is formed, which one by conducts at least one cyclone for separating solids.
- waste materials in particular are gasified and dust-containing fuel gas is fed through a cracking reactor with substoichiometric O 2 supply at temperatures of 1200 to 1600 ° C or even at even higher temperatures.
- the aim of the known methods is to convert the hydrocarbons contained in the fuel gas and the carbon-containing dusts as completely as possible into carbon oxides and hydrogen in the cracking reactor and, at the same time, to melt the ash that is carried in dust form with the fuel gas.
- the burned-out dust is difficult to burn out because the gaseous oxygen reacts preferentially with the gas components of the fuel gas.
- the invention has for its object to carry out the treatment of the exhaust gas as inexpensively as possible, without having to bring the entire exhaust gas to the highest temperatures and thus to increase the process efficiency.
- the object is achieved in the method mentioned at the outset by passing solid-containing exhaust gas at temperatures in the range from 700 to 1100 ° C.
- a flue gas or fuel gas and slag generates the flue gas or fuel gas together with the part of the exhaust gas coming from the gas discharge line of the separating cyclone into a mixing chamber through which the gas mixture is passed at temperatures of 900 to 1200 ° C. and with a residence time of at least 0.5 sec. and that it came from the mix withdrawn gas mixture cools.
- stoichiometric O 2 supply produces a fuel gas in the oxidation chamber and superstoichiometric O 2 supply a flue gas.
- the oxidation chamber is given separated solids together with a partial flow of Exhaust gas on. This ensures that the oxidation chamber can be made relatively small. Furthermore, on this Way compared to the known methods, an energy saving achieved, since only the partial flow of the exhaust gas on the brings the highest temperatures in the oxidation chamber to rule.
- the partial flow of the Exhaust gas accelerated by swirling the solids for ongoing reactions and the conversion of the solids into liquid slag.
- the carbon-containing material subjected to gasification can be, for example, waste materials, biomass, sludge, coal, brown coal or other substances which are usually gasified.
- the temperatures of the gasification range from 700 to 1100 ° C and mostly at least 800 ° C.
- Solid-containing exhaust gas from the gasification is passed through at least one cyclone, which is referred to here as a separating cyclone.
- the oxidation chamber is connected to this separating cyclone. It is possible but not absolutely necessary for one or more further cyclones to be interposed between the gasification and the separating cyclone.
- the calorific value of the exhaust gas fed to the separating cyclone is usually in the range from 3000 to 10000 kJ / Nm 3 .
- the removal takes place undesirable ingredients in two ways, namely once in the oxidation chamber at temperatures in the range of 1300 to 1800 ° C and usually 1500 to 1600 ° C, as well as in the Mixing chamber at temperatures from 900 to 1200 ° C and usually at least 1000 ° C. They are in the mixing chamber Residence times of the gas mixture, the remaining dust contains, at least 0.5 sec and mostly 1 to 5 sec temperatures and dwell times prevailing in the mixing chamber disruptive components are split in the gas mixture. Thereby you can withdraw a gas mixture from the mixing chamber, the largely free of hydrocarbons, dioxins and furans is.
- the oxidation chamber can be operated reducing or oxidizing.
- the O 2 content in the gas which is withdrawn from the oxidation chamber and passed into the mixing chamber is usually kept low and is approximately 1% by volume.
- the oxygen content of the flue gas coming from the oxidation chamber is then completely converted in the mixing chamber when it is mixed with the remaining exhaust gas. If you want to intensify oxidation reactions in the mixing chamber, it makes sense to add additional free oxygen.
- the channel of the separating cyclone coming solids together with the partial flow of the exhaust gas by pushing a propellant into the oxidation chamber.
- the propellant gas can e.g. around Air, oxygen-enriched air or also technically act pure oxygen, including the addition of water vapor is possible.
- Another option is to get one Partial stream of the gas mixture withdrawn from the mixing chamber as To use propellant.
- the propellant gas can e.g. together with one Ejectors are used in which the separator cyclone coming channel flows.
- a gasification reactor (1) is fed through line (2) gasifying, carbonaceous material supplied.
- Oxygen-containing gas e.g. Air or with oxygen Enriched air is fed through line (3) and serves at the same time as a fluidizing gas.
- the gasification in the circulating fluidized bed being a Gas-solid mixture through the channel (4) constantly to one Return cyclone (5) is guided. Separated solids go back through line (6) into the lower area of the Reactor (1), part of the solids is discharged through line (7) deducted.
