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EP0227196B1 - Oxydation de cendres volantes - Google Patents

Oxydation de cendres volantes Download PDF

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Publication number
EP0227196B1
EP0227196B1 EP19860202365 EP86202365A EP0227196B1 EP 0227196 B1 EP0227196 B1 EP 0227196B1 EP 19860202365 EP19860202365 EP 19860202365 EP 86202365 A EP86202365 A EP 86202365A EP 0227196 B1 EP0227196 B1 EP 0227196B1
Authority
EP
European Patent Office
Prior art keywords
coal
flyash
gasification
zone
heated gases
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
Application number
EP19860202365
Other languages
German (de)
English (en)
Other versions
EP0227196A2 (fr
EP0227196A3 (en
Inventor
Donald Ernest Hardesty
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.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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 Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0227196A2 publication Critical patent/EP0227196A2/fr
Publication of EP0227196A3 publication Critical patent/EP0227196A3/en
Application granted granted Critical
Publication of EP0227196B1 publication Critical patent/EP0227196B1/fr
Expired 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
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • 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
    • C10J3/46—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
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/78—High-pressure apparatus
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/30—Solid combustion residues, e.g. bottom or flyash

Definitions

  • the invention relates to a process for the gasification of coal to produce synthesis gas comprising the steps of
  • flyash unreacted or impurity matter
  • the flyash Separation of the flyash from the synthesis gas creates a disposal problem, since the flyash has undesirable properties which limit options for its disposal.
  • the flyash contains, in addition to mineral matter or components, a residual carbon content that has substantial energy value.
  • the flyash may contain from about 3 per cent by weight to about 30 per cent by weight of residual carbon. If the flyash is disposed of, e.g. by land fill, this energy value is lost. Accordingly, a procedure which captured this energy value, at the same time reducing the volume of material to be disposed of, could have great economic importance.
  • coal is dried to remove the bulk of the moisture therein before gasification, the removal of this moisture involves a significant energy expenditure. If coal is combusted to provide the heat necessary for the drying, from about 2 per cent to about 12 per cent by weight of the total coal supplied to the process may be utilized, thus lowering the efficiency of the process. The invention is directed to reducing this energy expenditure.
  • the process of the invention is characterized in that the heat in said heated gases is used either directly or indirectly to dry the coal to be fed to the gasification zone.
  • DE-A-2 729 764 discloses the oxidation of separated flyash in a separate fluidized bed, wherein the combustion gas from the flyash is directly fed to a gasification reactor and is used as additional gasifying medium and heat carrier within said gasification reactor. There is no indication at all, however, in this reference that the combustion gas from the flyash could be applied for other purposes, in particular outside the gasification reactor.
  • the heat in said heated gases is utilized by contacting the heated gases directly with moist feed coal to remove the moisture from the coal before gasification.
  • the heat in said heated gases is utilized by contacting moist feed coal with a solid or gas heated directly or indirectly by said heated gases.
  • the invention comprises a process, as described, in which the partial oxidation or gasification is carried out in a gasification zone, the outlet temperature of which is from 1100 ° C to 1800 ° C, more advantageously 1200 ° C to 1600 ° C, the stream produced is quenched and cooled to a temperature of from 650 °C to 145 ° C, and flyash separated is oxidized in a fluidized bed in a fluidization zone at a temperature of from 500 °C to 1150 ° C, more advantageously 650 ° C to about 1120 ° C.
  • Pressures in the gasification zone may be varied widely, but will for example, range from 10 to 100 atmospheres, more advantageously from 20 to 50 atmospheres, while pressures in the fluidization zone will range from atmospheric to 10 atmospheres or higher.
  • the invention relates to a process for the gasification of coal to produce synthesis gas in which particulate coal is dried in at least one drying zone, the coal is fed from at least one drying zone to a gasification zone, and partially oxidized or combusted, as hereinbefore described, to produce synthesis gas and flyash, which is treated as described, and the heat generated by oxidizing the flyash is utilized in drying coal in at least one drying zone.
  • flyash refers to matter carried out of the gasification zone by the synthesis gas, including unconverted coal particles, partially converted particles, and molten matter which solidifies as discrete particles in the quench or cooling stages of the process.
  • oxygen is taken herein to include air, pure oxygen, air enriched with oxygen, and other oxygen-containing gases.
  • the invention is particularly applicable to high pressure slagging coal gasification processes in which the coal is partially oxidized or combusted to produce, in addition to the synthesis gas and the flyash, a bottom materials variously known as char, fine slag, and coarse slag, which are removed separately from the gasification zone.
  • the oxygen and coal flows are controlled so that lit- tie C0 2 is produced in the gaseous product.
  • these procedures are carried out by feeding coal, advantageously dry coal, e.g., coal having a moisture content of below ten percent by weight, entrained in a gas, such as an inert gas, into a gasification zone, and combusting or oxidizing the coal with oxygen.
  • Flame temperatures may reach 3500 ° C, with zone outlet temperatures ranging from 1100 °C to 1800 °C.
  • Pressures in these processes may vary, but will advantageously range from 10 atmospheres to 100 atmospheres, more advantageously from 20 atmospheres to 50 atmospheres.
  • the synthesis gas and molten parti- des (which form flyash) are removed from the upper portion of the gasification zone, and the char, fine slag, and coarse slag are removed from the lower portion.
  • coals are suitable for use in the invention.
  • anthracite, bituminous coal, lignite, and so-called brown coal may be used in the invention.
  • a real advantage of the invention is the ability to use lower grade coals, such as lignite.
  • the term "coal” is taken to include these inferior grade carbonaceous fuels, as well as the higher quality coals.
  • the coal can be fed to the gasification zone in a particle size suitable for boiler furnace operation, e.g., 80 to 90 microns in diameter, although those skilled in the art may select the appropriate particle size, as desired.
  • the invention employs "dry" coal, that is, coal having a moisture content of less than 10 per cent by weight, based on the weight of the moist coal.
  • the synthesis gas and particles entrained therein are then subjected to various quench and cooling procedures, producing a synthesis gas stream containing flyash, the temperature of the stream produced being from about 650 ° C to 145 ° C. If the flyash is removed at this stage, the sensible heat therein may also be recovered. This may be done, for example, by separating the flyash in cyclone separators. If the temperatures are sufficiently low, bag filters may be used. However, it is within the scope of the invention to separate the flyash differently, e.g. by scrubbing with an aqueous stream. If this approach, or a combination of a cyclone and a scrubbing system is employed, the flyash will be separated from the aqueous stream, e.g., by filtration, before the utilization thereof in the manner of the invention.
