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CN1278292A - Method and apparatus for producing combustible, synthetic and reducing gases from solid fuels - Google Patents

Method and apparatus for producing combustible, synthetic and reducing gases from solid fuels Download PDF

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Publication number
CN1278292A
CN1278292A CN98810657A CN98810657A CN1278292A CN 1278292 A CN1278292 A CN 1278292A CN 98810657 A CN98810657 A CN 98810657A CN 98810657 A CN98810657 A CN 98810657A CN 1278292 A CN1278292 A CN 1278292A
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CN
China
Prior art keywords
combustion chamber
gas
fuel
reactor
slag
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
CN98810657A
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Chinese (zh)
Other versions
CN1136299C (en
Inventor
博多·沃尔夫
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Linde GmbH
Choren Industries GmbH
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Individual
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Publication of CN1278292A publication Critical patent/CN1278292A/en
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Publication of CN1136299C publication Critical patent/CN1136299C/en
Anticipated expiration legal-status Critical
Expired - Fee Related 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
    • C10J3/46—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

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

Abstract

The invention relates to a method and a device for producing combustible gases, synthesis gases and reducing gases from renewable and fossil fuels, other biomass, waste or coal slime, wherein the combustible gases, synthesis gases and reducing gases are separated into gaseous and solid products, such as low-temperature carbonization gases and charcoal, before being fed into a reactor, and are fed into the reactor separately. The liquid small slag drops into the water tank. The pulverized fuel can react endothermically with the gasifying agent from the combustion chamber to form gasified gas, and the remaining coke swirls so that it lowers the temperature of the combustion chamber wall to below the melting point of the slag by convective heat absorption, in which case a protective layer of solidified slag forms on the combustion chamber inner wall.