- the special is for the method according to the invention
- Design of the gasification is not essential.
- the gasification can e.g. in the circulating fluidized bed, in the stationary Fluidized bed, using a rotary tube or a Moving rust or in some other way take place at the dust-containing exhaust gas is generated.
- the superstoichiometric, stoichiometric or substoichiometric oxidation in the chamber (15) takes place under Supply of air, air enriched with oxygen or else technically pure oxygen, which is used as a propellant or through line (16).
- the propellant gas of the line (13) is brought up by the fan (17).
- that is Using an ejector is not absolutely necessary and you can e.g. by adjusting the pressure loss in the line (22) do without it.
- Liquid Slag is removed from the chamber (15) through the line (18) removed and passed into a water bath, not shown.
- the Oxidation chamber (15) can also be passed through line (19) ashes, dusts and / or Add additives to support slag formation.
- Carbon content of the supplied solids practically completely implemented, are also brought up with the exhaust gas Split hydrocarbons.
- a hot flue gas or fuel gas is directed into a mixing chamber (21) and leads the mixing chamber through the Line (22) also from the upper area of the Separation cyclones (10) exhaust gas drawn off.
- the gases from the Lines (20) and (22) are mixed in the mixing chamber (21), where for temperatures in the range of 900 to 1200 ° C and preferably at least 1000 ° C.
- the Residence time of the gas mixture in the mixing chamber (21) set at least 0.5 sec and usually 1 to 4 sec. This ensures that residual hydrocarbons as well especially dioxins and furans in the gas mixture destroyed become.
- the gas mixture withdrawn from the mixing chamber (21) passes through the line (24) to a waste heat boiler (25) and from there to one only schematically shown dedusting (26). Secluded Dust can be removed through the line (27) of the oxidation chamber (15) give up. Cooled and dedusted gas is drawn in the line (28) and it can be a known, not shown Add gas cleaning.
- One way how to mix the gas the line (24) can cool and dedust is detailed in DE-A-4412004.
- the temperature in the chamber (15) is 1600 ° C, 1980 Nm3 / h flue gas and 2550 kg / h slag are withdrawn.
- the gas mixture in the mixing chamber (21) in an amount of 6940 Nm 3 / h has a mixing temperature of 1,100 ° C and a residence time of 2 seconds.
- the gas flowing out in the line (24) is largely free of hydrocarbons, dioxins and furans.
Description
Die Erfindung betrifft ein Verfahren zum Behandeln von Abgas aus der Vergasung von kohlenstoffhaltigem Material, wobei die Vergasung unter Zugabe von freien Sauerstoff enthaltendem Gas bei Temperaturen im Bereich von 700 bis 1100°C erfolgt und dabei ein feststoffhaltiges Abgas gebildet wird, das man durch mindestens einen Zyklon zum Abscheiden von Feststoffen leitet.The invention relates to a method for treating exhaust gas the gasification of carbonaceous material, the Gasification with the addition of gas containing free oxygen at temperatures in the range of 700 to 1100 ° C and thereby a solid-containing exhaust gas is formed, which one by conducts at least one cyclone for separating solids.
Verfahren dieser Art sind in DE-A-4235412 und DE-A-4412004 beschrieben. Hierbei werden insbesondere Abfallstoffe vergast und staubhaltiges Brenngas bei unterstöchiometrischer O2-Zufuhr bei Temperaturen von 1200 bis 1600°C oder auch bei noch höheren Temperaturen durch einen Spaltreaktor geleitet. Das Ziel der bekannten Verfahren liegt darin, im Spaltreaktor die im Brenngas enthaltenen Kohlenwasserstoffe und die kohlenstoffhaltigen Stäube möglichst vollständig in Kohlenoxide und Wasserstoff umzusetzen und gleichzeitig die mit dem Brenngas staubförmig mitgeführte Asche einzuschmelzen. Hierbei ist es aber erforderlich, das gesamte Brenngas auf hohe Temperaturen zu bringen. Gleichzeitig gelingt der Ausbrand des mitgeführten Staubes nur schlecht, weil der gasförmige Sauerstoff bevorzugt mit den Gaskomponenten des Brenngases reagiert. Um diesem Problem bei den bekannten Verfahren zu begegnen, muß man mit einem Spaltreaktor von relativ großem Volumen arbeiten.Methods of this type are described in DE-A-4235412 and DE-A-4412004. In this case, waste materials in particular are gasified and dust-containing fuel gas is fed through a cracking reactor with substoichiometric O 2 supply at temperatures of 1200 to 1600 ° C or even at even higher temperatures. The aim of the known methods is to convert the hydrocarbons contained in the fuel gas and the carbon-containing dusts as completely as possible into carbon oxides and hydrogen in the cracking reactor and, at the same time, to melt the ash that is carried in dust form with the fuel gas. However, it is necessary to bring the entire fuel gas to high temperatures. At the same time, the burned-out dust is difficult to burn out because the gaseous oxygen reacts preferentially with the gas components of the fuel gas. In order to counter this problem with the known methods, one has to work with a gap reactor of relatively large volume.