  • the separated flyash is oxidized in a fluidization zone, comprising at least one fluidized bed, to remove the carbonaceous matter therein, producing a denser, more easily disposed of material.
  • the heat liberated during oxidation is used either directly or indirectly to dry the coal to be fed to the gasifier.
  • the amount of heat generated from the flyash will normally be insufficient to dry the large volume of coal needed for the process.
  • other combustible or partially combustible materials or fuels such as coal or coal fines, may be added to the fluidized bed and oxidized.
  • a separate drying technique may also be used, but it is an advantage of the invention that an independent dryer or drying zone may be eliminated.
  • the type of fluidized bed or beds employed is a matter of choice. What is required, however, is that the bed or beds be operated at a temperature below the fusion temperature of the mineral matter in the flyash, and of any mineral matter in the bed, including that of a coal or fuel supplement.
  • the mineral content of flyash comprises silica, alumina, and other inorganic components in varying quantities, and the melting point of this mixture may be determined routinely. Since these temperatures are normally above about 1482 ° C (although some may be less), problems with clogging will normally not be encountered if the bed is operated below this temperature.
  • the fusion temperature or range of temperatures may be determined routinely for each flyash or coal fuel utilized, and the temperatures in the fluidized bed may be controlled accordingly.
  • the temperatures are operated well below the fusion temperature, e.g., from 500 ° C to 1150 ° C, more advantageously from 650 ° C to 1120 °C.
  • Pressures in the fluidization zone may be varied, to the extent suitable for fluidized beds, but will for example range from atmospheric to 10 atmospheres, more advantageously from atmospheric to 5 atmospheres.
  • the fluidized bed or beds may be jacketed, or may have coils to absorb the heat produced by the oxidation.
  • the bed may contain other particulate matter, including catalysts.
  • the combustion gases generated are removed from the fluidization zone, and transfer their heat, either directly or indirectly, as desired, advantageously to the coal feed.
  • the coal is ground and dried in a combination procedure, and to allow conventional equipment to be used, a moderating gas, such as air or nitrogen, at a temperature of, for example, 15 °C to 40 ° C, is added to the combustion gases to lower the temperature to about 200 ° C to about 500 °C.
  • a moderating gas such as air or nitrogen
  • reference numeral (1) designates a supply line from, for example, a storage vessel, not shown, in which coal having an average particle size diameter of 1.3 cm is fed to a drying zone (2) which contains a combination pulverizer-dryer wherein the coal is crushed to an average particle size of from 80 to 90 microns and dried by the gas stream in a line (3) to a moisture content of about 10 per cent by weight, based on the weight of the moisture and the coal.
  • the gas stream in the line (3) has a temperature of about 250 ° C, contacts the coal directly in the combination pulverizer-dryer, and exits the drying zone (2) via a line (4).
  • the exit gas may be treated for control of pollutants, or utilized (not shown).
  • dried particulate coal is removed from the drying zone (2) through a line (5) and forwarded to a gasifier (6).
  • Means may be provided (not illustrated) for raising the pressure of the coal and entraining gas up to the level employed in the gasification zone.
  • the coal is injected in an entraining gas, e.g., nitrogen, through nozzles and combusted in a reducing atmosphere or partially oxidized with pure oxygen at 25 atmospheres and at a flame temperature of about 3400 ° C to about 3500 ° C.
  • Synthesis gas and impurity particles are removed overhead from the gasification zone at a temperature of about 1400 ° C, and sent to a quenching and cooling zone (7).
  • Char and slag which are heavier impurity materials, fall downward into the gasifier, and are removed from the lower portion thereof through a line A.
  • the quench and cooling zone (7) can be connected directly to the outlet of the gasifier (6).
  • the synthesis gas can first be quenched and cooled with cold recycle gas, if desirable.
  • the temperature of the synthesis gas is advantageously lowered to about 900 ° C, and molten impurities in the gas are solidified to what is known as flyash.
  • the quenching and cooling sequence can be carried out in more than one stage, the final temperature before separation of the flyash being from about 235 °C to about 320 ° C.
  • the stream is forwarded via a line (8) to a cyclone (9) (or the cooling zone may discharge directly thereto).
  • the great bulk of the flyash is separated in the cyclone (9), and the flyash is removed from the cyclone (9) via a line (10).
  • the gas stream is removed from the cyclone (9) via a line (11) and sent for further processing, such as for H 2 S removal, and for product use.
  • a final solids cleanup stage (12) e.g., bag filters, is provided in the line (11). Solids are removed from the unit (12) via a line (13). Solids from the cyclone (9) and the solids removal stage (12) are utilized for energy recovery according to the invention.
  • solids in the lines (10) and (13) are injected into a fluidized bed (14), and are reacted with oxygen in excess from a line (15) at a temperature of about 800 °C to about 900 °C, which is well below the fusion temperature of the mineral components of the bed.
  • the oxygen may serve as the fluidizing gas, or a separate fluidizing gas may be provided.
  • the substantially carbon-free residue may be removed via a line (16). Residence times of the solids will depend on the operating conditions, such as the temperatures, pressures, and specific equipment, and may be adjusted suitably by those skilled in the art.
  • the combustion gas is removed from the bed (14) via the line (3), and is utilized as described previously. Should the total carbon present in the flyash be insufficient for complete drying of the coal, as is normally the case, additional carbon-containing materials, such as coal fines, may be added to the fluidized bed (14) via a line (17).
  • a sample was heated in a quartz dish for at least one hour in air at 750 ° C in a muffle furnace.
  • the sample weighed 23.43 grams and had a volume of about 92 ml, thus having a bulk density of about 0.255 g/ml.
  • the sample weighed 17.72 grams, had a volume of about 40 ml., and a bulk density of about 0.443 g/ml.
  • the loss on ignition was 24.38 per cent by weight, based on the weight of the original sample.
  • zone includes, where suitable, the use of segmented equipment operated in series, or the division of one unit into multiple units to improve efficiency or overcome size constraints, etc.
  • multiple gasification reactors may be employed, and only one or more need supply flyash to the fluidization zone described herein, a series of cyclones may be employed, and the quench and cooling operations are preferably carried out in multiple units, utilizing different techniques.
  • Parallel operation of units is, of course, well within the scope of the invention, and all equipment, such as pumps, valves, control units, etc., has not been illustrated.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Claims (3)