Description

Make the method and apparatus of inflammable gas, synthesis gas and reducing gas by solid fuel
The present invention relates to make the method and apparatus of inflammable gas, synthesis gas and reducing gas by reproducible and mineral fuel, other biological amount, rubbish or coal slime, be preferably used for by these split products by patent DE 4404673 productions, in this case, if use split product, before their input reactors, as far as possible they are separated into solid and gaseous product, for example low-temperature pyrolysis gas and charcoal are distinguished input reactor then.
Can use in power facility, chemical industry and metallurgy by equipment of the present invention,, be used for engine, building-up process, ore reduction and pig iron production to make inflammable gas, synthesis gas and reducing gas efficiently.
Have considerable gasification process, they can be divided into fixed bed gasification, fluidized-bed gasification and flow type pump with injection gasification three major types basically.In equipment for gasification, especially in equipment, must aspect energy and in the vaporized chemical demand side, make many compromises here by the gasification of the flow type pump with injection under the equipment of the present invention class.The most single stage type operation of the flow type pump with injection gasifier of melting mineral component that is to say that all participate in the medium of gasification reaction and all import a reaction chamber.Therefore, all media are brought up to the temperature levels that is higher than mineral constituent slag melting point in the fuel.At reactor wall and to have in the reactor of reactor wall of cooling screen lining-up be this situation with refractory masonry.In having the reactor of cooling screen, this is typical (seeing document (1,2)) in GSP flow type pump with injection reactor, and gasifying gas overwhelming majority sensible heat looses to cooling stave.In addition, to the co-current reactor of water vapor temperature of saturation,, all there is a lot of heats to be reduced to low available energy level in the quenching of gasifying gas water no matter whether the cooled reactor wall is arranged.Under situation, and upwards leave reactor and liquid slag at gasifying gas and leave downwards under the situation of countercurrent reactor of reactor, must keep the discharge of slag to the additional combustion device by additional heat or its with cooled radiator inwall.These measures cause a large amount of oxygen of needs, reduce the calorific value of gasifying gas and thereby cause the low exothermal efficiency of whole gasification.But if do not take these preventive measures, then can destroy the work of gasifier, because can not keep flowing of slag.
Especially in the flow type pump with injection reactor of oxygen as vaporized chemical work, the residence time of reactive component is very short.Oxygen burns lining-up when the fuel crunch in order to avoid, and must pay very high measurement and monitoring expense.
The shortcoming of supplying with the flow type pump with injection reactor of independent cracked fuel is, split product is cooled before infeeding reactor, except thermosteresis, for gas purchase and the processing of liquid product incurs great expense.
The purpose that the present invention will reach is a kind of method of suggestion and a kind of reactor, compare them works under lower medial temperature level and higher exothermal efficiency with prior art, and generation does not have hydrocarbon polymer and chlorinated hydrocarbon (dioxine, furans) gasifying gas, it can be used to generating as inflammable gas, can be used in the heating phase of ore reduction as synthesis gas or reducing gas.
Reach by the feature of this purpose of the present invention by claim 1.Other claims have illustrated embodiments of the invention.Implement this solution in such a way, that is, reactor design is for increasing chemical combination heat with physics heat having only to remain on high temperature levels under the situation of minimum loss and be used in principle.For this reason, fuel and/or gas at first make it rotation in burner outlet or combustion chamber ingress under temperature of combustion, the little slag of heat are dripped flow to towards the wall centrifugation and on wall the slag bath in the bottom, combustion chamber.Meanwhile, combustion chamber wall remains on such temperature levels, promptly forms a molten slag layer that solidifies on it, and slag afterwards flows through on this slag blanket and washed away by (reflection) gasifying gas in its outside.
One centre hole is arranged at combustion chamber bottom, the gas that drips release from little slag as submerged jet from then on centre hole escape and enter the flow type pump with injection gasifier.The slag that flows down on wall is collected in the pond in this hole, and slag bath preferably is equipped with radially deslagging irrigation canals and ditches, and slag is parallel to gas inflow flow type pump with injection gasifier.Here pneumatic outlet is designed to passage, makes the gasifying gas stratification whereby.So reached two kinds of purposes.Effusive slag is quickened towards the tank direction in the gasifier lower end, the gas that enters downwards on the other hand in the gasifier keeps the long period as jet, jet because compressiblity influence slows down voluntarily and upwards turns to (reflection), rises along gasifier wall so that then be parallel to submerged jet above tank in this case.Carbonaceous pulverized fuel is blown under reductive condition in the gas-jet of decline, at first is being with to descend, and enters then in the gas part of housing type rising, and here the size of equipment and flow velocity are designed to make basically the pulverized fuel gasification.
Oppositely mix with the jet of discharging for the gas part that stops rising, establish the overcoat of usefulness high temperature steel or pottery system round pneumatic outlet, pulverized fuel can pass overcoat by jet pipe and infeed.
Ascending gas causes thermal equilibrium here and leaves this equipment by the gasifying gas outlet for example via in the space between guidance device access arrangement shell and the combustion outer case.
Equipment is provided with insulating inner lining and preferred cooling.
The gaseous mass that produces is high also can directly be used.
Before the gas that rises entered the thermal equilibrium passage, it for example can be by water spray or cooling gas quenching under unstable working state.