Der Erfindung liegt die Aufgabe zugrunde, die Behandlung des Abgases möglichst kostengünstig durchzuführen, dabei nicht das gesamte Abgas auf die höchsten Temperaturen bringen zu müssen und so den Prozeßwirkungsgrad zu erhöhen. Erfindungsgemäß wird die Aufgabe beim eingangs genannten Verfahren dadurch gelöst, daß man feststoffhaltiges Abgas mit Temperaturen im Bereich von 700 bis 1100°C in einen Abscheidezyklon leitet, der im oberen Bereich eine Gasabzugsleitung und im unteren Bereich einen Feststoffe abführenden Kanal aufweist, daß man durch den Kanal zusammen mit den abgeführten Feststoffen einen Partialstrom von 5 bis 30% des dem Abscheidezyklon zugeführten Abgases in eine Oxidationskammer leitet und in der Oxidationskammer bei unterstöchiometrischer bis überstöchiometrischer O2-Zufuhr und Temperaturen im Bereich von 1300 bis 1800°C ein Rauchgas oder Brenngas und Schlacke erzeugt, daß man das Rauchgas oder Brenngas zusammen mit dem aus der Gasabzugsleitung des Abscheidezyklons kommenden Teil des Abgases in eine Mischkammer leitet, durch welche das Gasgemisch mit Temperaturen von 900 bis 1200°C und mit einer Verweilzeit von mindestens 0,5 sec geführt wird, und daß man das aus der Mischkammer abgezogene Gasgemisch kühlt. Bei unterstöchiometrischem O2-Angebot entsteht in der Oxidationskammer ein Brenngas und bei überstöchiometrischem O2-Angebot ein Rauchgas.The invention has for its object to carry out the treatment of the exhaust gas as inexpensively as possible, without having to bring the entire exhaust gas to the highest temperatures and thus to increase the process efficiency. According to the invention, the object is achieved in the method mentioned at the outset by passing solid-containing exhaust gas at temperatures in the range from 700 to 1100 ° C. into a separating cyclone which has a gas discharge line in the upper region and a solids-discharging duct in the lower region, that through the Channel together with the removed solids conducts a partial flow of 5 to 30% of the exhaust gas fed to the separating cyclone into an oxidation chamber and in the oxidation chamber with substoichiometric to overstoichiometric O 2 supply and temperatures in the range from 1300 to 1800 ° C a flue gas or fuel gas and slag generates the flue gas or fuel gas together with the part of the exhaust gas coming from the gas discharge line of the separating cyclone into a mixing chamber through which the gas mixture is passed at temperatures of 900 to 1200 ° C. and with a residence time of at least 0.5 sec. and that it came from the mix withdrawn gas mixture cools. In stoichiometric O 2 supply produces a fuel gas in the oxidation chamber and superstoichiometric O 2 supply a flue gas.
Beim erfindungsgemäßen Verfahren gibt man der Oxidationskammer abgeschiedene Feststoffe zusammen mit einem Partialstrom des Abgases auf. Dadurch erreicht man, daß die Oxidationskammer relativ klein ausgeführt werden kann. Ferner wird auf diese Weise gegenüber den bekannten Verfahren eine Energieersparnis erzielt, da man nur den Partialstrom des Abgases auf die höchsten Temperaturen bringt, die in der Oxidationskammer herrschen. In der Oxidationskammer sorgt der Partialstrom des Abgases durch Verwirbelung der Feststoffe für beschleunigt ablaufende Reaktionen und die Umwandlung der Feststoffe in flüssige Schlacke.In the method according to the invention, the oxidation chamber is given separated solids together with a partial flow of Exhaust gas on. This ensures that the oxidation chamber can be made relatively small. Furthermore, on this Way compared to the known methods, an energy saving achieved, since only the partial flow of the exhaust gas on the brings the highest temperatures in the oxidation chamber to rule. The partial flow of the Exhaust gas accelerated by swirling the solids for ongoing reactions and the conversion of the solids into liquid slag.
