EP2883942A1 - Procédé et installation de gazage de matières de base organiques, solides - Google Patents

Procédé et installation de gazage de matières de base organiques, solides Download PDF

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Publication number
EP2883942A1
EP2883942A1 EP14004094.0A EP14004094A EP2883942A1 EP 2883942 A1 EP2883942 A1 EP 2883942A1 EP 14004094 A EP14004094 A EP 14004094A EP 2883942 A1 EP2883942 A1 EP 2883942A1
Authority
EP
European Patent Office
Prior art keywords
temperature gasifier
residual coke
synthesis gas
gas
coke
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.)
Withdrawn
Application number
EP14004094.0A
Other languages
German (de)
English (en)
Inventor
Sven Halang
Thomas Heidrich
Gerald GAUBE
Ralf Tatschke
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.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Publication of EP2883942A1 publication Critical patent/EP2883942A1/fr
Withdrawn legal-status Critical Current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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • 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
    • C10K1/024—Dust removal by filtration
    • 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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1693—Integration of gasification processes with another plant or parts within the plant with storage facilities for intermediate, feed and/or product
    • 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

Definitions

  • the invention relates to a method and a plant for the at least partial gasification of solid, organic feedstock, in particular of biomass, with a low-temperature gasifier and a high-temperature gasifier.
  • Processes for the production of synthesis gas from solid, organic feedstock also referred to for short as gasification processes, are known.
  • coal or biomass are used as starting material for such processes.
  • biomass gasification processes for example, used wood and forestry wood or so-called energy wood, but also agricultural residues such as straw or chaff are used.
  • BTL Biomass to Liquids method
  • GTL gas-to-liquids
  • CTL coal-to- Liquids
  • An example of a plant for the production of BTL fuels is at Kiener, C. and Bilas, I .: Synthetic biofuel of the second generation. World's first commercial BTL production plant. Energy 2.0, July 2008, pp. 42-44 , shown.
  • the feedstock such as biomass
  • a gasification agent at temperatures between about 300 ° C and 600 ° C to coke (in the case of biomass so-called biococ) and carbonization reacted.
  • the implementation is referred to in this application as "smoldering". Smoldering is known to be characterized by substoichiometric oxygen supply and thus incomplete combustion at a comparatively low temperature.
  • the carbonization gas is then transferred to a combustion chamber of the high-temperature gasifier and there with an oxygen-containing gas, for example with more or less pure oxygen, but also with air and / or oxygen-containing exhaust gases, e.g. from gas turbines or internal combustion engines, partially oxidized.
  • an oxygen-containing gas for example with more or less pure oxygen, but also with air and / or oxygen-containing exhaust gases, e.g. from gas turbines or internal combustion engines, partially oxidized.
  • an oxygen-containing gas for example with more or less pure oxygen, but also with air and / or oxygen-containing exhaust gases, e.g. from gas turbines or internal combustion engines, partially oxidized.
  • an oxygen-containing gas for example with more or less pure oxygen
  • air and / or oxygen-containing exhaust gases e.g. from gas turbines or internal combustion engines
  • the synthesis gas produced in this way can be brought into contact with coke from the low-temperature gasifier.
  • the coke may be previously treated separately (e.g., by grinding and sifting) and then introduced into the quench unit.
  • chemical quench By endothermic reactions between coke and synthesis gas (so-called chemical quench) the latter is cooled to a temperature of for example 800 ° C to 1200 ° C. This also causes partial conversion of the carbon dioxide to carbon monoxide.
  • the carbon monoxide-rich synthesis gas produced in this way can then be further conditioned.
  • the conditioning includes, for example, a further cooling, a dedusting, a compression and / or the separation of residual carbon dioxide.
  • a dedusting device for example, a cyclone is used.
  • the coke (residual coke) which has partially reacted in the quench unit is separated off and can be returned to the oxidation unit of the high-temperature gasifier.
  • the syngas stream is contacted with a scrubbing liquid stream to receive undesirable components of the syngas stream into the liquid. Purified and conditioned synthesis gas is then taken from the plant.
  • the residual coke separated off from the syngas in the dedusting device is typically cooled by means of cooling screws and discharged via a container lock from the dedusting device or from the pressure atmosphere in which it is located.
  • the object of the invention is therefore a more efficient utilization of residual coke.
  • the invention is based on a known process for the at least partial gasification of solid, organic feedstock, for example biomass.
  • a tar-containing carbonization gas is recovered in a low-temperature gasifier by smoldering, as explained above.
  • the carbonization gas is then reacted in a high-temperature gasifier by partial oxidation and then partial reduction to a synthesis gas and further processed downstream of the high-temperature gasifier in appropriate treatment facilities.
  • the present invention is characterized in that it allows a more effective recycling and thus recovery of residual coke.
  • the residual coke separated off in the wet scrubbing is fed to the high-temperature gasifier in the form of a slurry.
  • slurry is understood to mean a suspension of residual coke particles in a suitable liquid, in particular water.
  • alkalis dissolved in the wet scrubbing are at least partially stripped off with an excess washing liquid.
  • Such a removal of excess washing liquid makes it possible to adjust a tolerable alkali content of the slurry in an effective manner.
  • residual coke accumulating in the dedusting device is also separated from the synthesis gas during dedusting and at least partially supplied to the high-temperature gasifier in support of the reduction.