1. Procédé de gazéification du charbon pour produire du gaz de synthèse, comprenant les étapes qui consistent à
charger du charbon particulaire dans une zone de gazéification et oxyder partiellement le charbon avec de l'oxygène dans ladite zone de gazéification, pour produire un courant comprenant du gaz de synthèse et des cendres volantes;
éteindre et refroidir le courant et séparer les cendres volantes du courant, pour produire des cendres volantes séparées;
fluidiser les cendres volantes séparées dans un lit fluidisé dans une zone de fluidisation et oxyder lesdites cendres volantes dans ledit lit fluidisé avec de l'oxygène à une température inférieure à la température de fusion des constituants minéraux des cendres volantes et du lit fluidisé, pour produire un résidu essentiellement exempt de carbone et des gaz chauffés, caractérisé en ce que la chaleur dans lesdits gaz chauffés est utilisée directement ou indirectement pour sécher le charbon à charger dans la zone de gazéification.
2. Procédé selon la revendication 1, caractérisé en ce que la chaleur dans lesdits gaz chauffés est utilisée par mise en contact des gaz chauffés directement avec le charbon humide de la charge pour éliminer l'humidité du charbon avant la gazéification.
3. Procédé selon la revendication 1, caractérisé en ce que la chaleur dans lesdits gaz chauffés est utilisée par mise en contact du charbon humide de la charge avec un solide ou un gaz chauffé directement ou indirectement par lesdits gaz chauffés.
EP19860202365 1985-12-27 1986-12-23 Oxydation de cendres volantes Expired EP0227196B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US81373785A 1985-12-27 1985-12-27
US813737 1985-12-27