Bei dem der Vergasung unterworfenen kohlenstoffhaltigen Material kann es sich z.B. um Abfallstoffe, Biomassen, Schlämme, Kohle, Braunkohle oder andere Stoffe handeln, die üblicherweise vergast werden. Die Temperaturen der Vergasung liegen im Bereich von 700 bis 1100°C und zumeist bei mindestens 800°C. Feststoffhaltiges Abgas aus der Vergasung wird durch mindestens einen Zyklon, der hier als Abscheidezyklon bezeichnet ist, geleitet. An diesen Abscheidezyklon ist die Oxidationskammer angeschlossen. Es ist möglich aber nicht unbedingt erforderlich, daß zwischen der Vergasung und dem Abscheidezyklon ein oder mehrere weitere Zyklone zwischengeschaltet sind. Der Heizwert des dem Abscheidezyklon zugeführten Abgases liegt üblicherweise im Bereich von 3000 bis 10000 kJ/Nm3.The carbon-containing material subjected to gasification can be, for example, waste materials, biomass, sludge, coal, brown coal or other substances which are usually gasified. The temperatures of the gasification range from 700 to 1100 ° C and mostly at least 800 ° C. Solid-containing exhaust gas from the gasification is passed through at least one cyclone, which is referred to here as a separating cyclone. The oxidation chamber is connected to this separating cyclone. It is possible but not absolutely necessary for one or more further cyclones to be interposed between the gasification and the separating cyclone. The calorific value of the exhaust gas fed to the separating cyclone is usually in the range from 3000 to 10000 kJ / Nm 3 .
Beim erfindungsgemäßen Verfahren erfolgt die Beseitigung unerwünschter Inhaltsstoffe in zweifacher Weise, nämlich einmal in der Oxidationskammer bei Temperaturen im Bereich von 1300 bis 1800°C und üblicherweise 1500 bis 1600°C, sowie in der Mischkammer bei Temperaturen von 900 bis 1200°C und üblicherweise mindestens 1000°C. In der Mischkammer liegen die Verweilzeiten des Gasgemisches, das noch restlichen Staub enthält, bei mindestens 0,5 sec und zumeist 1 bis 5 sec. Bei den in der Mischkammer herrschenden Temperaturen und Verweilzeiten werden störende Bestandteile im Gasgemisch gespalten. Dadurch kann man aus der Mischkammer ein Gasgemisch abziehen, das weitestgehend frei von Kohlenwasserstoffen, Dioxinen und Furanen ist.In the method according to the invention, the removal takes place undesirable ingredients in two ways, namely once in the oxidation chamber at temperatures in the range of 1300 to 1800 ° C and usually 1500 to 1600 ° C, as well as in the Mixing chamber at temperatures from 900 to 1200 ° C and usually at least 1000 ° C. They are in the mixing chamber Residence times of the gas mixture, the remaining dust contains, at least 0.5 sec and mostly 1 to 5 sec temperatures and dwell times prevailing in the mixing chamber disruptive components are split in the gas mixture. Thereby you can withdraw a gas mixture from the mixing chamber, the largely free of hydrocarbons, dioxins and furans is.
Die Oxidationskammer kann man reduzierend oder oxidierend betreiben. Bei oxidierender Fahrweise wird üblicherweise der O2-Gehalt im Gas, das man aus der Oxidationskammer abzieht und in die Mischkammer leitet, niedrig gehalten und liegt bei etwa 1 Vol.-%. In der Mischkammer wird dann der Sauerstoffgehalt des aus der Oxidationskammer kommenden Rauchgases beim Vermischen mit dem restlichen Abgas vollständig umgesetzt. Wenn man Oxidationsreaktionen in der Mischkammer verstärkten will, bietet es sich an, zusätzlichen freien Sauerstoff zuzuführen.The oxidation chamber can be operated reducing or oxidizing. In an oxidizing mode of operation, the O 2 content in the gas which is withdrawn from the oxidation chamber and passed into the mixing chamber is usually kept low and is approximately 1% by volume. The oxygen content of the flue gas coming from the oxidation chamber is then completely converted in the mixing chamber when it is mixed with the remaining exhaust gas. If you want to intensify oxidation reactions in the mixing chamber, it makes sense to add additional free oxygen.
