EP0220342A1 - Process for treating an aqueous condensate - Google Patents

Process for treating an aqueous condensate Download PDF

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Publication number
EP0220342A1
EP0220342A1 EP85201775A EP85201775A EP0220342A1 EP 0220342 A1 EP0220342 A1 EP 0220342A1 EP 85201775 A EP85201775 A EP 85201775A EP 85201775 A EP85201775 A EP 85201775A EP 0220342 A1 EP0220342 A1 EP 0220342A1
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Prior art keywords
combustion
fluidized bed
gasification
condensate
gas
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German (de)
French (fr)
Inventor
Jakob Ergezinger
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GEA Group AG
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Metallgesellschaft AG
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Priority to EP85201775A priority Critical patent/EP0220342A1/en
Priority to US06/925,881 priority patent/US4731099A/en
Priority to ES8602867A priority patent/ES2003449A6/en
Priority to ZA868318A priority patent/ZA868318B/en
Publication of EP0220342A1 publication Critical patent/EP0220342A1/en
Withdrawn legal-status Critical Current

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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
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • 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
    • C10J3/56—Apparatus; Plants
    • 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
    • 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
    • C10J3/78—High-pressure apparatus
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0969—Carbon dioxide
    • 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
    • C10J2300/0976—Water as steam
    • 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
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • 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
    • 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
    • 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
    • C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam

Definitions

  • the invention relates to a method for treating water-containing condensate from the cooling of the raw gas of the gasification of solid fuels with gasifying agents containing oxygen, water vapor and carbon dioxide under a pressure of 5 to 100 bar, the fuels forming a fixed bed which slowly moves down and under which the incombustible mineral components of the fuel are extracted as solid ash or liquid slag.
  • the relaxation steam becomes one Combustion chamber fed and burned at temperatures above 800 ° C. Part of the liquid phase must be removed from the process and worked up, because otherwise the concentration of the impurities in the gas or in the condensate would increase to impermissible values. However, the processing and cleaning of liquids causes considerable costs.
  • the invention has for its object to eliminate the portion of the condensate that can not be returned to the gasification or reused in the treatment of the raw gas in a simple and economical manner.
  • this is done according to the invention in that the condensate is at least partially burned in a fluidized bed combustion at temperatures in the range from about 750 to 1000 ° C. and the combustion gas containing water vapor is passed from the combustion into the gasification. There is no need to clean a condensate component and the combustion gas serves as a gasifying agent in the gasification.
  • a further development of the invention consists in that the condensate obtained during the cooling of the raw gas is at least partially freed of dust and tar in a separator before the condensate is fed to the fluidized bed combustion. Dust and tar are returned to the gasification in a known manner.
  • Part of the combustion gas is expediently returned to the fluidized bed combustion, the gas serving as the fluidization medium.
  • the process also offers the advantageous possibility of sulfur compounds and from the raw gas after cooling Remove carbon dioxide and give up these substances of fluidized bed combustion together with calcium compounds.
  • the CO2 is retained in the gasification process and reduces coal consumption.
  • the sulfur compounds, in particular H2S, are converted to SO2 in the fluidized bed combustion and combine with the calcium compounds, in particular limestone or milk of lime, to form calcium sulfate. Calcium sulfate is then drawn off with the combustion axis and can be deposited without any problems.
  • An advantageous embodiment of the method consists in operating the fluidized bed combustion at a pressure which is at least 2 bar higher than the pressure of the gasification. As a result, the combustion gas can be introduced into the gasification without additional compression.
  • the classic fluidized bed or, preferably, the circulating fluidized bed can be used, for which details are described in German specification 25 39 546 and the corresponding US Pat. No. 4,165,717.
  • the speeds of the fluidizing gas are considerably higher than in the classic fluidized bed, so that large amounts of solids are continuously discharged from the fluidized bed reactor, separated from the gas and fed back into the fluidized bed reactor.
  • the gasification 1 is fed granular coal with a grain area of about 3 to 60 mm through the line 2.
  • lock devices are not shown in the drawing.
  • Gasifying agents come from line 3, they consist of a combustion gas to which oxygen is added through line 4.
  • the incombustible residue of the gasification, which is solid ash or liquid slag, is discharged in line 5.
  • the raw gas of the gasification passes in line 6 to a washer cooler 7, in which water or condensate consisting predominantly of water is fed through line 8.
  • a washer cooler 7 in which water or condensate consisting predominantly of water is fed through line 8.
  • further cooling takes place, so that the raw gas in line 11 is drawn off at temperatures in the range from 120 to 180 ° C. and in the bottom of waste heat boiler 10 a condensate is also obtained at temperatures of from 120 to 180 ° C.
  • This condensate is fed to a separator 13 in line 12.
  • the pressure in the separator 13 is only about 1 to 5 bar lower than in the gasification 1.
  • the gravitational separation of various components of the condensate takes place in a manner known per se.
  • a heavy phase which is rich in dust and tar, is drawn off in line 14, it being advisable to also feed this phase to gasification 1.
  • a water-rich phase which is usually referred to as gas water, is drawn off in the line 15 and, under the action of the pump 16, is given up to a fluidized bed combustion 17. If necessary, make-up water is introduced in line 9.
  • the fluidized bed combustion 17 is also supplied with an exhaust gas from the line 18, which is sucked in by the fan 19 from a gas cleaning device 20.
  • the raw gas from the line 11 is treated, sulfur compounds, in particular H2S, and also partly CO2 being removed by known processes. CO2 and these sulfur compounds are contained in the exhaust gas of line 18.
  • the cleaned gas which now mainly consists of hydrogen and carbon monoxide, is available for further use in line 21.
  • the fluidized bed combustion 17 is supplied with fine coal with a grain size of up to 10 mm through line 22 and ground limestone, dolomite or milk of lime through line 23 as fuel. These calcium compounds are converted in the combustion 17 at the prevailing temperatures of 750 to 1000 ° C and preferably 800 to 900 ° C to CaO, which binds the SO2 formed from the sulfur compounds as calcium sulfate.
  • the combustion 17 uses a partial flow of the combustion gases which is returned in line 25 and to which oxygen, air or also oxygen-enriched air is mixed in line 26.
  • this gas is introduced through line 34 Water sprayed in, which can also be condensate or gas water.
  • the combustion gas enriched with water vapor is then partly returned to the combustion 17 via the blower 35 and the line 25 in the manner already described, the remaining combustion gas is fed to the gasification 1 in line 3.
  • the gasification is given 1 1000 kg of coal (free of water and ash).
  • the coal which has a grain size range of 5 to 40 mm, contains 51 kg moisture, 126 kg ash and 21 kg sulfur.
  • Combustion gas which consists of the following gas components, is brought in through line 3 as the gasifying agent: CO2 107 Nm3 O2 7 Nm3 N2 2 Nm3 and that contains 323 kg of water vapor.
  • the temperature of the gas is 400 ° C. 477 Nm3 of oxygen from line 4 are mixed into the combustion gas.
  • the pressure in gasification 1 is 30 bar and in combustion 17 is 32 bar.