Publications (3)

Publication Number Publication Date
EP0227196A2 EP0227196A2 (fr) 1987-07-01
EP0227196A3 EP0227196A3 (en) 1988-01-20
EP0227196B1 true EP0227196B1 (fr) 1990-08-08

Family

ID=25213243

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19860202365 Expired EP0227196B1 (fr) 1985-12-27 1986-12-23 Oxydation de cendres volantes

Country Status (2)

Country Link
EP (1) EP0227196B1 (fr)
DE (1) DE3673362D1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7462235B2 (en) 2006-05-03 2008-12-09 Progress Materials, Inc. System and method for decomposing ammonia from fly ash
US7641878B2 (en) 2006-02-21 2010-01-05 Pmi Ash Technologies, Llc Fly ash beneficiation systems with sulfur removal and methods thereof
US7670424B2 (en) 2007-01-19 2010-03-02 Pmi Ash Technologies, Llc Methods for reclaiming and beneficiating fly ash particles and systems thereof
US7867462B2 (en) 2006-09-25 2011-01-11 Pmi Ash Technologies, Llc Coal combustion systems with emissions control and fly ash beneficiation and methods thereof
US8545598B2 (en) 2007-06-19 2013-10-01 Pmi Ash Technologies, Llc Mercury removal systems using beneficiated fly ash particles and methods thereof

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5160539A (en) * 1991-04-05 1992-11-03 Progress Materials Inc. Method and product of fly ash benefication by carbon burnout in a dry bubbling fluid bed
DE19544200A1 (de) * 1995-11-28 1997-06-05 Metallgesellschaft Ag Verfahren zum Behandeln von Abgas aus der Vergasung von kohlenstoffhaltigem Material
KR20010024644A (ko) * 1997-11-14 2001-03-26 엠 제이 에프 석탄의 기화 방법
EP1230515B1 (fr) * 1999-11-02 2006-12-27 Consolidated Engineering Company, Inc. Procede et appareil permettant la combustion du charbon residuel contenu dans des particules de cendres volantes
US7047894B2 (en) 1999-11-02 2006-05-23 Consolidated Engineering Company, Inc. Method and apparatus for combustion of residual carbon in fly ash
EA022252B1 (ru) * 2009-07-08 2015-11-30 Семекс Рисерч Груп Аг Способ и устройство для обогащения частиц золы уноса путем мгновенного сжигания
FI124206B (fi) * 2012-09-13 2014-05-15 Valmet Power Oy Menetelmä tuhkan käsittelemiseksi ja tuhkan käsittelylaitos
CZ307092B6 (cs) * 2013-09-20 2018-01-10 Svoboda A Syn, S.R.O. Žíhací pec
CN110628463B (zh) * 2019-10-28 2025-01-24 安徽科达洁能股份有限公司 一种煤气发生炉混合布风系统及工作方法

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Publication number Priority date Publication date Assignee Title
US2633417A (en) * 1947-12-03 1953-03-31 Standard Oil Dev Co Gasification of carbonaceous solids
GB1473395A (en) * 1973-09-13 1977-05-11 Parsons Co Ralph M Gasification of carbonaceous material
DE2729764A1 (de) * 1977-07-01 1979-01-04 Davy Bamag Gmbh Verfahren zur vergasung von kohlenstoffhaltigem material
DE3113993A1 (de) * 1981-04-07 1982-11-11 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur gleichzeitigen erzeugung von brenngas und prozesswaerme aus kohlenstoffhaltigen materialien

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7641878B2 (en) 2006-02-21 2010-01-05 Pmi Ash Technologies, Llc Fly ash beneficiation systems with sulfur removal and methods thereof
US7462235B2 (en) 2006-05-03 2008-12-09 Progress Materials, Inc. System and method for decomposing ammonia from fly ash
US7867462B2 (en) 2006-09-25 2011-01-11 Pmi Ash Technologies, Llc Coal combustion systems with emissions control and fly ash beneficiation and methods thereof
US7670424B2 (en) 2007-01-19 2010-03-02 Pmi Ash Technologies, Llc Methods for reclaiming and beneficiating fly ash particles and systems thereof
US8545598B2 (en) 2007-06-19 2013-10-01 Pmi Ash Technologies, Llc Mercury removal systems using beneficiated fly ash particles and methods thereof

Also Published As

Publication number Publication date
DE3673362D1 (de) 1990-09-13
EP0227196A2 (fr) 1987-07-01
EP0227196A3 (en) 1988-01-20

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