Es kann zweckmäßig sein, die vom Kanal des Abscheidezyklons kommenden Feststoffe zusammen mit dem Partialstrom des Abgases durch ein Treibgas in die Oxidationskammer zu drücken. Hierdurch wird eine gute Verwirbelung der Feststoffe in der Oxidationskammer erreicht. Bei dem Treibgas kann es sich z.B. um Luft, mit Sauerstoff angereicherte Luft oder auch um technisch reinen Sauerstoff handeln, wobei auch der Zusatz von Wasserdampf möglich ist. Eine weitere Möglichkeit besteht darin, einen Teilstrom des aus der Mischkammer abgezogenen Gasgemisches als Treibgas zu verwenden. Das Treibgas kann z.B. zusammen mit einem Ejektor angewandt werden, in welchen der vom Abscheidezyklon kommende Kanal mündet.It may be appropriate that the channel of the separating cyclone coming solids together with the partial flow of the exhaust gas by pushing a propellant into the oxidation chamber. Hereby there will be a good swirling of the solids in the Oxidation chamber reached. The propellant gas can e.g. around Air, oxygen-enriched air or also technically act pure oxygen, including the addition of water vapor is possible. Another option is to get one Partial stream of the gas mixture withdrawn from the mixing chamber as To use propellant. The propellant gas can e.g. together with one Ejectors are used in which the separator cyclone coming channel flows.
Ausgestaltungsmöglichkeiten des Verfahrens werden mit Hilfe der Zeichnung erläutert. Die Zeichnung zeigt ein Fließschema des Verfahrens.Design options of the process are with the help of Drawing explained. The drawing shows a flow diagram of the Procedure.
Einem Vergasungsreaktor (1) wird durch die Leitung (2) zu vergasendes, kohlenstoffhaltiges Material zugeführt. Sauerstoffhaltiges Gas, z.B. Luft oder mit Sauerstoff angereicherte Luft wird durch Leitung (3) herangeführt und dient gleichzeitig auch als Fluidisierungsgas. Im Reaktor (1) erfolgt die Vergasung in der zirkulierenden Wirbelschicht, wobei ein Gas-Feststoff-Gemisch durch den Kanal (4) ständig zu einem Rückführ-Zyklon (5) geführt wird. Abgeschiedene Feststoffe gelangen durch die Leitung (6) zurück in den unteren Bereich des Reaktors (1), ein Teil der Feststoffe wird durch die Leitung (7) abgezogen.A gasification reactor (1) is fed through line (2) gasifying, carbonaceous material supplied. Oxygen-containing gas, e.g. Air or with oxygen Enriched air is fed through line (3) and serves at the same time as a fluidizing gas. In the reactor (1) the gasification in the circulating fluidized bed, being a Gas-solid mixture through the channel (4) constantly to one Return cyclone (5) is guided. Separated solids go back through line (6) into the lower area of the Reactor (1), part of the solids is discharged through line (7) deducted.
Für das erfindungsgemäße Verfahren ist die spezielle Ausgestaltung der Vergasung nicht wesentlich. Die Vergasung kann z.B. in der zirkulierenden Wirbelschicht, in der stationären Wirbelschicht, unter Verwendung eines Drehrohrs oder eines Wanderrostes oder in anderer Weise erfolgen, bei der ein staubhaltiges Abgas entsteht.The special is for the method according to the invention Design of the gasification is not essential. The gasification can e.g. in the circulating fluidized bed, in the stationary Fluidized bed, using a rotary tube or a Moving rust or in some other way take place at the dust-containing exhaust gas is generated.