Abstract

Feste Brennstoffe werden mit Sauerstoff, Wasserdampf und Kohlendioxid bei einem Druck von 5 bis 100 bar im Festbett vergast. Das Rohgas aus der Vergasung wird gekühlt, wobei ein wasserhaltiges Kondensat entsteht. Das Kondensat wird zumindest teilweise in einer Wirbelschichtverbrennung bei Temperaturen im Bereich von etwa 750 bis 1000°C verbrannt, das dabei entstehende wasserdampfhaltoge Verbrennungsgas wird in die Vergasung geleitet. Das beim Kühlen des Rohgases anfallende Kondensat kann in einem Abscheider zumindest teilweise von Staub und Teer befreit werden, bevor man das Kondensat der Wirbelbettverbrennung zuführt. Die Wirbelbettverbrennung arbeitet vorzugsweise als zirkulierende Wirbelschicht.Solid fuels are gasified with oxygen, water vapor and carbon dioxide at a pressure of 5 to 100 bar in a fixed bed. The raw gas from the gasification is cooled, creating a water-containing condensate. The condensate is at least partially burned in a fluidized bed combustion at temperatures in the range of about 750 to 1000 ° C, the resulting steam containing combustion gas is passed into the gasification. The condensate obtained when the raw gas is cooled can be at least partially freed of dust and tar in a separator before the condensate is fed to the fluidized bed combustion. The fluidized bed combustion preferably works as a circulating fluidized bed.

Description

Die Erfindung betrifft ein Verfahren zum Behandeln von wasserhaltigem Kondensat aus der Kühlung des Rohgases der Vergasung fester Brennstoffe mit Sauerstoff, Wasserdampf und Kohlendioxid enthaltenden Vergasungsmitteln unter ei­nem Druck von 5 bis 100 bar, wobei die Brennstoffe ein Festbett bilden, das sich langsam nach unten bewegt und unter dem man die unverbrennlichen mineralischen Bestand­teile des Brennstoffs als feste Asche oder flüssige Schlacke abzieht.The invention relates to a method for treating water-containing condensate from the cooling of the raw gas of the gasification of solid fuels with gasifying agents containing oxygen, water vapor and carbon dioxide under a pressure of 5 to 100 bar, the fuels forming a fixed bed which slowly moves down and under which the incombustible mineral components of the fuel are extracted as solid ash or liquid slag.