Further specify the present invention by means of accompanying drawing with reference to embodiment below.
Use combination burner 1 here, it receives the gaseous state low-temperature pyrolysis product of heat at the inlet connection place of low-temperature pyrolysis product passage 4, comprise vaporific component, as tar, oil, water and powder, and by slewer 33 introducing combustion chambers 9.In combination burner low-temperature pyrolysis product passage, be provided with the pipe that is used for residual coke, ash and additive 8 input reactors, so as the mineral constituent band that will in combustion chamber 1, melt together reverse, heat and in combustion chamber 9 with liquid state towards the wall throwing.Be vaporized chemical in order more than ash fusion point, to be lower than the burning of stoichiometry ground, combination burner 1 also has the input channel of oxygen 7 or air 3, they introduce combustion chamber 9 with the direction identical with the low-temperature pyrolysis product by slewer 33, are used for being converted into vaporized chemical fast and being used to melt residual coke, ash and the mineral constituent of additive in case of necessity with the low-temperature pyrolysis product.In order to prevent not enter too much heat in the refrigerative member; starting and heat required igniter fuel input unit 2, igniting air input unit 5 and lighter for ignition and igniting monitor 6 and be contained in together in the combination burner, these members are protected with other flow medias when the gasification operation of stable state there.
Also can use the known turbulence type burner that is used for firing coal dust.
Combustion chamber 9 is moved more than the fusing point of the mineral constituent of residual coke, ash and additive.The wall of combustion chamber 9 is heat conduction, so slag is frozen into a protective layer owing to outwards dispel the heat on wall, and flows through liquid slag based on the temperature in the combustion chamber 9 on this protective layer.The bottom design of reaction chamber 10 is the collection slag bath of the superincumbent deslagging irrigation canals and ditches 12 of band processing, so that can constitute slag chute 13, even because slag directly contact with vaporized chemical 11 and owing to also also flow with vaporized chemical 11 when passing pneumatic outlet 34, so slag chute can guarantee the mobile of slag all the time.The vaporized chemical 11 that generates under substoichiometric gasification condition in combustion chamber 9 is because it is adjusted into high CO 2And H 2O content is used as vaporized chemical in the flow type pump with injection gasifier 14 of heat absorption.Satisfy the needs of the gasification reaction that absorbs heat between pulverized fuel and the vaporized chemical with the sensible heat utilization of vaporized chemical 11 addings.Therefore be provided with the jet pipe 15,17 of pulverized fuel being sent into reactor.Vaporized chemical 11 enters the flow type pump with injection gasifier 14 of heat absorption as submerged jet 16 and makes the little slag of carrying secretly drip 18 and quickens, and they is entered in the tank 19, and be frozen into the granular solid of energy elution there.Be provided with slag-drip opening 22, feed water inlet 21 and water overflow port 20, be used for deslagging and replenish the water that evaporates.They are with the lower end of the flow type pump with injection reactor 14 of tank 19 formation heat absorptions.
Submerged jet is stabilization and mixes and can prevent with the direction that wall is the housing type ascending gas that is parallel to of reflection further, as long as establish the overcoat 35 that a usefulness high temperature steel or pottery are made below pneumatic outlet 34, pulverized fuel jet pipe 15 passes this overcoat.Other jet pipe 17 can be positioned at below it.
Designed structure guarantees can not take place oxidation and burns by vaporized chemical 11 that infeeds anaerobic in the flow type pump with injection reactor 14 of heat absorption and the pulverized fuel that will gasify and by gasification temperature high more than 500 ℃ in cold reactor zone.
Thermal equilibrium passage 26 is used to heat the gasifying gas 23 that is cooled in the endothermic gasification process, is provided with guidance device 24 in this passage in case of necessity.They make gasification air-flow 23 produce vortexs, strengthen from the combustion chamber 9 wall and discharge convection heat, make the combustion chamber inwall be cooled to be lower than the fusing point of slag and cause the protective layer that is made of the slag that solidifies thus.The cooling of strengthening combustion chamber wall by means of refrigerating unit 27 in addition, it is provided with coolant inlet and outlet 28,29.For gasification temperature being reduced between 500-1200 ℃ that should be in, the device 30 that makes the gasifying gas quenching is set, on this device, quenching nozzle 31 is installed.Gasifying gas leaves reactor through the gasifying gas outlet 25 that refractory liner is arranged.
Adopt the design of another kind of staged reactor, can significantly expand the range of application of reactor.For example, by changing residual coke/ash and pulverized fuel jet pipe 8,15,17, part combination burner and quenching nozzle 31, provide the possibility fusing external possible contaminated mineral substance, but also can melt ore, and the fine-grannular fuel that gasifies external, the inflammable gas of utilization itself or the external delivering gas that is used to measure, or with different media such as water, water vapour or cooling gas quenching.
A kind of collection 9 designs of flowing out the groove be in liquid melt from the combustion chamber also can be provided, and its replaces the lower end that tank 19 constitutes the flow type pump with injection gasifier 14 of heat absorption.
For chemistry and thermal protection, reactor is established fire-resistant lining-up 32.But it also can and have withstand voltage outer heat-proof device to 10MPa with the design of heat resisting corrosion-proof material.
For prevent combustion chamber 9 burn the heat absorption flow type pump with injection gasifier 14 in, the bottom of thermal equilibrium passage 26 is designed to taper shape.
Document:
〔1〕CARL/FRITZ：“NOELL-KONVERSIONSVERFAHREN”
EF-Verlag?für?Energie-und?Umwelttechnik?GmbH?1994
〔2〕LUCAS?u.a.：“Ein?Vergleich?von?Kohlevergasungsverfahren
unter?Druck?in?der?Flugstaubwolke”Chemische?Technik?1988，
Heft?7，Seite?277-282