Aus dem Rückführ-Zyklon (5) zieht man durch die Leitung (9) feststoffhaltiges Abgas mit einer Temperatur im Bereich von 700 bis 1100°C ab. Dieses Abgas leitet man in den Abscheidezyklon (10), der speziell ausgestaltet ist. Der untere Bereich des Zyklons (10) geht in einen relativ weiten Kanal (11) über, der üblicherweise einen Innendurchmesser im Bereich von 100 bis 500 mm aufweist. Dadurch gelangen nicht nur die im Zyklon abgeschiedenen Feststoffe sondern auch ein Partialstrom des Abgases von 5 bis 30% des Abgases der Leitung (9) in den Kanal (11). Die Feststoffe und der Abgas-Partialstrom werden durch den Ejektor (12) angesaugt und mit Hilfe des Treibgases aus der Leitung (13) in die Oxidationskammer (15) gedrückt. Die überstöchiometrische, stöchiometrische oder unterstöchiometrische Oxidation in der Kammer (15) erfolgt unter Zufuhr von Luft, mit Sauerstoff angereicherter Luft oder auch technisch reinem Sauerstoff, die man als Treibgas verwendet oder durch die Leitung (16) zuführt. Das Treibgas der Leitung (13) wird durch das Gebläse (17) herangeführt. Für die Praxis ist die Verwendung eines Ejektors nicht unbedingt nötig und man kann z.B. durch Einstellen des Druckverlustes in der Leitung (22) darauf verzichten.From the return cyclone (5), pull through line (9) solid exhaust gas with a temperature in the range of 700 up to 1100 ° C. This exhaust gas is led into the separating cyclone (10), which is specially designed. The lower area of the Cyclones (10) merges into a relatively wide channel (11) usually an inner diameter in the range of 100 to 500 mm. This not only gets them into the cyclone separated solids but also a partial flow of Exhaust gas from 5 to 30% of the exhaust gas of line (9) into the duct (11). The solids and the exhaust gas partial flow are through the Ejector (12) sucked in and with the help of the propellant gas from the Line (13) pressed into the oxidation chamber (15). The superstoichiometric, stoichiometric or substoichiometric oxidation in the chamber (15) takes place under Supply of air, air enriched with oxygen or else technically pure oxygen, which is used as a propellant or through line (16). The propellant gas of the line (13) is brought up by the fan (17). In practice, that is Using an ejector is not absolutely necessary and you can e.g. by adjusting the pressure loss in the line (22) do without it.
In der Oxidationskammer (15) herrschen Temperaturen im Bereich von 1300 bis 1800°C und vorzugsweise 1500 bis 1600°C. Flüssige Schlacke wird aus der Kammer (15) durch die Leitung (18) abgezogen und in ein nicht dargestelltes Wasserbad geleitet. Der Oxidationskammer (15) kann man zusätzlich durch die Leitung (19) im Verfahren anfallende Asche, Stäube und/oder die Schlackebildung unterstützende Additive zuführen. Bei den in der Kammer (15) herrschenden hohen Temperaturen wird der Kohlenstoff-Gehalt der zugeführten Feststoffe praktisch restlos umgesetzt, auch werden mit dem Abgas herangeführte Kohlenwasserstoffe gespalten. Temperatures in the area prevail in the oxidation chamber (15) from 1300 to 1800 ° C and preferably 1500 to 1600 ° C. Liquid Slag is removed from the chamber (15) through the line (18) removed and passed into a water bath, not shown. The Oxidation chamber (15) can also be passed through line (19) ashes, dusts and / or Add additives to support slag formation. In the in the Chamber (15) prevailing high temperatures Carbon content of the supplied solids practically completely implemented, are also brought up with the exhaust gas Split hydrocarbons.
Aus der Oxidationskammer (15) zieht man durch die Leitung (20) ein heißes Rauchgas oder Brenngas ab. Dieses Gas leitet man in eine Mischkammer (21) und führt der Mischkammer durch die Leitung (22) auch das aus dem oberen Bereich des Abscheidezyklons (10) abgezogene Abgas zu. Die Gase aus den Leitungen (20) und (22) werden in der Mischkammer (21) gemischt, wobei man für Temperaturen im Bereich von 900 bis 1200°C und vorzugsweise mindestens 1000°C sorgt. Gleichzeitig wird die Verweilzeit des Gasgemisches in der Mischkammer (21) auf mindestens 0,5 sec und üblicherweise 1 bis 4 sec eingestellt. Dadurch erreicht man, daß restliche Kohlenwasserstoffe sowie insbesondere auch Dioxine und Furane im Gasgemisch zerstört werden. Um die Oxidationsreaktionen in der Mischkammer (21) noch zu fördern, kann es zweckmäßig sein, Luft, mit Sauerstoff angereicherte Luft oder technisch reinen Sauerstoff zusätzlich durch die Leitung (23) heranzuführen, doch wird dies zumeist nicht erforderlich sein.From the oxidation chamber (15), one pulls through the line (20) a hot flue gas or fuel gas. This gas is directed into a mixing chamber (21) and leads the mixing chamber through the Line (22) also from the upper area of the Separation cyclones (10) exhaust gas drawn off. The gases from the Lines (20) and (22) are mixed in the mixing chamber (21), where for temperatures in the range of 900 to 1200 ° C and preferably at least 1000 ° C. At the same time, the Residence time of the gas mixture in the mixing chamber (21) set at least 0.5 sec and usually 1 to 4 sec. This ensures that residual hydrocarbons as well especially dioxins and furans in the gas mixture destroyed become. To the oxidation reactions in the mixing chamber (21) still to promote, it may be expedient to air, with oxygen enriched air or technically pure oxygen to lead through the line (23), but this is usually not be necessary.