Die Vergasung fester Brennstoffe, insbesondere von Kohle oder Braunkohle, im Festbett mit festbleibender Asche ist z.B. in Ullmanns Enzyklopädie der Technischen Chemie, 4. Auflage (1977), Band 14, Seiten 383-386, dargestellt. Einzelheiten dieser bekannten Vergasungsmethode sind auch in den US-Patentschriften 3 540 867 und 3 854 895 veröf­fentlicht. Die Vergasung des Brennstoffs im Festbett mit Abzug flüssiger Schlacke ist in den britischen Patent­schriften 1 507 905, 1 506 671 und 1 512 677 erläutert. Beim Verfahren des europäischen Patents 12 456 und dem da­zu korrespondierenden US-Patent 4 295 864 wird das beim Kühlen des Rohgases unter erhöhtem Druck anfallende Kon­densat entspannt, wobei Entspannungsdampf und eine flüssi­ge Phase entstehen. Der Entspannungsdampf wird einer Brennkammer zugeführt und bei Temperaturen oberhalb von 800°C verbrannt. Ein Teil der flüssigen Phase muß aus dem Prozeß entfernt und aufgearbeitet werden, weil sich sonst die Konzentration der Verunreinigungen im Gas oder im Kon­densat auf unzulässige Werte steigern würde. Das Aufarbei­ten und Reinigen von Flüssigkeit verursacht jedoch be­trächtliche Kosten.The gasification of solid fuels, in particular coal or lignite, in a fixed bed with ashes remaining is shown, for example, in Ullmanns Enzyklopadie der Technischen Chemie, 4th edition (1977), volume 14, pages 383-386. Details of this known gasification method are also published in U.S. Patents 3,540,867 and 3,854,895. The gasification of the fuel in a fixed bed with the removal of liquid slag is explained in British Patents 1 507 905, 1 506 671 and 1 512 677. In the process of European patent 12 456 and the corresponding US patent 4,295,864, the condensate obtained when the crude gas is cooled under elevated pressure is expanded, with expansion vapor and a liquid phase being produced. The relaxation steam becomes one Combustion chamber fed and burned at temperatures above 800 ° C. Part of the liquid phase must be removed from the process and worked up, because otherwise the concentration of the impurities in the gas or in the condensate would increase to impermissible values. However, the processing and cleaning of liquids causes considerable costs.

Der Erfindung liegt die Aufgabe zugrunde, den Anteil des Kondensats, der nicht in die Vergasung zurückgeführt oder beim Behandeln des Rohgases wiederverwendet werden kann, auf einfache und wirtschaftliche Weise zu beseitigen. Beim eingangs genannten Verfahren geschieht dies erfindungsge­mäß dadurch, daß man das Kondensat zumindest teilweise in einer Wirbelschichtverbrennung bei Temperaturen im Bereich von etwa 750 bis 1000°C verbrennt und das wasserdampfhal­tige Verbrennungsgas aus der Verbrennung in die Vergasung leitet. Das Reinigen eines Kondensatanteils entfällt hier­bei völlig und das Verbrennungsgas dient in der Vergasung als Vergasungsmittel.The invention has for its object to eliminate the portion of the condensate that can not be returned to the gasification or reused in the treatment of the raw gas in a simple and economical manner. In the process mentioned at the outset, this is done according to the invention in that the condensate is at least partially burned in a fluidized bed combustion at temperatures in the range from about 750 to 1000 ° C. and the combustion gas containing water vapor is passed from the combustion into the gasification. There is no need to clean a condensate component and the combustion gas serves as a gasifying agent in the gasification.

Eine Weiterbildung der Erfindung besteht darin, daß man das beim Kühlen des Rohgases anfallende Kondensat in einem Abscheider von Staub und Teer zumindest teilweise befreit, bevor man das Kondensat der Wirbelbettverbrennung zuführt. Staub und Teer werden in bekannter Weise in der Vergasung zurückgeführt.A further development of the invention consists in that the condensate obtained during the cooling of the raw gas is at least partially freed of dust and tar in a separator before the condensate is fed to the fluidized bed combustion. Dust and tar are returned to the gasification in a known manner.

Zweckmäßigerweise führt man einen Teil des Verbrennungsga­ses in die Wirbelbettverbrennung zurück, wobei das Gas als Fluidisierungsmedium dient.Part of the combustion gas is expediently returned to the fluidized bed combustion, the gas serving as the fluidization medium.

