EP1027407A1 - Procede et dispositif de production de gaz de combustion, de gaz de synthese et de gaz de reduction a partir de combustibles solides - Google Patents

Procede et dispositif de production de gaz de combustion, de gaz de synthese et de gaz de reduction a partir de combustibles solides

Info

Publication number
EP1027407A1
EP1027407A1 EP98949009A EP98949009A EP1027407A1 EP 1027407 A1 EP1027407 A1 EP 1027407A1 EP 98949009 A EP98949009 A EP 98949009A EP 98949009 A EP98949009 A EP 98949009A EP 1027407 A1 EP1027407 A1 EP 1027407A1
Authority
EP
European Patent Office
Prior art keywords
gas
combustion chamber
gasification
slag
reactor
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.)
Granted
Application number
EP98949009A
Other languages
German (de)
English (en)
Other versions
EP1027407B1 (fr
Inventor
Bodo Wolf
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.)
Choren Industries GmbH
Original Assignee
Individual
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 Individual filed Critical Individual
Publication of EP1027407A1 publication Critical patent/EP1027407A1/fr
Application granted granted Critical
Publication of EP1027407B1 publication Critical patent/EP1027407B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow gasifiers
    • 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
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C10J3/487—Swirling or cyclonic gasifiers
    • 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
    • C10J3/48—Apparatus; Plants
    • C10J3/52—Ash-removing devices
    • C10J3/526—Ash-removing devices for entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners

Definitions

  • the invention relates to a method and a device for generating fuel, synthesis and reduction gas from renewable and fossil fuels, other biomass, waste or sludge, preferably for pyrolysis products made therefrom according to patent DE 44 04 673, these being used when pyrolysis products are used their supply to the reactor largely in solid and gaseous products, eg. B. carbonization gas and charcoal, separately and separately to the reactor.
  • the device according to the invention can be used in the energy industry, chemical industry and metallurgy for the highly efficient generation of fuel, synthesis and reduction gas for engines, synthesis processes, ore reduction and pig iron production.
  • the reactants have very short residence times.
  • a very large measurement and monitoring effort is necessary.
  • Entrained-flow reactors which are fed with fuel by a separate pyrolysis have the disadvantage that the pyrolysis products are cooled before being fed into the reactor and, in addition to the heat losses, also require a high outlay for gas processing and handling of the liquid products.
  • the object to be achieved by the invention is to propose a process and a reactor which, compared with the prior art, operate at an average lower temperature level with higher exergetic efficiency and generate a gasification gas which is free from hydrocarbons and chlorinated hydrocarbons (dioxins, furans), which can be used as a fuel gas for electricity generation, as a synthesis gas or as a reducing gas in a heat with ore reduction.
  • a gasification gas which is free from hydrocarbons and chlorinated hydrocarbons (dioxins, furans), which can be used as a fuel gas for electricity generation, as a synthesis gas or as a reducing gas in a heat with ore reduction.
  • the object is achieved with the features of claim 1.
  • the further claims represent embodiments of the invention.
  • the solution is such that the reactor is constructed in such a way that, in principle, the physical heat is retained at a high temperature level with only minimal losses and is used to increase the chemically bound heat.
  • fuel and / or gas is initially at the outlet at the firing temperature the burner or at the entrance to the combustion chamber is rotated, which leads to the fact that hot droplets of slag are thrown against the wall and flow off to a slag pan at the bottom of the combustion chamber.
  • the combustion chamber wall is kept at such a temperature level that a layer of solidified slag melt forms on it, on which the further slag runs, for which purpose the (reflected) gasification gas flows around it on the outside.
  • the combustion chamber floor has a central opening from which the gas freed of the slag droplets emerges as a submerged jet and reaches the entrained-flow gasifier.
  • the slag running off the wall is collected in the trough surrounding the opening, which is preferably equipped with radial drainage channels, and flows parallel to the gas into the entrained-flow gasifier.
  • the gas outlet is designed as a channel, whereby the gasification gas is laminarized. This accomplishes two things.
  • the slag flowing off is accelerated towards the water bath at the foot of the carburettor
  • the gas exiting downwards into the carburetor remains in the form of a jet for a relatively long time, whereby it is braked above the water bath by compression effects and deflected upwards (reflected) is then to rise parallel to the immersion jet on the carburetor wall.
  • the carbon-containing fuel dust is blown into the descending gas jet, first taken with it in descending order and then reaches the gas section in the form of a jacket, the dimensions of the device and the flow rate being designed for extensive gasification of the fuel dust.
  • a jacket made of temperature-resistant steel or ceramic can be arranged around the gas outlet, through which the fuel dust can be fed through lances.
  • the rising gas arrives, for example, via a guide device in an intermediate space between an outer shell of the device and the jacket of the combustion chamber, causes a heat balance on this and leaves the device via the gasification gas outlet.
  • the device is provided with a heat protection lining and is preferably cooled.
  • the resulting gas is of high quality and can be used directly.
  • a combination burner 1 which receives hot, gaseous products of the smoldering, including the vaporous constituents such as tar, oil, water and dust at the inlet connection of the smoldering product channel 4 and guides them into the combustion chamber 9 via the swirl device 33.
  • Pipes for the supply of residual coke, ash and additives 8 are arranged in the reactor in the smoldering product channel of the combination burner, so that the mineral components to be melted in the combustion chamber 1 are also twisted, heated and flung in the combustion chamber 1 in liquid form to the wall.
  • the combination burner 1 has further supply channels for oxygen 7 or air 3, which, in the same way as the smoldering products via swirl devices 33, for rapid reaction with the smoldering products into a lubricant and for melting the mineral components of the residual coke, the ash and where appropriate, the supplements are introduced into the combustion chamber 1.
  • the pilot fuel supply 2, pilot air supply 5 and ignition device and ignition monitoring 6 necessary for starting and heating are installed in the combination burner, where these elements elements are protected from the other flowing media during stationary gasification operations.
  • the combustion chamber 9 is operated above the melting temperature of the mineral components of the residual coke, the ashes and the additives.
  • the wall of the combustion chamber 9 is thermally conductive, so that its slag solidifies to form a protective layer due to heat dissipation to the outside and liquid slag runs off due to the temperature in the combustion chamber 9.
  • the bottom of the reaction chamber 10 is designed as a Schiackeaufangwanne with incorporated drainage channels 12 so that a slag bath 13 can form, the slag flow through the gas outlet 34 through the direct contact of the slag with the gasifying agent 11 and through the direct current with the gasifying agent 11 always guaranteed.
  • the sensible heat introduced with the gasification agent 11 is used to cover the gas flow endothermic gasification reaction between fuel dust and gasification agent. Lances 15, 17 are therefore provided for the fuel dust in the reactor.
  • the gasification agent 11 enters the endothermic entrained-flow gasifier 14 as an immersion jet 16 and accelerates the entrained slag droplets 18 so that they are introduced into the water bath 19 and solidify there to form granules which are resistant to elution.
  • the slag discharge 22, the water inlet 21 and overflow 20 were provided for media removal and to supplement evaporated water. Together with the water bath 19, they form the lower end of the endothermic entrained flow reactor 14.
  • the immersion jet can also be stabilized and backmixing with the reflected gas rising in the shape of a jacket parallel to the wall can be prevented if a jacket 35 made of heat-resistant steel or ceramic is arranged beneath the gas outlet 34, through which the combustion dust lances 15 are passed. Additional lances 17 can be located below.
  • the construction carried out ensures by the supply of oxygen-free gasification agent 11 and fuel dust to be gasified in the endothermic entrained flow reactor 14 and by the high gasification temperature above 500 ° C. that no oxygen breakthrough can occur in cold reactor areas.
  • the heat equalization channel 26, in which guide devices 24 are located if necessary, serves to heat the gasification gas 23 cooled in the endothermic gasification. They impart a swirl swirl to the gasification gas stream 23, which increases the removal of convective heat from the wall of the combustion chamber 9 in such a way that the inner wall of the combustion chamber is cooled below the melting temperature of the slag, thereby forming a protective layer of solidified slag.
  • the cooling of the combustion chamber wall is intensified by the cooling device 27, which is supplied via coolant inlets and outlets 28, 29.
  • the device 30 for quenching the gasification gas is provided, to which quench nozzles 31 are mounted. The gasification gas leaves the reactor via the refractory-lined gasification gas outlet 25.
  • the reactor is provided with a fire-resistant delivery 32 for chemical and thermal protection. It is also designed with heat-resistant, corrosion-resistant material and thermal external insulation for pressures up to 10 MPa.
  • the lower part of the heat compensation channel 26 is designed conically.
  • CARL / FRITZ "NOELL CONVERSION PROCESS” EF publishing house for energy and environmental technology GmbH 1994
  • Combustion chamber 27 cooling device
  • Reaction space 28 coolant inlet

Landscapes

  • 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)
  • Processing Of Solid Wastes (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Treatment Of Sludge (AREA)
  • Industrial Gases (AREA)