Das aus der Mischkammer (21) abgezogene Gasgemisch gelangt durch die Leitung (24) zu einem Abhitzekessel (25) und von da zu einer nur schematisch dargestellten Entstaubung (26). Abgeschiedenen Staub kann man durch die Leitung (27) der Oxidationskammer (15) aufgeben. Gekühltes und entstaubtes Gas zieht man in der Leitung (28) ab und kann es einer an sich bekannten, nicht dargestellten Gasreinigung zuführen. Eine Möglichkeit, wie man das Gasgemisch der Leitung (24) kühlen und entstauben kann, ist detailliert in DE-A-4412004 beschrieben.The gas mixture withdrawn from the mixing chamber (21) passes through the line (24) to a waste heat boiler (25) and from there to one only schematically shown dedusting (26). Secluded Dust can be removed through the line (27) of the oxidation chamber (15) give up. Cooled and dedusted gas is drawn in the line (28) and it can be a known, not shown Add gas cleaning. One way how to mix the gas the line (24) can cool and dedust is detailed in DE-A-4412004.
Es wird in einer der Zeichnung entsprechenden Anlage ohne die
Leitungen (19) und (23) gearbeitet, wobei man dem
Vergasungsreaktor (1) pro Stunde 5880 kg kommunalen Müll
zuführt, den man bei 900°C mit O2 angereicherter Luft (O2-Gehalt
30 Vol.%) zu einer Menge von 1906 Nm3/h Schwachgas vergast. Die
nachfolgenden Daten sind teilweise berechnet:
Feststoff-Umlauf durch Leitung (6): 200 t/h;
Feststoff-Abzug durch Leitung (7) : 4 t/h;
das Abgas in der Leitung (9) in einer Menge von 6160 Nm3/h
enthält pro Nm3 100 g staubförmige Feststoffe; durch den Ejektor
(12) gelangen pro Stunde 1200 Nm3 Abgas und 800 kg Feststoffe in
die Oxidationskammer (15), welcher man 915 Nm3/h O2 zuführt. Die
Temperatur in der Kammer (15) liegt bei 1600°C, es werden 1980
Nm3/h Rauchgas und 2550 kg/h Schlacke abgezogen. Das Gasgemisch
in der Mischkammer (21) in einer Menge von 6940 Nm3/h hat eine
Mischtemperatur von 1.100°C und eine Verweilzeit von 2 sec. Das
in der Leitung (24) abströmende Gas ist weitestgehend frei von
Kohlenwasserstoffen, Dioxinen und Furanen.Work is carried out in a system corresponding to the drawing without lines (19) and (23), 5880 kg of municipal waste being fed to the gasification reactor (1) per hour, which waste is enriched with O 2 -enriched air (O 2 - Content 30 vol.%) To a quantity of 1906 Nm 3 / h of weak gas. The following data are partially calculated:
Solids circulation through line (6): 200 t / h;
Solids withdrawal through line (7): 4 t / h;
the exhaust gas in line (9) in an amount of 6160 Nm 3 / h contains 100 g of dust-like solids per Nm 3 ; 1200 Nm 3 of exhaust gas and 800 kg of solids pass through the ejector (12) into the oxidation chamber (15), to which 915 Nm 3 / h of O 2 are fed. The temperature in the chamber (15) is 1600 ° C, 1980 Nm3 / h flue gas and 2550 kg / h slag are withdrawn. The gas mixture in the mixing chamber (21) in an amount of 6940 Nm 3 / h has a mixing temperature of 1,100 ° C and a residence time of 2 seconds. The gas flowing out in the line (24) is largely free of hydrocarbons, dioxins and furans.