Claims (22)

  1. By reproducible and mineral fuel, other biological amount, rubbish or coal slime by in burner, adding gaseous oxygen and/or oxygen-containing gas and more than the inorganic components fusing point, burn and become to contain CO by being lower than stoichiometric ratio 2And H 2The vaporized chemical of O is made the method for inflammable gas, synthesis gas and reducing gas, it is characterized by:
    -fuel and/or gas cause spin in entering the combustion chamber time, and the liquid state that produces during burning expands burner wall throwing that the thing component arranges towards perpendicular and separates with the vaporized chemical that here produces;
    -vaporized chemical is introduced gasifying reactor by the centre hole of bottom, combustion chamber, and forms submerged jet in this process;
    -isolating liquid composition is dripped by the vaporized chemical submerged jet by the centre hole discharge of bottom, combustion chamber and as little slag and is carried secretly towards the reactor bottom acceleration, assembles there and bottom derivation from then on;
    -carbonaceous pulverized fuel infeeds vaporized chemical in gasifier, and in gasification reaction process subsequently, carbon dioxide reduction is that carbon monoxide and water vapor are reduced to hydrogen;
    -gas submerged jet turns to above reactor bottom, and the gasifying gas of generation is discharged on reactor top, and is prepared into inflammable gas, synthesis gas or reducing gas by follow-up dedusting and chemical purification.
  2. 2. in accordance with the method for claim 1, it is characterized by: he thermally or autothermally is heated to be 300 to 800 ℃ fuel, product was separated into gaseous state and solid carbonaceous fuel before infeeding the combustion chamber in this case, as low-temperature pyrolysis gas and charcoal, then imported this process respectively.
  3. 3. according to claim 1 or 2 described methods, it is characterized by: solid carbon fuel pulverize fuel.
  4. 4. according to the described method of one of claim 1 to 3, it is characterized by: the part of burning institute heat requirement obtains by the heat exchange with gasifying gas and/or inflammable gas, synthesis gas or reducing gas.
  5. 5. in accordance with the method for claim 4, it is characterized by: gasifying gas is by the guiding of the cavity between reactor wall and the outer wall of combustion chamber, and absorption will be from the part heat of combustion chamber discharge.
  6. 6. according to claim 5 or 6 described methods, it is characterized by: the gasifying gas of heat is before the cavity that enters between reactor wall and the outer wall of combustion chamber or at this cavity internal cooling.
  7. 7. according to the described method of one of claim 1 to 6, it is characterized by: slag concentrates on the interior and discharge from here of tank of reactor bottom.
  8. 8. it is characterized by in accordance with the method for claim 6: cooling directly realizes by water, water vapor and/or cooling gas quenching or by means of the cooling surface that is connected with reactor wall or its liner.
  9. 9. according to the described method of one of claim 1 to 8, it is characterized by: mineral substance that adds and/or ore are added in the carbonaceous solid fuel and fusing when burning.
  10. 10. according to the described method of one of claim 3 to 14, it is characterized by: the particulate fuel that adds is added in the pulverized fuel.
  11. 11., it is characterized by: preferred directly being blown in the submerged jet of pulverized fuel in the bottom, combustion chamber below by one or more jet pipe according to the described method of one of claim 1 to 10.
  12. 12. according to the described method of one of claim 1 to 11, it is characterized by: slag concentrates in the collection slag bath of bottom, combustion chamber, and by deslagging irrigation canals and ditches input centre hole.
  13. 13. implement equipment according to the described method of claim 1 to 12, comprise that a combination burner (1) and one are located at the combustion chamber (9) that has fuel and gas (2,3,4,5,7,8) input unit below it, its characteristics are following feature:
    A) (9) head is established slewer (33) in the combustion chamber, and fuel and gas are guided the pneumatic outlet (34) that is positioned at the combustion chamber bottom center from combination burner (1) downwards into through slewer;
    B) pneumatic outlet (34) upper end is centered on by a slag bath (12);
    C) be provided with a flow type pump with injection gasifier (14) that comprises the heat absorption of slag bath (19) and slag-drip opening (22) in pneumatic outlet (34) below;
    D) establish the granular fuel nozzle (15) that extends in the gasifier (14) in pneumatic outlet (34) below.
  14. 14. according to the described equipment of claim 13, it is characterized by: the pneumatic outlet (34) in flow type pump with injection gasifier (14) upper zone of heat absorption is centered on by the overcoat of heat-stable material system (35).
  15. 15. according to claim 13 or 14 described equipment, it is characterized by: establish top pulverized fuel jet pipe (15) and bottom pulverized fuel jet pipe (17), its middle and upper part powdery burning jet pipe (15) passes overcoat (35).
  16. 16. according to the described equipment of one of claim 13 to 15, it is characterized by: the flow type pump with injection gasifier (14) of heat absorption is centered on by insulating inner lining (32).
  17. 17. according to the described equipment of one of claim 13 to 16, it is characterized by: insulating inner lining (32) is separated by a distance ground around combustion chamber (9), and it is the hot average channel (26) of annular chamber that this spacing constitutes one in form.
  18. 18. according to the described equipment of one of claim 13 to 17, it is characterized by: insulating inner lining (32) is established refrigerating unit (27) in the zone of combustion chamber (9).
  19. 19., it is characterized by: in annular chamber or hot average channel (26), establish guidance device (24) according to the described equipment of one of claim 13 to 18.
  20. 20., it is characterized by: in the upper zone of flow type pump with injection gasifier (14) of heat absorption and/or in the thermal equilibrium passage, establish chilling apparatus (30) according to the described equipment of one of claim 13 to 19.
  21. 21., it is characterized by according to the described equipment of one of claim 13 to 20; Slag bath (12) is designed to taper shape and the deslagging irrigation canals and ditches is arranged.
  22. 22. according to the described equipment of one of claim 13 to 21, it is characterized by: combustion chamber (9) bottom design is that taper and flow type pump with injection gasifier (14) have the anti-cone of burning device as anti-, and its standoff distance ground is around the bottom, combustion chamber.
CNB988106574A 1997-10-28 1998-10-06 Method and device for producing combustible gas, synthesis gas and reducing gas from solid fuel Expired - Fee Related CN1136299C (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19747324.5 1997-10-28
DE19747324A DE19747324C2 (en) 1997-10-28 1997-10-28 Device for generating fuel, synthesis and reducing gas from renewable and fossil fuels, biomass, waste or sludge

