EP0776961B1 - Procédé de traitement des gaz de fumées provenant de la gazéification de matières carbonées - Google Patents

Procédé de traitement des gaz de fumées provenant de la gazéification de matières carbonées Download PDF

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Publication number
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
Authority
EP
European Patent Office
Prior art keywords
gas
exhaust gas
solids
temperatures
passed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP96116298A
Other languages
German (de)
English (en)
Other versions
EP0776961A1 (fr
Inventor
Johannes Dr. Albrecht
Johannes Dr. Löffler
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
MG Technologies AG
Original Assignee
Metallgesellschaft AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Metallgesellschaft AG filed Critical Metallgesellschaft AG
Publication of EP0776961A1 publication Critical patent/EP0776961A1/fr
Application granted granted Critical
Publication of EP0776961B1 publication Critical patent/EP0776961B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • 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
    • C10J3/72—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
    • 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
    • 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
    • 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

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.

Claims (4)

  1. Procédé de traitement de l'effluent gazeux de la gazéification de matière carbonée, la gazéification s'effectuant avec addition de gaz contenant de l'oxygène libre à des températures de l'ordre de 700 à 1100°C et avec formation d'un effluent gazeux contenant de la matière solide que l'on fait passer dans au moins un cyclone pour séparer les matières solides, caractérisé en ce qu'il consiste à envoyer l'effluent gazeux contenant de la matière solide à des températures de l'ordre de 700 à 1100°C dans un cyclone de séparation qui comporte à la partie supérieure un conduit d'évacuation de gaz et à la partie inférieure un canal de déchargement de la matière solide, à envoyer dans une chambre d'oxydation en passant par le canal en même temps que les matières solides déchargées un courant partiel de 5 à 30 % de l'effluent gazeux envoyé au cyclone de séparation et à produire dans la chambre d'oxydation avec addition hypostoechiométrique à hyperstoechiométrique de O2 et à des températures de l'ordre de 1300 à 1800°C un gaz de fumée ou un gaz combustible et de la scorie, à envoyer le gaz de fumée ou le combustible en même temps que la partie de l'effluent gazeux provenant du conduit d'évacuation des gaz du cyclone de séparation dans une chambre de mélange dans laquelle le mélange gazeux passe à des températures de 900 à 1200°C et avec une durée de séjour d'au moins 0,5 seconde et à refroidir le mélange gazeux soutiré de la chambre de mélange.
  2. Procédé suivant la revendication 1, caractérisé en ce qu'il consiste à refouler dans la chambre d'oxydation les matières solides provenant du canal du cyclone de séparation en même temps que le courant partiel de l'effluent gazeux par un gaz de poussée.
  3. Procédé suivant la revendication 2, caractérisé en ce qu'il consiste à envoyer du gaz contenant de l'oxygène libre à la chambre de mélange.
  4. Procédé suivant la revendication 1 ou l'une des suivantes, caractérisé en de qu'il consiste à envoyer des additifs à la chambre d'oxydation.
EP96116298A 1995-11-28 1996-10-11 Procédé de traitement des gaz de fumées provenant de la gazéification de matières carbonées Expired - Lifetime EP0776961B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19544200A DE19544200A1 (de) 1995-11-28 1995-11-28 Verfahren zum Behandeln von Abgas aus der Vergasung von kohlenstoffhaltigem Material
DE19544200 1995-11-28

Publications (2)

Publication Number Publication Date
EP0776961A1 EP0776961A1 (fr) 1997-06-04
EP0776961B1 true EP0776961B1 (fr) 2001-02-28

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP96116298A Expired - Lifetime EP0776961B1 (fr) 1995-11-28 1996-10-11 Procédé de traitement des gaz de fumées provenant de la gazéification de matières carbonées

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EP (1) EP0776961B1 (fr)
DE (2) DE19544200A1 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19754802B4 (de) * 1997-12-10 2008-04-03 Sasol-Lurgi Technology Company (Pty) Ltd Verfahren zum thermischen Behandeln eines aus der Vergasung kohlenstoffhaltiger Materialien kommenden Gasgemisches
DE10021448A1 (de) * 2000-05-03 2001-11-08 Messer Griesheim Gmbh Verfahren und Vorrichtung für die Verbrennung von organischem Reststoff
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 (zh) * 2016-03-04 2016-06-08 广东工业大学 锯末高温气化炉

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2836175A1 (de) * 1978-08-18 1980-02-28 Metallgesellschaft Ag Verfahren zum vergasen fester, feinkoerniger brennstoffe
DE3673362D1 (de) * 1985-12-27 1990-09-13 Shell Int Research Oxydation von flugasche.
DE4235412A1 (de) * 1992-10-21 1994-04-28 Metallgesellschaft Ag Verfahren zum Vergasen von brennbare Bestandteile enthaltenden Abfallstoffen
DE4412004A1 (de) * 1994-04-07 1995-10-12 Metallgesellschaft Ag Verfahren zum Vergasen von Abfallstoffen in der zirkulierenden Wirbelschicht

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Publication number Publication date
DE59606497D1 (de) 2001-04-05
DE19544200A1 (de) 1997-06-05
EP0776961A1 (fr) 1997-06-04

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