Das Verfahren bietet auch die vorteilhafte Möglichkeit, aus dem Rohgas nach der Kühlung Schwefelverbindungen und Kohlendioxid zu entfernen und diese Stoffe der Wirbelbett­verbrennung zusammen mit Calciumverbindungen aufzugeben. Das CO₂ bleibt so dem Vergasungsverfahren erhalten und reduziert den Kohleverbrauch. Die Schwefelverbindungen, insbesondere H₂S, werden in der Wirbelbettverbrennung zu SO₂ umgewandelt und verbinden sich mit den Calciumver­bindungen, insbesondere Kalkstein oder Kalkmilch, zu Cal­ciumsulfat. Calciumsulfat wird dann mit der Achse der Ver­brennung abgezogen und kann problemlos deponiert werden.The process also offers the advantageous possibility of sulfur compounds and from the raw gas after cooling Remove carbon dioxide and give up these substances of fluidized bed combustion together with calcium compounds. The CO₂ is retained in the gasification process and reduces coal consumption. The sulfur compounds, in particular H₂S, are converted to SO₂ in the fluidized bed combustion and combine with the calcium compounds, in particular limestone or milk of lime, to form calcium sulfate. Calcium sulfate is then drawn off with the combustion axis and can be deposited without any problems.

Eine vorteilhafte Ausgestaltung des Verfahrens besteht da­rin, daß man die Wirbelbettverbrennung bei einem Druck be­treibt, der um mindestens 2 bar höher ist als der Druck der Vergasung. Dadurch kann das Verbrennungsgas ohne zu­sätzliche Kompression in die Vergasung eingeleitet werden.An advantageous embodiment of the method consists in operating the fluidized bed combustion at a pressure which is at least 2 bar higher than the pressure of the gasification. As a result, the combustion gas can be introduced into the gasification without additional compression.

Da das Rohgas und das daraus durch Abkühlung gebildete Kondensat etwa unter dem in der Vergasung herrschenden Druck anfallen, empfiehlt es sich, daß auch der Druck im Abscheider zum Behandeln des Kondensats etwa der gleiche wie in der Vergasung ist. Eine Entspannung von Kondensat, und somit die Behandlung von Entspannungsgasen, entfallen daher. Die Pumpleistung zum Einleiten der aus dem Abschei­der abgezogenen Flüssigkeiten in die Wirbelbettverbrennung und die Vergasung verringert sich.Since the raw gas and the condensate formed from it by cooling occur approximately under the pressure prevailing in the gasification, it is recommended that the pressure in the separator for treating the condensate is approximately the same as in the gasification. A relaxation of condensate, and thus the treatment of expansion gases, is therefore not necessary. The pumping power for introducing the liquids withdrawn from the separator into the fluidized bed combustion and the gasification are reduced.

Beim erfindungsgemäßen Verfahren ist es ohne weiteres mög­lich, den in der Vergasung benötigten Wasserdampf allein durch den Wasserdampfgehalt des aus der Wirbelbettverbren­nung kommenden Verbrennungsgases aufzubringen. Ein Dampf­kessel zum Erzeugen zusätzlichen Wasserdampfes für die Vergasung entfällt somit. Das Verfahren kommt auch ohne Rauchgasbehandlung, z.B. Rauchgaswäsche, aus, da Stickoxi­de und Schwefeloxide in der Vergasung reduziert werden und als N₂ bzw. H₂S anfallen, wobei das H₂S zusammen mit anderen Schwefelverbindungen in der Rohgasreinigung ent­fernt werden kann. Im Ergebnis werden beim erfindungsge­mäßen Verfahren nach außen weder SO₂ noch Stickoxide ab­gegeben, es wird Wasser gespart und die Wiederverwendung von CO₂ reduziert den Kohleverbrauch. Wegen der Reini­gungswirkung der Wirbelbettverbrennung ist das Gesamtver­fahren umweltfreundlich. Ein geringer Mehrverbrauch an Sauerstoff fällt gegenüber bekannten Verfahren nicht ins Gewicht.In the method according to the invention, it is readily possible to apply the water vapor required in the gasification solely by the water vapor content of the combustion gas coming from the fluidized bed combustion. A steam boiler for generating additional water vapor for the gasification is therefore not necessary. The process also works without flue gas treatment, eg flue gas scrubbing, since nitrogen oxides and sulfur oxides are reduced in the gasification and accumulate as N₂ or H₂S, whereby the H₂S can be removed together with other sulfur compounds in the raw gas purification. As a result, neither SO₂ nor nitrogen oxides are released to the outside in the process according to the invention, water is saved and the reuse of CO₂ reduces coal consumption. Because of the cleaning effect of fluidized bed combustion, the overall process is environmentally friendly. A small additional consumption of oxygen is not significant compared to known processes.