  • the combination of a (dry) residual coke recycle with a (wet) residual coke slurry recycle in the high-temperature gasifier proves to be particularly advantageous, since depending on the specific operating conditions variations are conceivable. For example, it is possible to completely dispense with the dry separation of residual coke from the synthesis gas. In this case, the entire residual coke is then deposited over the slurry and recycled. It is also possible, a large part of the residual coke, in particular most of the residual coke, z. B.
  • the slurry system treats only the amount of residual coke that the cyclone does not deposit.
  • the system primarily serves to reduce the coke load of the wastewater.
  • the residual coke slurry is introduced via a filter into a residual coke slurry container.
  • a container can be used in a simple manner for the buffer of residual coke slurry.
  • a pressure within the residual coke slurry container is adjustable in a particularly simple manner by application of an inert gas, such as nitrogen or carbon dioxide.
  • FIG. 1 a system is shown, which is set up for carrying out the method according to the invention.
  • the plant comprises a low temperature carburetor 1 and a high temperature carburetor 2.
  • a solid organic feedstock A such as biomass such as wood or corresponding waste, as previously explained, are fed.
  • the low-temperature gasifier 1 is set up to blaze the solid organic feedstock A.
  • the Low temperature carburetor 1 externally, ie allothermic, for example, be heated to 300 to 600 ° C.
  • the provision of the heat can be done for example by the waste heat of the high-temperature gasifier 2.
  • the low-temperature gasifier 1 can also be heated autothermally, for example by partial oxidation of the carbon present in the solid organic feedstock A with a separately supplied oxygen G.
  • a line can be discharged from the low temperature carburetor 1 a carbonization B and transferred to the high-temperature carburetor 2.
  • the high temperature carburetor 2 is formed in two parts. It comprises an oxidation unit 21 and a quench unit 22.
  • the carbonization gas B is partially oxidized with a supplied oxygen-containing gas H, resulting in temperatures of, for example, 1400 ° C. to 2000 ° C.
  • the quench unit 22 the synthesis gas D is brought into contact with pyrolysis coke C from the low-temperature gasifier 10.
  • the carbon monoxide-rich synthesis gas D produced in this way is subsequently cooled in a cooling device 3 downstream of the quench unit 22, for example to a temperature of 600 to 800 ° C.
  • a cooling device 3 downstream of the quench unit 22, for example to a temperature of 600 to 800 ° C.
  • alkalis there is a condensation of alkalis, which are initially present in the gaseous state in the synthesis gas D, on the surface of the coke still present in the synthesis gas.
  • a dedusting device 4 Downstream of the cooling device 3 are a dedusting device 4, for example a cyclone, and a wet scrubber 5.
  • the dedusting device 4 the coke which has partially reacted in the quench unit 22, the so-called residual coke E, is separated and passed to the oxidation unit 21 of the high-temperature gasifier 2.
  • the synthesis gas stream is brought into contact with a washing liquid stream, in particular water, in order to take up undesired components of the synthesis gas stream into the liquid.
  • Sufficient Purified and conditioned synthesis gas F can then be taken from the plant and fed to downstream processes, for example for the production of synthetic biofuels.
  • scrubbing liquid for example water, in the wet scrubber 5
  • alkalies which are condensed on the remaining coke particles are dissolved in the scrubbing liquid, thus particularly containing the contaminated scrubbing liquid Residual coke particles, dissolved alkalis and other water-soluble constituents of the crude synthesis gas.
  • a circuit for washing liquid is provided, via which washing liquid can be withdrawn at an outlet 5a of the wet scrubber and, after passing through the circuit at an inlet 5b, can again be introduced into the wet scrubber.
  • a circulation pump 6, a backwashable filter 8 and a circulation cooler 10 is provided.
  • This detergent circuit serves for the extraction of washing liquid, which, as mentioned, in particular contains dissolved alkalis and residual coke.
  • washing liquid which, as mentioned, in particular contains dissolved alkalis and residual coke.
  • the filter 8 residual coke present in the scrubbing liquid is filtered out, and fed to a residual coke slurry container 12.
  • the washing water with the alkalis dissolved therein passes through the filter 8, and can either be withdrawn from the system as excess water via a valve 14, or returned to the wet scrubber 5 via the circulation cooler 10 and the inlet 5b.
  • the residual coke slurry container 12 can be acted upon to provide a slurry of a desired viscosity with a corresponding liquid, for example water.
  • the residual coke slurry container is provided with a mixing device 13 which can be driven by a motor 15.
  • An inert gas can be supplied to the residual coke slurry container 12 via a valve 18, whereby a desired pressure in the container can be provided.
  • residual coke slurry G is withdrawn from the residual coke slurry container via an outlet 12a and fed to the high-temperature gasifier 2.
  • the connection between the output 12a and the oxidation unit 21 of the high-temperature gasifier is not shown in detail.
  • the optional dedusting device 4 is partially or completely bypassable by means of a bypass line 20, in which a valve 22 is provided.
  • a valve 22 is provided.
  • complete circumvention of the dedusting 4 for example, by complete opening of the valve 22
  • the slurry system treats only the amount that the dedusting device 4 does not deposit.
  • the system is primarily used to reduce the coke load of the wastewater.
  • the slurry residual coking system described can be made considerably less expensive than residual coking systems according to the prior art.
  • such a residual coking system has substantially fewer mechanical moving parts, and therefore proves to be more reliable in practice.
  • the illustrated slurry residual coking system enables a reduction of the load of the waste water with coke, whereby a simplified wastewater treatment is provided.
  • the overall efficiency of the carburetor increases because no coke needs to be discarded. It turns out that such a slurry residual coking system requires less electrical energy than solutions according to the prior art.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)
EP14004094.0A 2013-12-11 2014-12-04 Procédé et installation de gazage de matières de base organiques, solides Withdrawn EP2883942A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE102013020792.4A DE102013020792A1 (de) 2013-12-11 2013-12-11 Verfahren und Anlage zur Vergasung von festem, organischem Einsatzmaterial