Publications (2)

Publication Number Publication Date
CN1278292A true CN1278292A (en) 2000-12-27
CN1136299C CN1136299C (en) 2004-01-28

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

Cited By (11)

* Cited by examiner, † Cited by third party
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CN100467578C (en) * 2001-07-09 2009-03-11 考尔德伦合成气公司 A way to generate clean energy from coal
CN1935951B (en) * 2006-09-21 2010-12-08 武汉凯迪工程技术研究总院有限公司 High temperature gasifying apparatus for solid carbon raw material
CN101283076B (en) * 2005-10-14 2013-04-24 国际壳牌研究有限公司 Improvements relating to coal to liquid processes
CN103484162A (en) * 2012-06-12 2014-01-01 通用电气公司 System for initiating a gasification reaction in a gasifier
CN104403694A (en) * 2014-10-16 2015-03-11 煤炭科学技术研究院有限公司 Liquid-state continuous slag discharge device and slag discharge method of fixed bed gasification furnace
CN101331213B (en) * 2005-12-14 2015-05-13 国际壳牌研究有限公司 Method of controlling synthesis gas production
CN105482852A (en) * 2015-11-20 2016-04-13 新奥科技发展有限公司 Gasification furnace and hydrogasification method for coal
CN107129833A (en) * 2017-06-23 2017-09-05 航天长征化学工程股份有限公司 Annular pulverized coal cavity
CN107674712A (en) * 2017-11-13 2018-02-09 煤炭科学技术研究院有限公司 A kind of fixed bed slag gasification furnace
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