Bei der Wirbelbettverbrennung kann die klassische Wirbel­schicht oder bevorzugt die zirkulierende Wirbelschicht zur Anwendung kommen, für welche Einzelheiten in der deutschen Auslegeschrift 25 39 546 und dem dazu korrespondierenden US-Patent 4 165 717 beschrieben sind. Bei der zirkulieren­den Wirbelschicht sind die Geschwindigkeiten des Fluidi­sierungsgases erheblich höher als bei der klassischen Wir­belschicht, so daß ständig große Feststoffmengen aus dem Wirbelschichtreaktor ausgetragen, vom Gas getrennt und zu­rück in den Wirbelschichtreaktor geleitet werden.In fluidized bed combustion, the classic fluidized bed or, preferably, the circulating fluidized bed can be used, for which details are described in German specification 25 39 546 and the corresponding US Pat. No. 4,165,717. In the circulating fluidized bed, the speeds of the fluidizing gas are considerably higher than in the classic fluidized bed, so that large amounts of solids are continuously discharged from the fluidized bed reactor, separated from the gas and fed back into the fluidized bed reactor.

Einzelheiten des erfindungsgemäßen Verfahrens werden mit Hilfe der Zeichnung erläutert.Details of the method according to the invention are explained with the aid of the drawing.

Der Vergasung 1 wird körnige Kohle mit einem Kornbereich von etwa 3 bis 60 mm durch die Leitung 2 zugeführt. Zur Vereinfachung sind in der Zeichnung Schleuseneinrichtungen nicht dargestellt. Die Vergasung 1, bei welcher sich der körnige Brennstoff im Festbett befindet, arbeitet im Druckbereich von 5 bis 100 bar. Vergasungsmittel kommen aus der Leitung 3, sie bestehen aus einem Verbrennungsgas, dem durch die Leitung 4 Sauerstoff zugegeben wird. Der un­verbrennliche Rückstand der Vergasung, bei dem es sich um feste Asche oder flüssige Schlacke handelt, wird in der Leitung 5 abgeführt.The gasification 1 is fed granular coal with a grain area of about 3 to 60 mm through the line 2. For simplification, lock devices are not shown in the drawing. The gasification 1, in which the granular fuel is in the fixed bed, works in the pressure range from 5 to 100 bar. Gasifying agents come from line 3, they consist of a combustion gas to which oxygen is added through line 4. The incombustible residue of the gasification, which is solid ash or liquid slag, is discharged in line 5.

Das Rohgas der Vergasung gelangt in der Leitung 6 zu einem Waschkühler 7, in welchen durch die Leitung 8 Wasser oder überwiegend aus Wasser bestehendes Kondensat zugeführt wird. Im anschließenden Abhitzekessel 10 erfolgt eine wei­tere Kühlung, so daß das Rohgas in der Leitung 11 mit Tem­peraturen im Bereich von 120 bis 180°C abzieht und im Sumpf des Abhitzekessels 10 ein Kondensat mit ebenfalls Temperaturen von 120 bis 180°C anfällt. Dieses Kondensat wird in der Leitung 12 einem Abscheider 13 aufgegeben.The raw gas of the gasification passes in line 6 to a washer cooler 7, in which water or condensate consisting predominantly of water is fed through line 8. In the subsequent waste heat boiler 10, further cooling takes place, so that the raw gas in line 11 is drawn off at temperatures in the range from 120 to 180 ° C. and in the bottom of waste heat boiler 10 a condensate is also obtained at temperatures of from 120 to 180 ° C. This condensate is fed to a separator 13 in line 12.

Der Druck im Abscheider 13 ist im vorliegenden Fall nur etwa 1 bis 5 bar niedriger als in der Vergasung 1. Im Ab­scheider 13 erfolgt in an sich bekannter Weise die Schwer­krafttrennung verschiedener Komponenten des Kondensats. Eine schwere Phase, die reich an Staub und Teer ist, wird in der Leitung 14 abgezogen, wobei es sich anbietet, diese Phase ebenfalls der Vergasung 1 zuzuführen. Eine wasser­reiche Phase, die üblicherweise als Gaswasser bezeichnet wird, zieht man in der Leitung 15 ab und gibt sie unter der Wirkung der Pumpe 16 einer Wirbelbettverbrennung 17 auf. Falls erforderlich, wird Zusatzwasser in der Lei­tung 9 herangeführt.In the present case, the pressure in the separator 13 is only about 1 to 5 bar lower than in the gasification 1. In the separator 13, the gravitational separation of various components of the condensate takes place in a manner known per se. A heavy phase, which is rich in dust and tar, is drawn off in line 14, it being advisable to also feed this phase to gasification 1. A water-rich phase, which is usually referred to as gas water, is drawn off in the line 15 and, under the action of the pump 16, is given up to a fluidized bed combustion 17. If necessary, make-up water is introduced in line 9.