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EP2883942A1 true EP2883942A1 (fr) 2015-06-17

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EP14004094.0A Withdrawn EP2883942A1 (fr) 2013-12-11 2014-12-04 Procédé et installation de gazage de matières de base organiques, solides

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023281085A1 (fr) * 2021-07-08 2023-01-12 Mash Makes A/S Hydrotraitement d'une charge de combustible

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4139512A1 (de) 1991-11-29 1993-06-03 Noell Dbi Energie Entsorgung Verfahren zur thermischen verwertung von abfallstoffen
DE4209549A1 (de) 1992-03-24 1993-09-30 Vaw Ver Aluminium Werke Ag Verfahren zur thermischen Behandlung von Reststoffen, z.B. zur Trennung und Verwertung von Metallverbunden mit organischen Anteilen, mittels einer Kombination aus Pyrolyse und Vergasung
EP0745114B1 (fr) 1994-02-15 1999-03-24 CRG Kohlenstoffrecycling Ges.mbH Procede de generation de gaz combustible
DE10047787A1 (de) * 2000-09-20 2002-03-28 Ver Energiewerke Ag Verfahren zur Brenngaserzeugung aus Hausmüll und ähnlichen Abfällen durch Pyrolyse mit nachgeschalteter Umwandlung der Pyrolyseprodukte Schwelgas und Schwelkoks in Permanentgas
WO2010069068A1 (fr) * 2008-12-19 2010-06-24 Enerkem, Inc. Production de gaz de synthèse par oxydation contrôlée de biomasse
US20110197510A1 (en) * 2010-02-16 2011-08-18 Boris Nickolaevich Eiteneer Method and apparatus to reactivate carbon solids

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4139512A1 (de) 1991-11-29 1993-06-03 Noell Dbi Energie Entsorgung Verfahren zur thermischen verwertung von abfallstoffen
DE4209549A1 (de) 1992-03-24 1993-09-30 Vaw Ver Aluminium Werke Ag Verfahren zur thermischen Behandlung von Reststoffen, z.B. zur Trennung und Verwertung von Metallverbunden mit organischen Anteilen, mittels einer Kombination aus Pyrolyse und Vergasung
EP0745114B1 (fr) 1994-02-15 1999-03-24 CRG Kohlenstoffrecycling Ges.mbH Procede de generation de gaz combustible
DE10047787A1 (de) * 2000-09-20 2002-03-28 Ver Energiewerke Ag Verfahren zur Brenngaserzeugung aus Hausmüll und ähnlichen Abfällen durch Pyrolyse mit nachgeschalteter Umwandlung der Pyrolyseprodukte Schwelgas und Schwelkoks in Permanentgas
WO2010069068A1 (fr) * 2008-12-19 2010-06-24 Enerkem, Inc. Production de gaz de synthèse par oxydation contrôlée de biomasse
US20110197510A1 (en) * 2010-02-16 2011-08-18 Boris Nickolaevich Eiteneer Method and apparatus to reactivate carbon solids

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
KIENER, C.; BILAS, 1.: "Synthetischer Biokraftstoff der zweiten Generation. Weltweit erste kommerzielle BTL-Produktionsanlage", ENERGY, vol. 2.0, July 2008 (2008-07-01), pages 42 - 44

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023281085A1 (fr) * 2021-07-08 2023-01-12 Mash Makes A/S Hydrotraitement d'une charge de combustible

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