Abstract

L'invention concerne un procédé et un dispositif permettant de produire des gaz de combustion, de synthèse et de réduction à partir de combustibles fossiles renouvelables, d'autres biomasses, d'ordures ou de boues, ces derniers étant largement séparés, avant leur introduction dans le réacteur, en produits gazeux et en solides, p.ex. en gaz dégagé de distillation lente et en charbon de bois, puis cédés séparément au réacteur. Selon l'invention, le réacteur comprend un brûleur mixte, une chambre de combustion, un gazéificateur de flux de particules, un canal de compensation de température et un bain d'eau. Le brûleur mixte dispose de dispositifs permettant la combustion substoechiométrique des produits gazeux dégagés de distillation lente et de dispositifs de rotation qui lancent par centrifugation les particules fluides sur la paroi de la chambre de combustion. Les gouttelettes de scories fluides tombent dans un bain d'eau. La poussière combustible peut réagir par endothermie avec l'agent de gazéification provenant de la chambre de combustion pour produire un gaz de gazéification. Le coke résiduel est amené à tourbillonner de telle façon qu'il ramène la température de la paroi de la chambre de combustion en-deçà de la température de fusion des scories par absorption thermique par convection. Il se forme alors une couche de protection de scories solidifiées sur la paroi interne de la chambre de combustion.
EP98949009A 1997-10-28 1998-10-06 Procede et dispositif de production de gaz de combustion, de gaz de synthese et de gaz de reduction a partir de combustibles solides Expired - Lifetime EP1027407B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19747324A DE19747324C2 (de) 1997-10-28 1997-10-28 Vorrichtung zur Erzeugung von Brenn-, Synthese- und Reduktionsgas aus nachwachsenden und fossilen Brennstoffen, Biomassen, Müll oder Schlämmen
DE19747324 1997-10-28
PCT/EP1998/006342 WO1999021940A1 (fr) 1997-10-28 1998-10-06 Procede et dispositif de production de gaz de combustion, de gaz de synthese et de gaz de reduction a partir de combustibles solides

Publications (2)

Publication Number Publication Date
EP1027407A1 true EP1027407A1 (fr) 2000-08-16
EP1027407B1 EP1027407B1 (fr) 2001-04-25

Family

ID=7846707

Family Applications (1)

Application Number Title Priority Date Filing Date
EP98949009A Expired - Lifetime EP1027407B1 (fr) 1997-10-28 1998-10-06 Procede et dispositif de production de gaz de combustion, de gaz de synthese et de gaz de reduction a partir de combustibles solides

Country Status (20)

Country Link
EP (1) EP1027407B1 (fr)
JP (1) JP4112173B2 (fr)
CN (1) CN1136299C (fr)
AR (1) AR010952A1 (fr)
AT (1) ATE200791T1 (fr)
AU (1) AU754147B2 (fr)
BR (1) BR9813292B1 (fr)
CA (1) CA2306889C (fr)
DE (2) DE19747324C2 (fr)
DK (1) DK1027407T3 (fr)
ES (1) ES2157673T3 (fr)
GR (1) GR3036233T3 (fr)
ID (1) ID21135A (fr)
MY (1) MY127842A (fr)
NO (1) NO328487B1 (fr)
PL (1) PL190794B1 (fr)
PT (1) PT1027407E (fr)
TW (1) TW518363B (fr)
WO (1) WO1999021940A1 (fr)
ZA (1) ZA989759B (fr)

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RO134445B1 (ro) * 2020-05-18 2021-06-30 Bogdan-Sabin Frâncu Procedeu şi instalaţie de gazeificare a amestecurilor eterogene de substanţe şi compuşi organici
WO2022040389A1 (fr) * 2020-08-19 2022-02-24 The Regents Of The University Of California Réaction chimique et conversion dans des réacteurs chimiques thermiquement hétérogènes et à l'état non stable

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EP1027407B1 (fr) 2001-04-25
DE59800654D1 (de) 2001-05-31
NO20001993L (no) 2000-06-15
AU9542798A (en) 1999-05-17
PT1027407E (pt) 2001-10-30
CA2306889C (fr) 2008-12-16
AR010952A1 (es) 2000-07-12
DK1027407T3 (da) 2001-08-13
TW518363B (en) 2003-01-21
DE19747324C2 (de) 1999-11-04
CN1278292A (zh) 2000-12-27
PL190794B1 (pl) 2006-01-31
BR9813292A (pt) 2000-08-22
CN1136299C (zh) 2004-01-28
JP4112173B2 (ja) 2008-07-02
JP2001521056A (ja) 2001-11-06
PL340217A1 (en) 2001-01-15
DE19747324A1 (de) 1999-04-29
NO20001993D0 (no) 2000-04-17
ATE200791T1 (de) 2001-05-15
ID21135A (id) 1999-04-29
BR9813292B1 (pt) 2009-12-01
CA2306889A1 (fr) 1999-05-06
ZA989759B (en) 1999-05-03
GR3036233T3 (en) 2001-10-31
NO328487B1 (no) 2010-03-01
MY127842A (en) 2006-12-29
ES2157673T3 (es) 2001-08-16
AU754147B2 (en) 2002-11-07
WO1999021940A1 (fr) 1999-05-06

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