Der Wirbelbettverbrennung 17 führt man auch ein Abgas aus der Leitung 18 zu, das durch das Gebläse 19 aus einer Gas­reinigung 20 angesaugt wird. In der Gasreinigung 20 wird das Rohgas aus der Leitung 11 behandelt, wobei man durch bekannte Verfahren Schwefelverbindungen, insbesondere H₂S, sowie auch teilweise CO₂ entfernt. CO₂ und die­se Schwefelverbindungen sind im Abgas der Leitung 18 ent­halten. Das gereinigte Gas, das nun vor allem aus Wasser­stoff und Kohlenmonoxid besteht, steht zur weiteren Ver­wendung in der Leitung 21 zur Verfügung.The fluidized bed combustion 17 is also supplied with an exhaust gas from the line 18, which is sucked in by the fan 19 from a gas cleaning device 20. In the gas cleaning 20, the raw gas from the line 11 is treated, sulfur compounds, in particular H₂S, and also partly CO₂ being removed by known processes. CO₂ and these sulfur compounds are contained in the exhaust gas of line 18. The cleaned gas, which now mainly consists of hydrogen and carbon monoxide, is available for further use in line 21.

Der Wirbelbettverbrennung17 führt man als Brennstoff Feinkohle mit Korngrößen bis 10 mm durch die Leitung 22 und gemahlenen Kalkstein, Dolomit oder Kalkmilch durch die Leitung 23 zu. Diese Calciumverbindungen werden in der Verbrennung 17 bei den dort herrschenden Temperaturen von 750 bis 1000°C und vorzugsweise 800 bis 900°C zu CaO umge­wandelt, welches das aus den Schwefelverbindungen gebilde­te SO₂ als Calciumsulfat bindet. Als Wirbelgas wird der Verbrennung 17 ein in der Leitung 25 zurückgeführter Teil­strom der Verbrennungsgase verwendet, dem man in der Lei­tung 26 Sauerstoff, Luft oder auch mit Sauerstoff angerei­cherte Luft zumischt.The fluidized bed combustion 17 is supplied with fine coal with a grain size of up to 10 mm through line 22 and ground limestone, dolomite or milk of lime through line 23 as fuel. These calcium compounds are converted in the combustion 17 at the prevailing temperatures of 750 to 1000 ° C and preferably 800 to 900 ° C to CaO, which binds the SO₂ formed from the sulfur compounds as calcium sulfate. The combustion 17 uses a partial flow of the combustion gases which is returned in line 25 and to which oxygen, air or also oxygen-enriched air is mixed in line 26.

Durch die hohen Wirbelgasgeschwindigkeiten in der Verbren­nung 17 werden zusammen mit den Verbrennungsgasen ständig erhebliche Feststoffmengen aus der Verbrennungszone ausge­tragen und durch die Leitung 27 einem Zyklon 28 zugeführt, in welchem die Feststoffe aus dem Gas weitgehend abge­schieden werden. Die Feststoffe, die überwiegend aus Brennstoffasche und Calciumsulfat bestehen, verlassen den Zyklon 28 in der Leitung 30 und werden zu etwa 80 bis 90 % in der Leitung 31 in die Verbrennung 17 zurückgeführt. Die restlichen Feststoffe zieht man in der Leitung 32 ab und kann sie nach einer nicht dargestellten Kühlung z.B. depo­nieren. Die Wirbelbettverbrennung 17 mit der Verbindungs­leitung 27, dem Zyklon 28 sowie den Leitungen 30 und 31 stellt die für die zirkulierende Wirbelschicht typische apparative Anordnung dar.Due to the high fluidizing gas velocities in the combustion 17, substantial amounts of solids are continuously discharged from the combustion zone together with the combustion gases and fed through the line 27 to a cyclone 28 in which the solids are largely separated from the gas. The solids, which predominantly consist of fuel ash and calcium sulfate, leave the cyclone 28 in line 30 and about 80 to 90% are returned in line 31 to the combustion 17. The remaining solids are drawn off in line 32 and can be used after cooling, not shown, e.g. deposit. The fluidized bed combustion 17 with the connecting line 27, the cyclone 28 and the lines 30 and 31 represents the apparatus arrangement which is typical for the circulating fluidized bed.