Claims (4)
- A process for treating exhaust gas from the gasification of carbon-containing material, in which the gasification takes place with the addition of gas containing free oxygen at temperatures in the range of 700 to 1100°C and in the process a solids-containing exhaust gas is formed which is passed through at least one cyclone for separating off solids, characterised in that solids-containing exhaust gas at temperatures in the range of 700 to 1100°C is passed into a cyclone separator, which has in its upper region a gas extraction pipe and in its lower region a channel which carries away solids, that a partial stream of 5 to 30% of the exhaust gas supplied to the cyclone separator is passed through the channel, together with the solids which are carried away, into an oxidation chamber and a flue gas or combustion gas and slag is produced in the oxidation chamber with a hypostoichiometric to hyperstoichiometric supply of O2 and temperatures in the range of 1300 to 1800°C, that the flue gas or combustion gas together with the portion of the exhaust gas coming from the gas extraction pipe of the cyclone separator is passed into a mixing chamber, through which the gas mixture is passed at temperatures of 900 to 1200°C and with a dwell time of at least 0.5 seconds, and that the gas mixture withdrawn from the mixing chamber is cooled.
- A process according to Claim 1, characterised in that the solids coming from the channel of the cyclone separator, together with the partial stream of the exhaust gas, are pushed into the oxidation chamber by a propellant gas.
- A process according to Claim 1 or 2, characterised in that the mixing chamber is supplied with gas containing free oxygen.
- A process according to Claim 1 or one of the following claims, characterised in that additives are fed to the oxidation chamber.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19544200A DE19544200A1 (en) | 1995-11-28 | 1995-11-28 | Process for treating exhaust gas from the gasification of carbonaceous material |
| DE19544200 | 1995-11-28 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0776961A1 EP0776961A1 (en) | 1997-06-04 |
| EP0776961B1 true EP0776961B1 (en) | 2001-02-28 |
Family
ID=7778544
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP96116298A Expired - Lifetime EP0776961B1 (en) | 1995-11-28 | 1996-10-11 | Process for the treatment of the exhaust gas form the gasification of carbonaceous material |
Country Status (2)
| Country | Link |
|---|---|
| EP (1) | EP0776961B1 (en) |
| DE (2) | DE19544200A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19754802B4 (en) * | 1997-12-10 | 2008-04-03 | Sasol-Lurgi Technology Company (Pty) Ltd | Process for the thermal treatment of a gas mixture coming from the gasification of carbonaceous materials |
| DE10021448A1 (en) * | 2000-05-03 | 2001-11-08 | Messer Griesheim Gmbh | Method for burning organic waste involves passing fluidizising gas through waste in combustion chamber to produce fluidized particle layer whereby in free space above same the mean oxygen content is 0-3 percent by volume |
| US8317510B2 (en) * | 2006-07-13 | 2012-11-27 | The Regents Of The University Of Michigan | Method of waste heat recovery from high temperature furnace exhaust gases |
| CN105647587A (en) * | 2016-03-04 | 2016-06-08 | 广东工业大学 | High-temperature sawdust gasification furnace |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2836175A1 (en) * | 1978-08-18 | 1980-02-28 | Metallgesellschaft Ag | METHOD FOR GASIFYING SOLID, FINE-GRAIN FUELS |
| EP0227196B1 (en) * | 1985-12-27 | 1990-08-08 | Shell Internationale Researchmaatschappij B.V. | Oxidation of flyash |
| DE4235412A1 (en) * | 1992-10-21 | 1994-04-28 | Metallgesellschaft Ag | Process for gasifying waste materials containing combustible components |
| DE4412004A1 (en) * | 1994-04-07 | 1995-10-12 | Metallgesellschaft Ag | Process for gasifying waste materials in the circulating fluidized bed |
-
1995
- 1995-11-28 DE DE19544200A patent/DE19544200A1/en not_active Withdrawn
-
1996
- 1996-10-11 EP EP96116298A patent/EP0776961B1/en not_active Expired - Lifetime
- 1996-10-11 DE DE59606497T patent/DE59606497D1/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| EP0776961A1 (en) | 1997-06-04 |
| DE59606497D1 (en) | 2001-04-05 |
| DE19544200A1 (en) | 1997-06-05 |
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