Das im Zyklon 28 von Feststoffen weitgehend befreite Ver­brennungsgas strömt in der Leitung 33 ab, wobei es Tempe­raturen von 750 bis 1000°C und vorzugsweise 800 bis 900°C aufweist. Zum Kühlen und zum Erhöhen des Wasserdampfgehal­tes wird diesem Gas durch die Leitung 34 herangeführtes Wasser, bei dem es sich auch um Kondensat oder Gaswasser handeln kann, eingesprüht. Das mit Wasserdampf angerei­cherte Verbrennungsgas wird dann teilweise über das Geblä­se 35 und die Leitung 25 in der bereits beschriebenen Wei­se zur Verbrennung 17 zurückgeführt, das restliche Ver­brennungsgas führt man in der Leitung 3 der Vergasung 1 zu.The combustion gas largely freed of solids in the cyclone 28 flows out in the line 33, it having temperatures of 750 to 1000 ° C. and preferably 800 to 900 ° C. For cooling and increasing the water vapor content, this gas is introduced through line 34 Water sprayed in, which can also be condensate or gas water. The combustion gas enriched with water vapor is then partly returned to the combustion 17 via the blower 35 and the line 25 in the manner already described, the remaining combustion gas is fed to the gasification 1 in line 3.

Beispiel:Example:

In einer der Zeichnung entsprechenden Verfahrensführung gibt man der Vergasung 1 1000 kg Kohle (wasser- und aschefrei gerechnet) auf. Die Kohle, die einen Körnungs­bereich von 5 bis 40 mm aufweist, enthält 51 kg Feuchte, 126 kg Asche und 21 kg Schwefel. Als Vergasungsmittel führt man durch die Leitung 3 Verbrennungsgas heran, das aus folgenden Gaskomponenten besteht:
CO₂ 107 Nm³
O₂ 7 Nm³
N₂ 2 Nm³
und das 323 kg Wasserdampf enthält. Die Temperatur des Ga­ses liegt bei 400°C. Dem Verbrennungsgas werden 477 Nm³ Sauerstoff aus der Leitung 4 zugemischt. Der Druck in der Vergasung 1 liegt bei 30 bar und in der Verbrennung 17 bei 32 bar.In a procedure corresponding to the drawing, the gasification is given 1 1000 kg of coal (free of water and ash). The coal, which has a grain size range of 5 to 40 mm, contains 51 kg moisture, 126 kg ash and 21 kg sulfur. Combustion gas, which consists of the following gas components, is brought in through line 3 as the gasifying agent:
CO₂ 107 Nm³
O₂ 7 Nm³
N₂ 2 Nm³
and that contains 323 kg of water vapor. The temperature of the gas is 400 ° C. 477 Nm³ of oxygen from line 4 are mixed into the combustion gas. The pressure in gasification 1 is 30 bar and in combustion 17 is 32 bar.

Im Abhitzekessel 10 fallen bei einer Temperatur von 180°C 230 kg Kondensat an, das 185 kg Wasser enthält. Dieses Wasser wird in einem Abscheider13 als Gaswasser abge­trennt und durch die Leitung 15 der Verbrennung 17 zuge­führt. Durch die Leitung 9 wird Rohwasser in einer Menge von 20 kg zugegeben. In der Gasreinigung 20 entsteht ein Abgas aus 49 Nm³ CO₂, 14 Nm³ H₂S und 1 Nm³ COS, das über den Kompressor 19 und die Leitung 18 ebenfalls in die Verbrennung 17 gegeben wird, die als zirkulierende Wirbelschicht ausgestaltet ist. Der Verbrennung 17 gibt man ferner 26 kg Feinkohle, 110 kg gemahlenen Kalkstein und 76 Nm³ Sauerstoff auf. Das Verbrennungsgas der Lei­tung 33 weist eine Temperatur von 850°C auf, es wird mit 96 kg Rohwasser aus der Leitung 34 bedüst und dabei auf 400°C abgekühlt. 2200 Nm³ Reingas verlassen in der Lei­tung 21 die Gasreinigung 20.In the waste heat boiler 10 at a temperature of 180 ° C 230 kg of condensate containing 185 kg of water. This water is separated as gas water in a separator 13 and fed to the combustion 17 through the line 15. Raw water is added in an amount of 20 kg through line 9. In the gas cleaning 20, an exhaust gas of 49 Nm³ CO₂, 14 Nm³ H₂S and 1 Nm³ COS is created, which is also passed through the compressor 19 and line 18 into the combustion 17, which is designed as a circulating fluidized bed. The combustion 17 is also given up to 26 kg of fine coal, 110 kg of ground limestone and 76 Nm³ of oxygen. The combustion gas of line 33 has a temperature of 850 ° C, it is sprayed with 96 kg of raw water from line 34 and cooled to 400 ° C. 2200 Nm³ of clean gas leave the gas cleaning 20 in line 21.

Claims (7)

1. Verfahren zum Behandeln von wasserhaltigem Kondensat aus der Kühlung des Rohgases der Vergasung fester Brennstoffe mit Sauerstoff, Wasserdampf und Kohlendiox­id enthaltenden Vergasungsmitteln unter einem Druck von 5 bis 100 bar, wobei die Brennstoffe ein Festbett bil­den, das sich langsam nach unten bewegt und unter dem man die unverbrennlichen mineralischen Bestandteile des Brennstoffs als feste Asche oder flüssige Schlacke ab­zieht, dadurch gekennzeichnet, daß man das Kondensat zumindest teilweise in einer Wirbelschichtverbrennung bei Temperaturen im Bereich von etwa 750 bis 1000°C verbrennt und das wasserdampfhaltige Verbrennungsgas aus der Verbrennung in die Vergasung leitet.1. A method for treating water-containing condensate from the cooling of the raw gas of the gasification of solid fuels with oxygen, water vapor and carbon dioxide-containing gasifying agents under a pressure of 5 to 100 bar, the fuels forming a fixed bed which moves slowly downwards and under which the incombustible mineral constituents of the fuel are drawn off as solid ash or liquid slag, characterized in that the condensate is at least partially burned in a fluidized bed combustion at temperatures in the range from approximately 750 to 1000 ° C. and the combustion gas containing water vapor is passed from the combustion into the gasification . 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das beim Kühlen des Rohgases anfallende Kondensat in einem Abscheider von Staub und Teer zumindest teilweise befreit wird, bevor man das Kondensat der Wirbelbett­verbrennung zuführt.2. The method according to claim 1, characterized in that the condensate obtained during cooling of the raw gas is at least partially freed of dust and tar in a separator before the condensate is fed to the fluidized bed combustion. 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeich­net, daß man einen Teil des Verbrennungsgases in die Wirbelbettverbrennung zurückführt.3. The method according to claim 1 or 2, characterized in that a part of the combustion gas is returned to the fluidized bed combustion. 4. Verfahren nach Anspruch 1 oder einem der folgenden, da­durch gekennzeichnet, daß man aus dem Rohgas nach der Kühlung Schwefelverbindungen und einen Teil des Kohlen­dioxid entfernt und diese Stoffe der Wirbelbettverbren­nung zusammen mit Calciumverbindungen aufgibt.4. The method according to claim 1 or one of the following, characterized in that one removes sulfur compounds and a portion of the carbon dioxide from the raw gas after cooling and gives up these substances of the fluidized bed combustion together with calcium compounds. 5. Verfahren nach Anspruch 1 oder einem der folgenden, da­durch gekennzeichnet, daß man das Verbrennungsgas durch Einsprühen von Wasser kühlt.5. The method according to claim 1 or one of the following, characterized in that the combustion gas is cooled by spraying water. 6. Verfahren nach Anspruch 1 oder einem der folgenden, da­durch gekennzeichnet, daß die Wirbelbettverbrennung bei einem Druck betrieben wird, der um mindestens 2 bar hö­her ist als der Druck in der Vergasung.6. The method according to claim 1 or one of the following, characterized in that the fluidized bed combustion is operated at a pressure which is at least 2 bar higher than the pressure in the gasification. 7. Verfahren nach Anspruch 1 oder einem der folgenden, da­durch gekennzeichnet, daß der Druck im Abscheider etwa der gleiche ist wie in der Vergasung.7. The method according to claim 1 or one of the following, characterized in that the pressure in the separator is approximately the same as in the gasification.
EP85201775A 1985-11-01 1985-11-01 Process for treating an aqueous condensate Withdrawn EP0220342A1 (en)

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ES8602867A ES2003449A6 (en) 1985-11-01 1986-10-31 Process for treating an aqueous condensate.
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FR2694566A1 (en) * 1992-08-06 1994-02-11 Schwarze Pumpe Energiewerke Ag Combined process for the gasification of residual materials and / or solid, pasty and liquid rejects.
WO2009108737A2 (en) * 2008-02-27 2009-09-03 Alstom Technology Ltd Air-fired co2 capture ready circulating fluidized bed steam generators
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DE3929926A1 (en) * 1989-09-08 1991-03-21 Metallgesellschaft Ag METHOD FOR THE TREATMENT OF GASES FROM THE GASIFICATION OF SOLID, FINE-COMBINED FUELS
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RIN1 Information on inventor provided before grant (corrected)

Inventor name: ERGEZINGER, JAKOB